Cell culture improvements.
Abstract
The invention describes improved methods and compositions for producing a recombinant protein, e.g., an antibody, in mammalian cell culture. In addition, the invention provides improved cell culture media, including improved production media, feed solutions, and combination feeds, which may be used to improve protein productivity in mammalian cell culture.

Term
1 yearleft in the term
Expires 13 September 2027.
- Priority
- Filed
- Granted
- Today
- Expires
28 claims: 4 independent, 24 dependent
- 1CLAIMS REIVINDICACIONES IMPI IMPI INSTITUTO MSXICANO MSXICAN INSTITUTE DE LA PROHEDAD INDUSTRIAL OF INDUSTRIAL PROPERTY 1. Un método de lote alimentado para producir un anticuerpo anti-TNF-α humano que comprende una región variable de cadena ligera (LCVR) que comprende la secuencia SEQ ID NO:1 y una región variable de cadena pesada (HCVR) que comprende la secuencia SEQ ID NO:2, el método comprende cultivar células de Ovario de Hámster Chino (CHO) que comprenden un ácido nucleico que codifica la LCVR y la HCVR del anticuerpo anti-TNF-α en un medio de producción de cultivo celular a gran escala, en donde se monitorea la concentración de glucosa en el medio de producción celular, la concentración de glucosa en el medio disminuye por debajo de 2 g/L y se añade glucosa al medio cuando la concentración de glucosa en el medio disminuye por debajo de 2 g/L, o se monitorea la concentración de glucosa en el medio y se añade glucosa al medio para mantener la concentración de glucosa en el medio a una concentración de al menos 2 g/L pero no mayor de 7 g/L, de manera que se produce el anticuerpo anti-TNF-α, y en donde el anticuerpo producido se purifica adicionalmente por afinidad utilizando una resina de proteína A. one. A powered batch method of producing an anti-human TNF-α antibody comprising a light chain variable region (LCVR) comprising the sequence SEQ ID NO: 1 and a heavy chain variable region (HCVR) comprising the sequence SEQ ID NO: 2, the method comprises culturing Chinese Hamster Ovary (CHO) cells comprising a nucleic acid encoding the LCVR and HCVR of the anti-TNF-α antibody in a large-scale cell culture production medium, wherein the glucose concentration in the cell production medium is monitored, the glucose concentration in the medium decreases below 2 g / L and glucose is added to the medium when the glucose concentration in the medium falls below 2 g / L, or the glucose concentration in the medium is monitored and glucose is added to the medium to maintain the glucose concentration in the medium at a concentration of at least 2 g / L but not greater than 7 g / L, such that the anti-TNF-α antibody is produced, and wherein the produced antibody is further affinity purified using a protein A resin.
- 10A fed batch production method for producing adalimumab, which comprises cultivating Chinese Hamster Ovary (CHO) cells comprising a nucleic acid encoding adalimumab in a large-scale cell culture production medium, where the concentration of glucose in the medium, the concentration of glucose in the medium decreases by 10. Un método de producción de lote alimentado para producir adalimumab, que comprende cultivar células de Ovario de Hámster Chino (CHO) que comprenden un ácido nucleico que codifica adalimumab en un medio de producción de cultivo celular a gran escala, en donde se monitores la concentración de glucosa en el medio, la concentración de glucosa en el medio disminuye por 212 212 IMPI ^ IMPI^ INSTITUTO MEXICANO iC ^ΊΓ£χ DE LA PROPIEDAD debajo de 2 g/L, y se añade glucosa al medidNWCT^ndo¿2ta' concentración de glucosa en el medio disminuye ρδ Γ debajo der2 g7 L,1 o se monitorea la concentración de glucosa en el medio y se añade glucosa al medio para mantener la concentración de glucosa en el medio a una concentración de al menos 2 g/L pero no mayor de 7 g/L, de manera que se produce adalimumab, y en donde el adalimumab producido se purifica adicionalmente por afinidad utilizando una resina de proteína A. MEXICAN INSTITUTE iC ^ ΊΓ £ χ OF PROPERTY below 2 g / L, and glucose is added to the measureNWCT ^ ndo¿2ta 'concentration of glucose in the medium decreases ρδ Γ belowr2 g7 L,1 o The glucose concentration in the medium is monitored and glucose is added to the medium to maintain the glucose concentration in the medium at a concentration of at least 2 g / L but not greater than 7 g / L, so that adalimumab is produced , and wherein the produced adalimumab is further affinity purified using a protein A resin.
- 1717. El método de la reivindicación The method of claim IMPI® IMPI® INSTITUTO MEXICAI*’ MEXICAI INSTITUTE * ' 16, en don^e^S^c 16, in don ^ e ^ S ^ c
- 25A powered batch method of producing adalimumab, which comprises expressing adalimumab in Chinese Hamster Ovary (CHO) cells in a large-scale cell culture production medium, wherein the CHO cells comprise an expression vector encoding adalimumab, in where the glucose concentration in the medium is monitored, and the glucose concentration in the medium falls to a level between 1 and 5 g / L, and glucose is added to the medium to maintain the glucose concentration in the medium at least 1-5 g / L, and wherein adalimumab is further affinity purified using a protein A resin. 25. Un método de lote alimentado para producir adalimumab, que comprende expresar adalimumab en células de Ovario de Hámster Chino (CHO) en un medio de producción de cultivo celular a gran escala, en donde las células CHO comprenden un vector de expresión que codifica adalimumab, en donde se monitorea la concentración de glucosa en el medio, y la concentración de glucosa en el medio cae a un nivel entre 1 y 5 g/L, y se añade glucosa al medio para mantener la concentración de glucosa en el medio al menos 1-5 g/L, y en donde el adalimumab se purifica adicionalmente por afinidad utilizando una resina de proteína A.
Independent claims4
1,998 paragraphs in 128 sections, as filed
(54) Title: IMPROVEMENTS OF CELL CULTURES.
(54) Title: CELL CULTURE IMPROVEMENTS.
(57) Summary
The present invention relates to improved methods for producing a recombinant protein, for example an antibody, in a mammalian cell culture. Furthermore, the invention provides improved culture media, including improved production media, feeding solutions and combined solutions, which can be used to improve protein productivity in mammalian cell cultures. A fed batch production method of producing adalimumab, comprising culturing Chinese Hamster Ovary / CHO cells) comprising a nucleic acid encoding adalumimab in a large scale cell culture production medium, wherein the concentration of glucose in the medium, the concentration of glucose in the medium decreases below 2 g / L, and glucose is added to the medium when the concentration of glucose in the medium decreases below 2 g / L, o The glucose concentration in the medium is monitored and glucose is added to the medium to maintain the glucose concentration in the medium at a concentration of at least 2 g / L but not greater than 7 g / L, so that adalimumab is produced , and wherein the produced adalimumab is further affinity purified using a protein A resin.
(57) Abstract
The invention describes improved methods and compositions for producing a recombinant protein, eg, an antibody, in mammalian cell culture. In addition, the invention provides improved cell culture media, including improved production media, feed solutions, and combination feeds, which may be used to mprove prote in productivity n mammalian cell culture.
IMPI í
PATENT TITLE No. 353340
Headlines):
ABBVIE, INC.
Home:
North Waukegan Road, North Chicago, Illinois, 60064, USA
D nomination:
IMPROVEMENTS OF CELL CULTURES.
Classification:
CIP: CPC:
C07K16 / 24; C12N5 / 10; C12P21 / 08
C07K16 / 241; C07K16 / (> 65; C07K16 / Í44; C12N5 / 10
Inventor (s)
ITZCOATL A. PLA; JOSEPH C. MATUCK; JQHN C. FANN; CHRISTOF SCHULZ; NICOLE A. ROY; DAVID F. BRUTON,., JAMES MCINTIRE; YU- HSIANG DAVID CHANG; THOMAS SEEWOÍSTBé, '·' ·>
Number:
MX / a / 2017/0036
<img file="MX353340B_D0001.tif" />
<img file="MX353340B_D0002.tif" />
Number:
60/845,158
60/87.6,374
Country:
US US
Validity: Twenty years
Expiration date: 13
Shipping Date: January 9, 2018
The reference patent was otOteaton fundaffnentów.los- «T articles
In accordance with article 23 of the InrOustosrt Property Law. Tte ptésÉnte ^ Aé ^ has urte4®encia of twenty years non-extendable, counted from the date of filing dp YswSntntimactonal and expires subject to taritepara * lYianteoer.vlgentes the rights.
Who subscribes the present title hai? Íj | sor¡ # jn <iamentoep fadisíteesto por ^ piart! Cul8s 6 ° iraMoneS: lll jrtA bar2xlrte Industrial Property Law (Official Gazette of the Federation (D »F.) 7/08 / 1994 »· reformó pl OÍfOá / 1994,» ¿5/10/1986, 26/42 / ^ 07, 06/17/1999, 01/26/2004, 06/16/2005, 01/25/2006, 06 / 05 / 2009,06 / 01/2010, 18/06 / 2ΜΛ, 28/06 / 8010ζ 27 / O1 / 2 (Í12y-0WM / »H2), artícete» 4 °, 3 ° tácdóOV clause a), 4<sup>or</sup> and 12th sections I and III of the Regulations of the Mexican Institute of PMpiq & M WutteiaMBkftfe<sup>1</sup>-! ¢ 12 | 1ft82, _cateNaatte-8L <ft ^ 07ÍK) 02, 15/07/2004, 07/28/2004 and 09/07/2007); items 1<sup>or</sup>, 3 °, 4 °, 5 ° fraction V subsection a), 16 ftactíí & rír / tel tstetWwWltí ^ rfteH & tutorto Mexicano de la Propiedad Industrial (DOF
12/27/1999, amended on 10/10/2002, 07/29/2004, 04/080 »4 <13 * tempted *» 5 ”Agreement that delegates powers to the Directors
Deputy Generals, Coordinator, Divisional Directors, Titul RL ^ sR8tficinasTRegionales, Divisional Subdirectors, Departmental Coordinators and other subordinates of the Mexican Institute of Industry. (DOF 12/15/1999, amended on 02/04/2000, 07/29/2004, 08/04/2004 and 09/13/2007).
This letter is signed with an advanced electronic signature (FIEL), based on articles 7 BIS 2 of the Industrial Property Law; 3 of its Regulations, and 1 fraction III, 2 fraction V, 26 BIS and 26 TER of the Agreement establishing the guidelines for the use of the Electronic Payment and Services Portal (PASE) of the Mexican Institute of Industrial Property, in the procedures indicated.
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i septíémb ^ é'de'lkl2> · sr ·. . · ¿
I. “Los 1 ifec ^ ióp V, S'Lfteeción JIL ^ .SSdeia Ley dete P« ó¡ »sdad Industrial. .Yi ^ santefaOte has ur ^ ryfgei i fasáípago dáalSn & paraNnar haj4'pon * n <tementoep fódisíuesto by Ysnartícutes 6? Ía¿cjt> nee til y 7 * i (0ΌΡ.) 27/08/1991 »reformante pl OÍ / Oá / 1994, »10/5/1986, 2632 / ^ 07,
<img file="MX353340B_D0004.tif" />
DIVISIONAL DIRECTOR OF PATENTS NAHANNY CANAL REYES
<img file="MX353340B_D0005.tif" />
Original string:
NAHANNY MARISOL CANAL REYES | 00001000000403252793 | Administration Service
Tax | 1695 || MX / 2018/3430 | MX / a / 2017/003647 | Normal patent title with divisional PCT | 1223 | GAGV | Page (s) 1 | 6whjRAt5m8ZqfmO1 VCVcZmC MfYQ =
<img file="MX353340B_D0006.tif" />
Arena: No 550 Piso 1, Pueblo Santa María Tepepan. Xochimilco, 16020 (andad de México.
(55) 53340700 www.gob.mx/impi
ΜΧ / 2018/3430
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IMPROVEMENTS OF CELL CULTURES
<img file="MX353340B_D0008.tif" />
Related Requests
This Application claims the priority benefit of North American Provisional Patent Application No. 60/845158, filed on September 13, 2006, and North American Provisional Patent Application No. 60/876374, filed on December 21, 2006. The content of each of the above priority documents is incorporated herein by reference.
Background of the Invention
Recombinant DNA technology has provided a means of producing proteins in amounts that are allowed to be used in a spectrum of applications, including therapeutic, diagnostic, agricultural, and research purposes.
A goal of recombinant protein production is the optimization of cell culture conditions and media, in order to obtain a larger quantity of proteins and the most efficient means of productivity. Any improvement, including increasing improvement, can have enormous economic benefits. In the pharmaceutical industry, optimizing protein production for biologics used in therapies for disease treatment is advantageous, as is any improvement that can have a significant impact when the biologic is large-scale manufacturing. <sub>; <í</sub> Thus, there is a need to maximize the production of cell culture proteins that
<img file="MX353340B_D0009.tif" />
tw express biological proteins for use in medicine.
Typically, mammalian cell culture media are based on commercially available formulation media, including, for example, DMEM or Ham's F12. Often, the formulation media is not sufficiently enriched to support the increase in both cell growth and expression of biological proteins. There is a need to improve cell culture media, supplements, and cell culture methods to improve protein production. Brief Description of the Invention
The invention provides methods and compositions for improving protein expression in cell cultures, particularly mammalian cell cultures. The invention relates to improved cell culture media, including cell growth media for protein expression and cell culture production media optimized for protein expression.
The invention also includes methods and formulation media optimized for high protein expression in mammalian cell cultures. In particular, cell culture media are optimized for the expression of antibodies in mammalian cell cultures, for example CHO cells. Improved batch feeding methods and compositions are also provided to promote protein production by adding supplemental solutions, for example solutions containing hydrolyzate and basic media solutions.
<img file="MX353340B_D0010.tif" />
<img file="MX353340B_D0011.tif" />
ot the rxcwsPAD tNOUlTtl Al
The invention provides improved salt-free basal growth media for use in mammalian cell cultures. The invention includes a serum-free cell culture medium comprising Part, Part B and Part C, where Part A consists essentially of a modified basal medium that excludes the following components: sodium bicarbonate, a buffer, phosphate of monobasic sodium, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; Part B consists essentially of a source of inorganic iron; and Part C comprises a recombinant growth factor; a regulatory solution; an osmolarity regulator; a source of energy; and at least two different hydrolyzates that are not of animal origin.
In one embodiment, Part A further comprises non-ferrous metal ions, vitamins, or a combination of both. In one embodiment, the source of Part B inorganic iron is ferric citrate, for example approximately 100 to 150 mg / L or a solution of 0.1 to 1 mM final concentration of ferric citrate. In another embodiment, the source of inorganic iron from Part B is ferric citrate, for example, approximately 122.5 mg / L or 0.5 mM of final concentration of ferric citrate.
In one embodiment, the Part C recombinant growth factor is selected from the group consisting of insulin or a recombinant analog, IGF-1, and a combination of insulin and IGF-1,
<img file="MX353340B_D0012.tif" />
for example, about 4 mg / L a
IMPI Mexican fNJTrruTo <sup>01</sup> U MUMÍOAD IHDUSTRML
<img file="MX353340B_D0013.tif" />
recombinant analog thereof.
In one embodiment, the regulatory solution that is excluded from the modified basal medium is HEPES regulatory solution.
In one embodiment, the Part C buffer solution comprises a buffer solution for phosphates, HEPES, and sodium bicarbonate, for example, about 0.1 to 3 g / L of sodium bicarbonate, about 0.1 to 3 g / L of HEPES. In one embodiment, the Part C buffer solution comprises 1.6 g / L of sodium bicarbonate and / or approximately 1.8 g / L of HEPES. In one embodiment, the phosphate buffer solution comprises approximately 0.01 to 0.5 g / L of monobasic and dibasic sodium phosphates.
In a further embodiment, Part C further comprises asparagine, glutamine, or glutamine and asparagine.
In one embodiment, the Part C osmolarity regulator is NaCI, eg, about 1.0 to 6.5 g / L NaCI.
In one embodiment, the energy source for Part C is a monosaccharide, for example glucose (such as D-glucose), maltose, trickle, galactose, and fructose. In one embodiment, the cell culture medium of the invention comprises no more than about 7.0 g / L glucose.
In another embodiment, the cell culture medium of the invention comprises at least two different hydrolyzates that are not of Part C animal origin, which are a hydrolyzate
<img file="MX353340B_D0014.tif" />
<img file="MX353340B_D0015.tif" />
plant-based and a hydrolyzate that is not
<img file="MX353340B_D0016.tif" />
of animal origin or based on plants. An example of a plant based hydrolyzate that can be used in the invention is a soy based hydrolyzate. An example of a hydrolyzate that is neither animal based nor plant based is a yeast based hydrolyzate.
In one embodiment, the cell culture medium of the invention further comprises methotrexate. In one embodiment, the cell culture medium further comprises approximately 100 nM to 5000 nM of methotrexate.
In yet another embodiment, the cell culture medium further comprises a cell protector or surfactant. An example of a surfactant that can be used in the cell culture medium of the invention is Pluronic methyl cellulose or polyol, for example Pluronic F-68. In one embodiment, the cell culture medium comprises approximately 0.1-5 g / L Pluronic F-68. In one embodiment, the cell culture medium comprises approximately 1.0 g / L Pluronic F-68.
In yet another embodiment of the invention, the cell culture medium further comprises L-glutamine.
In one embodiment, the cell culture medium has a pH in the range of 7.1 to 7.3.
In another embodiment, the cell culture medium of the invention has an osmolarity in the range of about 320 to 450 mOsm / kg.
The invention includes a cell culture medium free of
<img file="MX353340B_D0017.tif" />
IMPI serum comprising: a basal medium; approximately 8-12 mL / kg or 116-126 mg / L of ferric citrate; approximately 2-6 mg / kg of recombinant human insulin; approximately 2-5 g / kg of anhydrous glucose; about 0.1-0.5 g / kg L-glutamine; about 1-3 g / kg of sodium bicarbonate; approximately 0.01-0.05 g / kg NaH<sub>2</sub>PO<sub>4</sub>'H<sub>2</sub>OR; approximately 0.4 to 0.5 g / kg of Na<sub>2</sub>HPO<sub>4</sub>»7H<sub>2</sub>OR; and approximately 1.0-3.0 g / kg of yeast-based hydrolyzate. In one embodiment, the cell culture medium comprises a basal medium; approximately 10.0 mL / kg or 122 mg / L of ferric citrate; approximately 4.0 mg / kg of recombinant human insulin; approximately 3.5 g / kg of anhydrous glucose; about 0.29 g / kg L-glutamine; about 1.6 g / kg of sodium bicarbonate; about 0.03 g / kg NaH<sub>2</sub>PO<sub>4</sub>* H<sub>2</sub>OR; approximately 0.43 to 0.44 g / kg Na<sub>2</sub>HPO<sub>4</sub>"7H<sub>2</sub>OR; and approximately 2.0 g / kg of yeast-based hydrolyzate. In one embodiment, the cell culture medium essentially consists of a basal medium; approximately 10.0 mL / kg or 122 mg / L of ferric citrate; approximately 4.0 mg / kg of recombinant human insulin; approximately 3.5 g / kg of anhydrous glucose; about 0.29 g / kg L-glutamine; about 1.6 g / kg of sodium bicarbonate; about 0.03 g / kg NaH<sub>2</sub>PO<sub>4</sub>»H<sub>2</sub>OR; approximately 0.43 to 0.44 g / kg NaH<sub>2</sub>PO<sub>4</sub>»7H<sub>2</sub>OR; and approximately 2.0 g / kg of yeast-based hydrolyzate.
The invention further provides a serum-free cell culture medium, consisting essentially of a basal medium;
<img file="MX353340B_D0018.tif" />
about 2-6 mg / kg of human insulin; about 2-5 g / kg anhydrous glucose; about 0.1-0.5 g / kg L-glutamine; about 1-3 g / kg of sodium bicarbonate; approximately 0.01-0.05 g / kg NaH<sub>2</sub>PO<sub>4</sub>»H<sub>2</sub>OR; approximately 0.4 to 0.5 g / kg Na<sub>2</sub>HPO<sub>4</sub>"7H<sub>2</sub>OR; and approximately 1.0-3.0 g / kg of yeast-based hydrolyzate. In one embodiment, cell culture essentially consists of a basal medium; approximately 8-12 mL / kg or 116-126 mg / L of ferric citrate; approximately 2-6 mg / kg of recombinant human insulin; about 2-5 g / kg anhydrous glucose; about 0.1-0.5 g / kg L-glutamine; about 1-3 g / kg of sodium bicarbonate; approximately 0.01-0.05 g / kg NaH<sub>2</sub>PO<sub>4</sub>* H2O; approximately 0.4 to 0.5 g / kg Na<sub>2</sub>HPO<sub>4</sub>"7H<sub>2</sub>OR; and approximately 1.0-3.0 g / kg of yeast-based hydrolyzate.
In one embodiment, the cell culture medium further comprises approximately 2.50 mL / kg of methotrexate.
The invention also includes a method of producing a protein, comprising culturing mammalian cells comprising a nucleic acid encoding the protein in the culture medium of the invention; and transferring the culture to the cell culture production medium, so that the protein is produced.
In one embodiment, the protein is an antibody, including, for example, D2E7 (adalimumab).
IMPI
<img file="MX353340B_D0019.tif" />
The invention further provides a serum-free cell culture production medium, comprising: a modified basal medium that excludes the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; approximately 8 to 12 mL / kg or 122.45 mg / L of ferric citrate; approximately 4 to 8 mL / kg or 10 to 14 mg / kg of recombinant human insulin; about 5 to 9 g / kg of anhydrous glucose; approximately 0.5 to 0.7 g / kg of Lglutamine; about 1 to 2 g / kg of sodium bicarbonate; about 1 to 2 g / kg HEPES; about 2 to 3 g / kg NaCI; about 0.5 to 2 g / kg Pluronic F-68; approximately 0.01 to 0.1 g / kg NaH<sub>2</sub>PO<sub>4</sub>'H<sub>2</sub>OR; approximately 0.4 to 0.5 g / kg Na<sub>2</sub>HPO<sub>4</sub>* 7H<sub>2</sub>OR; approximately 8 to 12 g / kg of yeast-based hydrolyzate; and approximately 60 to 70 g / kg of plant-based hydrolyzate. In one embodiment, the cell culture production medium consists essentially of a modified basal medium that excludes the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; approximately 8 to 12 mL / kg or 122.45 mg / L of ferric citrate; approximately 4 to 8 mL / kg or 10 to 14 mg / kg of recombinant human insulin; about 5 to 9 g / kg of anhydrous glucose; approximately 0.5 to 0.7 g / kg L-glutamine;
IMPI
<img file="MX353340B_D0020.tif" />
about 2 g / kg of baking soda;
about 1 to 2 g / kg HEPES; about 2 to 3 g / kg NaCI; about 0.5 to 2 g / kg Pluronic F-68; approximately 0.01 to 0.1 g / kg NaH<sub>2</sub>PO<sub>4</sub>»H<sub>2</sub>OR; approximately 0.4 to 0.5 g / kg Na<sub>2</sub>HPO<sub>4</sub>»7H<sub>2</sub>OR; approximately 8 to 12 g / kg of yeast-based hydrolyzate;
and approximately 60 to 70 g / kg of plant-based hydrolyzate.
In another embodiment, the cell culture production medium comprises a basal medium, approximately 10.0 mL / kg or 122.45 mg / L of ferric citrate; approximately 6.0 mL / kg or 12 mg / kg of recombinant human insulin; approximately 7.0 g / kg of anhydrous glucose; approximately 0.58 to 0.59 g / kg L-glutamine;
about 1.6 g / kg of sodium bicarbonate; about 1.8 g / kg HEPES; about 2.4 to 2.5 g / kg NaCI; about 1.0 g / kg Pluronic F-68; approximately 0.03 to 0.04 g / kg NaH<sub>2</sub>PO<sub>4</sub>* H<sub>2</sub>OR; approximately 0.43 to 0.44 g / kg Na<sub>2</sub>HPO<sub>4</sub>* 7H<sub>2</sub>OR; approximately 10.7 g / kg of yeast-based hydrolyzate; and approximately 6.9 to 7.0 g / kg of plant-based hydrolyzate.
The invention also provides a serum-free cell culture medium comprising a modified basal medium, which excludes the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; approximately 8 to 12 mL / kg or 122.45 mg / L of ferric citrate;
IMPI
<img file="MX353340B_D0021.tif" />
approximately 3 to 5 mL / kg or 6 to 8 mg / kg human growth rate; about 5 to 9 g / kg of anhydrous glucose; about 0.1 to 2 g / kg L-glutamine; about 1 to 2 g / kg of sodium bicarbonate; about 1 to 2 g / kg of
HEPES; about 2 to 3 g / kg of NaCI; about 0.1 to 2 g / kg Pluronic F-68; about 0.01 to 0.1 g / kg NaH2PO4 * H2O; about 0.4 to 0.5 g / kg NaH2PO4 »7H2O; about 0.4 to 0.5 g / kg L-asparagine monohydrate; approximately 2 to 6 g / kg of yeast-based hydrolyzate; and about 2 to 4 g / kg of plant-based hydrolyzate. In one embodiment, the cell culture medium consists essentially of a modified basal medium, which excludes the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; approximately 8 to 12 mL / kg or 122.45 mg / L of ferric citrate; approximately 3 to 5 mL / kg or 6 to 8 mg / kg of recombinant human insulin; about 5 to 9 g / kg of anhydrous glucose; about 0.1 to 2 g / kg L-glutamine; about 1 to 2 g / kg of sodium bicarbonate; about 1 to 2 g / kg of HEPES;
about 2 to 3 g / kg of NaCI; about 0.1 to 2 g / kg Pluronic F-68; approximately 0.01 to 0.1 g / kg NaH<sub>2</sub>PO<sub>4</sub>* H<sub>2</sub>OR; about 0.4 to 0.5 g / kg Ν3<sub>2</sub>ΗΡΟ<sub>4</sub>7Η<sub>2</sub>Ο; about 0.4 to 0.5 g / kg L-asparagine monohydrate; approximately 2 to 25 6 g / kg of yeast-based hydrolyzate; and approximately 2 to 4 g / kg of plant-based hydrolyzate.
cell culture comprises a
MEXICAN INSTITUTE Λ
OF THE INDUSTRIAL POWERS OFeurSflllif
In one embodiment, the modified basal medium medium;
approximately 10.0 mL / kg or 122.45 mg / kg of ferric citrate; approximately 3.8 to 3.9 mL / kg or 7.8 mg / kg of recombinant human insulin; approximately 7.0 g / kg of anhydrous glucose; about 0.8 to 0.9 g / kg L-glutamine; approximately
1.6 g / kg of sodium bicarbonate; about 1.8 g / kg HEPES; about 2.6 to 2.7 g / kg NaCI; about 1.0 g / kg Pluronic F-68; approximately 0.03 to 0.04 g / kg NaH<sub>2</sub>PO<sub>4</sub>* H<sub>2</sub>OR; approximately 0.43 to 0.44 g / kg Na<sub>2</sub>HPO4 «7H<sub>2</sub>OR; about 0.45 g / kg L-asparagine monohydrate; approximately 4.0 g / kg of yeast-based hydrolyzate; and approximately 2.6 g / kg of plant-based hydrolyzate.
The invention also includes a serum-free cell culture medium comprising a modified basal medium, which excludes the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; approximately 8 to 10 mL / kg or 120 to 130 mg / L of ferric citrate; approximately 3 to 5 mL / kg or 7.8 mg / kg of recombinant human insulin; about 5 to 9 g / kg of anhydrous glucose; about 0.8 to 0.9 g / kg L-glutamine; approximately 0.3 to 0.5 g / kg of L-asparagine monohydrate; about 1 to 2 g / kg of sodium bicarbonate; about 1 to 2 g / kg of HEPES; about 2 to 3 g / kg
IMPI
<img file="MX353340B_D0022.tif" />
NaCI; approximately 0.5 to 2 g / kg of Pluronic F-68; approximately 0.01 to 0.1 g / kg NaH<sub>2</sub>PO<sub>4</sub>«H<sub>2</sub>OR; approximately
0.1 to 1.0 g / kg Na<sub>2</sub>HPO<sub>4</sub>* 7H<sub>2</sub>OR; approximately 2 to 6 g / kg of yeast-based hydrolyzate; and approximately 2 to 4 g / kg of plant-based hydrolyzate. In one embodiment, the cell culture medium consists essentially of a modified basal medium, which excludes the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; approximately 8 to 10 mL / kg or 120 to 130 mg / L of ferric citrate; approximately 3 to 5 mL / kg or 7.8 mg / kg of recombinant human insulin; about 5 to 9 g / kg of anhydrous glucose; about 0.8 to 0.9 g / kg L-glutamine; approximately 0.3 to 0.5 g / kg of L-asparagine monohydrate; about 1 to 2 g / kg of sodium bicarbonate; about 1 to 2 g / kg of HEPES; about 2 to 3 g / kg of NaCI; approximately 0.5 to 2 g / kg of Pluronic F-68;
approximately 0.01 to 0.1 g / kg NaH<sub>2</sub>PO4-H<sub>2</sub>OR; about 0.1 to 1.0 g / kg Na<sub>2</sub>HPO<sub>4</sub>* 7H<sub>2</sub>OR; approximately 2 to 6 g / kg of yeast-based hydrolyzate; and approximately 2 to 4 g / kg of plant-based hydrolyzate. In another modality, the medium
<td colspan="2">cell culture</td><td colspan="2">understands</td><td>a</td><td>means, medium</td><td colspan="2">baseline modified;</td>
<td>approximately</td><td> 10</td><td>mL / kg</td><td>or</td><td> 122</td><td>mg / L</td><td>citrate</td><td>ferric;</td>
<td>approximately</td><td> 3.8</td><td>to 3.9</td><td colspan="2">mL / kg</td><td>or 7.8</td><td>mg / kg of</td><td>insulin</td>
recombinant human; approximately 7.0 g / kg of anhydrous glucose;
<img file="MX353340B_D0023.tif" />
«R fT
<img file="MX353340B_D0024.tif" />
about 0.87 to 0.88 g / kg L-glutamine; approximately __n .J<sup>1ΓΙ</sup>*-<sup>ί</sup> *** <sup>T fl</sup>—*****
0.45 g / kg L-asparagine monohydrate; approximately 1.6 g / kg of sodium bicarbonate, approximately 1.8 g / kg of HEPES;
about 2.67 to 2.68 g / kg NaCI; about 1.0 g / kg Pluronic F-68; approximately 0.03 to 0.04 g / kg NaH<sub>2</sub>PO<sub>4</sub>»H<sub>2</sub>OR; approximately 0.43 to 0.44 g / kg Na<sub>2</sub>HPO<sub>4</sub>"7H<sub>2</sub>OR; approximately 4.0 g / kg yeast-based hydrolyzate; and approximately 2.6 g / kg of plant-based hydrolyzate.
The invention includes a serum free cell culture medium comprising a basal cell growth medium; approximately 8 to 12 mL / kg or 120 to 130 mg / L of ferric citrate; approximately 2 to 6 mg / kg of recombinant human insulin; approximately 150 to 250 g / kg of anhydrous glucose; approximately 0.1 to 0.5 g / kg of L-glutamine; about 1 to 2 g / kg of sodium bicarbonate; and approximately 5 to 15 g / kg of yeast-based hydrolyzate. In one embodiment, the cell culture medium consists essentially of a basal cell growth medium; approximately 8 to 12 mL / kg or 120 to 130 mg / L of ferric citrate; about 2 to 6 mg / kg of recombinant human insulin; approximately 150 to 250 g / kg of anhydrous glucose; approximately 0.1 to 0.5 g / kg of L-glutamine; about 1 to 2 g / kg of sodium bicarbonate; and approximately 5 to 15 g / kg of yeast-based hydrolyzate. In a further embodiment, the cell culture medium comprises a basal cell growth medium; about 10 mL / kg or
<img file="MX353340B_D0025.tif" />
*
<img file="MX353340B_D0026.tif" />
<img file="MX353340B_D0027.tif" />
IMPI
MLAMKWDAD MEXICAN INSTITUTE. ,,,,. industrial
122.45 mg / L ferric citrate; approximately 4 mg / kg of recombinant human insulin; approximately 2ÜU g / kg of anhydrous glucose; about 0.29 to 0.30 g / kg L-glutamine; about 1.6 g / kg of sodium bicarbonate; and approximately 11 g / kg of yeast-based hydrolyzate. In a further embodiment, the protein is an antibody, including, for example, a fully human anti-IL-12 antibody, for example, ABT-874.
The invention also includes a serum free cell culture medium, comprising a basal cell growth medium;
approximately 8 to 12 mL / kg or 120 to 130 mg / L of ferric citrate; about 2 to 6 mg / kg of recombinant human insulin; about 1 to 3 g / kg of anhydrous glucose; about 0.1 to 1 g / kg L-glutamine; about 1 to 2 g / kg of sodium bicarbonate; and about 1 to 4 g / kg of yeast-based hydrolyzate. In one embodiment, the cell culture medium consists essentially of a basal cell growth medium; approximately 8 to 12 mL / kg or 120 to 130 mg / L of ferric citrate; approximately 2 to 6 mg / kg of recombinant human insulin; about 1 to 3 g / kg of anhydrous glucose; about 0.1 to 1 g / kg L-glutamine; about 1 to 2 g / kg of sodium bicarbonate; and about 1 to 4 g / kg of yeast-based hydrolyzate. In another embodiment, the cell culture medium comprises a basal cell growth medium; approximately mL / kg or 122.45 mg / L of ferric citrate; about 4 mg / kg
<img file="MX353340B_D0028.tif" />
recombinant human insulin; approximately 1.5 g / kg of anhydrous glucose; about 0.29 to 0.30 g / kg L-glutamine;
about 1.6 g / kg of sodium bicarbonate; and approximately 2 g / kg of yeast-based hydrolyzate. In one embodiment, the pH of the cell culture medium is approximately 7.10 to 7.30 and the osmolarity is in the range of approximately 300 to 340 mOsm / kg. In yet another embodiment, the cell culture medium comprises at least 8 g / kg of yeast-based hydrolyzate. In one embodiment, the protein that is produced in a mammalian cell, eg, CHO cell, using the cell culture medium, is an antibody, including for example, an anti-IL-12 antibody or an anti-IL receptor antibody. EPO-R, for example ABT-874.
The invention further provides a cell culture medium comprising a modified basal medium that excludes the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide ; approximately 8 to 12 mL / kg or 120 to 130 mg / L of ferric citrate; approximately 2.5 to 4.5 mL / kg or 7.8 mg / kg of recombinant human insulin; about 5 to 9 g / kg of anhydrous glucose; about 0.5 to 1 g / kg of L-glutamine; about 0.1 to 1 g / kg L-asparagine monohydrate; about 1 to 2 g / kg of sodium bicarbonate; about 1 to 2 g / kg of HEPES; about 1 to 4 g / kg NaCI; about 0.1 to 2 g / kg
<img file="MX353340B_D0029.tif" />
Pluronic F-68;
approximately 0.01 to 0.1 g / kg NaH<sub>2</sub>PO<sub>4</sub>'H<sub>2</sub>OR; approximately
0.1 to 1 g / kg of Na<sub>2</sub>HPO<sub>4</sub>* 7H<sub>2</sub>OR; approximately 2 to 6 g / kg of yeast-based hydrolyzate; and approximately 2 to 6 g / kg of plant-based hydrolyzate. In one embodiment, the cell culture medium of the invention consists essentially of a modified basal medium that excludes the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant , and glucose monosaccharide; approximately 8 to 12 mL / kg or 120 to 130 mg / L of ferric citrate; approximately 2.5 to 4.5 mL / kg or 7.8 mg / kg of recombinant human insulin; about 5 to 9 g / kg of anhydrous glucose; about 0.5 to 1 g / kg of L-glutamine; approximately 0.1 to 1 g / kg of Lasparagine monohydrate; about 1 to 2 g / kg of sodium bicarbonate; about 1 to 2 g / kg of HEPES; about 1 to 4 g / kg NaCI; about 0.1 to 2 g / kg Pluronic F-68; approximately 0.01 to 0.1 g / kg NaH<sub>2</sub>PO<sub>4</sub>»H<sub>2</sub>OR; about 0.1 to 1 g / kg Na<sub>2</sub>HPO<sub>4</sub>* 7H<sub>2</sub>OR; approximately 2 to 6 g / kg of yeast-based hydrolyzate; and approximately 2 to 6 g / kg of plant-based hydrolyzate. In another embodiment, the cell culture medium comprises a modified basal medium; approximately 10 mL / kg or 122.45 mg / L of ferric citrate; approximately 3.8 to 3.9 mL / kg or 7.8 mg / kg of recombinant human insulin; approximately 7.0 g / kg of anhydrous glucose;
<1
IMPIOS, MEXICAN INSTITUTE OF tA MONEDAD
INDUSTRIAL 'OwJÜL.—' approximately 0.87 to 0.88 g / kg L-glutamine; apwwinodamerite · 0.45 g / kg L-asparagine monohydrate; about 1.6 g / kg of sodium bicarbonate; about 1.8 g / kg HEPES; about 2.67 g / kg NaCI; about 1.0 g / kg Pluronic F-68; approximately 0.03 to 0.04 g / kg NaH<sub>2</sub>PO<sub>4</sub>»H<sub>2</sub>OR; approximately 0.43 to 0.44 g / kg Na<sub>2</sub>HPO<sub>4</sub>"7H<sub>2</sub>OR; approximately 4.0 g / kg of yeast-based hydrolyzate; and approximately 2.6 g / kg of plant-based hydrolyzate.
The invention also includes a cell culture production medium comprising a modified basal medium, which is modified to remove the following components: sodium bicarbonate, HEPES buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator , a surfactant, and glucose monosaccharide; approximately 8 to 12 mL / kg or 120 to 130 mg / L of ferric citrate; approximately 4 to 8 mL / kg or 10 to 14 mg / kg of recombinant human insulin; about 5 to 9 g / kg of anhydrous glucose; about 0.1 to 1 g / kg Lglutamine; about 1 to 2 g / kg of sodium bicarbonate; about 1 to 2 g / kg of HEPES; about 1 to 3 g / kg NaCI; approximately 0.5 to 2 g / kg of Pluronic F-68; approximately 0.01 to 0.1 g / kg NaH<sub>2</sub>PO<sub>4</sub>* H<sub>2</sub>OR; about 0.1 to 1 g / kg Na<sub>2</sub>HPO<sub>4</sub>* 7H2O; approximately 8 to 12 g / kg of yeast-based hydrolyzate; and approximately 6 to 8 g / kg of plant-based hydrolyzate. In one embodiment, the cell culture production medium of the invention consists essentially
<img file="MX353340B_D0030.tif" />
IMPI ^
MEXICAN INSTITUTE 'fe *
DE LA FRORIF0AI,, ·,, ...., INDUSTRIA! _____ of a modified basal medium, which is modified to remove the
<td>following components:</td><td>baking soda, buffer solution</td>
HEPES, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; approximately 8 to 12 mL / kg or 120 to 130 mg / L of ferric citrate; approximately 4 to 8 mL / kg or 10 to 14 mg / kg of recombinant human insulin; about 5 to 9 g / kg of anhydrous glucose; about 0.1 to 1 g / kg L-glutamine; about 1 to 2 g / kg of sodium bicarbonate; about 1 to 2 g / kg of HEPES; about 1 to 3 g / kg NaCI; approximately 0.5 to 2 g / kg of Pluronic F-68;
about 0.01 to 0.1 g / kg Ν3Η<sub>2</sub>ΡΟ<sub>4</sub>· Η<sub>2</sub>Ο; approximately
0.1 to 1 g / kg of Na<sub>2</sub>HPO<sub>4</sub>* 7H<sub>2</sub>OR; approximately 8 to 12 g / kg of yeast-based hydrolyzate; and approximately 6 to 8 g / kg of plant-based hydrolyzate. In another embodiment, the cell culture production medium comprises a modified basal medium; approximately 10 mL / kg or 122.45 mg / L of ferric citrate; approximately 6.0 mL / kg or 12 mg / kg of recombinant human insulin; approximately 7.0 g / kg of anhydrous glucose; about 0.58 to 0.59 g / kg L-glutamine; approximately 1.6 g / kg of sodium bicarbonate, approximately 1.8 g / kg of HEPES; about 2.45 g / kg NaCI; about 1.0 g / kg Pluronic F-68; approximately 0.03 to 0.04 g / kg NaH<sub>2</sub>PO<sub>4</sub>»H<sub>2</sub>OR; approximately 0.43 to 0.44 g / kg Na<sub>2</sub>HPO<sub>4</sub>* 7H<sub>2</sub>OR; approximately 10.7 g / kg of yeast-based hydrolyzate; and
IMPI
<img file="MX353340B_D0031.tif" />
approximately 6.9 to 7.0 g / kg of plant-based hydrolyzate.
Another aspect of the invention is a cell culture production medium comprising a modified basal medium that excludes the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant , and glucose monosaccharide; approximately 8 to 12 mL / kg or 110 to 130 mg / L of ferric citrate; approximately 4 to 8 mL / kg or 11 to 15 mg / kg of recombinant human insulin; about 5 to 9 g / kg of anhydrous glucose; about 0.1 to 1 g / kg L-glutamine; about 1 to 2 g / kg of sodium bicarbonate, about 1 to 2 g / kg of HEPES; about 1 to 3 g / kg NaCI; about 0.1 to 2 g / kg Pluronic F-68; approximately 0.01 to 0.1 g / kg NaH<sub>2</sub>PO<sub>4</sub>* H<sub>2</sub>OR; about 0.1 to 1 g / kg Na<sub>2</sub>HPO<sub>4</sub>"7H<sub>2</sub>OR; approximately 12 to 16 g / kg of yeast-based hydrolyzate; and approximately 8 to 10 g / kg of plant-based hydrolyzate. In one embodiment, the cell culture production medium consists essentially of a modified basal medium that excludes the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; approximately 8 to 12 mL / kg or 110 to 130 mg / L of ferric citrate; approximately 4 to 8 mL / kg or 11 to 15 mg / kg of recombinant human insulin; about 5 to 9 g / kg of anhydrous glucose; approximately
ΙΜΡΪ
<img file="MX353340B_D0032.tif" />
0.1 to 1 g / kg of L-glutamine; about 1 to 2 g / kg of sodium bicarbonate, about 1 to 2 g / kg of HEPES;
about 1 to 3 g / kg NaCI; about 0.1 to 2 g / kg Pluronic F-68; approximately 0.01 to 0.1 g / kg NaH<sub>2</sub>PO<sub>4</sub>* H<sub>2</sub>OR; about 0.1 to 1 g / kg Na<sub>2</sub>HPO<sub>4</sub>»7H<sub>2</sub>OR; approximately 16 g / kg yeast-based hydrolyzate; and approximately 10 g / kg of plant-based hydrolyzate. In another embodiment, the cell culture production medium of the invention comprises a modified basal medium; approximately 10 ml_ / kg or 122.45 mg / L of ferric citrate; approximately 6.5 mL / kg or 13 mg / kg of recombinant human insulin; approximately 7.0 g / kg of anhydrous glucose;
approximately 0.58 to 0.59 g / kg of L-glutamine: approximately 1.6 g / kg of sodium bicarbonate; about 1.8 g / kg HEPES; about 2.45 g / kg NaCI; about 1.0 g / kg Pluronic F-68; approximately 0.03 to 0.04 g / kg NaH<sub>2</sub>PO4 »H<sub>2</sub>OR; approximately 0.43 to 0.44 g / kg Na<sub>2</sub>HPO<sub>4</sub>* 7H<sub>2</sub>OR; approximately 14.2 to 14.3 g / kg of yeast-based hydrolyzate; and approximately 9.2 to 9.3 g / kg of plant-based hydrolyzate.
In one embodiment, the cell culture medium has a pH of approximately 6 to 8. In another embodiment, the cell culture medium has a pH of approximately 7.10 to 7.20.
In one embodiment, the cell culture medium has an osmolarity of about 350 to 450 mOsm / kg. In another embodiment, the cell culture medium has an osmolarity from the Mexican Institute DE LA FROnfUAP LVwwa & VlA'lT INDUSTRIAL approximately 373 to 403 mOsm / kg.
-------.-. . - -. II I r i. ..inm — ll-irr
The cell culture media of the invention may further comprise methotrexate. In one embodiment, the cell culture medium further comprises methotrexate, eg, about 1-10 mL / kg. In another embodiment, the cell culture medium further comprises methotrexate, eg, about 2.50 mL / kg.
In one embodiment, the protein that is expressed in the cell culture is an antibody, or an antigen-binding fragment thereof. In one embodiment, the antibody, or antigen-binding fragment thereof, is an anti-TNFa antibody or an anti-EPO-R antibody. In another embodiment, the anti-TNFa antibody, or an antigen-binding fragment thereof, is a fully human anti-TNFa antibody, including, for example, the fully human antiTNFa antibody, D2E7 (adalimumab). In yet another embodiment, the antibody or antigen-binding fragment thereof, is an anti-IL-12 antibody or an anti-IL-18 antibody, including a fully anti-IL-12 antibody or an anti-IL-18 antibody. human.
The invention also includes a method of producing a protein, eg, an antibody or antigen-binding portion thereof, which comprises culturing a mammalian cell comprising a nucleic acid encoding the protein, eg, an antibody, in a cell culture medium provided herein. In one embodiment, the cell culture medium is a medium
IMPI
<img file="MX353340B_D0033.tif" />
of cell culture production.
Examples of antibodies or antigen-binding fragments thereof, which can be produced using the methods and compositions of the invention, include an anti-IL-12 antibody antibody, and an anti-TNFa antibody, an antibody against the EPO receptor. (EPO-R).
In one embodiment, the invention further comprises isolating the protein from cell culture media, eg, cell culture production media, described herein.
In one embodiment, the cell culture media and methods of the invention are for culturing mammalian cells, including Chinese Hamster Ovary (CHO) cells.
The invention also includes a Chinese Hamster Ovary (CHO) cell in any of the cell culture media described herein.
The invention also provides an improved batch feeding method and related cell culture media for producing proteins in a culture of mammalian cells, eg, CHO cells. One aspect of the invention is a batch feeding method of producing a protein comprising culturing mammalian cells comprising a nucleic acid encoding the protein in a cell culture, comprising a cell culture production medium; and feeding the mammalian cells by adding a hydrolyzate enrichment solution and a basal enrichment solution to the cell culture during a
<img file="MX353340B_D0034.tif" />
IMPI
MEXICAN INSTITUTE
OF THE PROPERTY
INDUSTRIAL period of time, where the enrichment solution of
Mijuijí> <sup>1</sup> * hydrolyzate comprises at least two different hydrolyzates that are not of animal origin, so that the protein is produced.
In one embodiment, the basal enrichment solution comprises a concentrated basal medium. In another embodiment, the basal enrichment solution comprises a basal medium, asparagine, and glucose. In yet another embodiment, the basal medium is PF CHO.
In one embodiment, the hydrolyzate enrichment solution comprises a first hydrolyzate that is not derived from a plant or an animal, and a second plant-based hydrolyzate. In one embodiment, the hydrolyzate that is not derived from a plant or animal and a plant based hydrolyzate is a yeast based hydrolyzate. In one embodiment, the plant-based hydrolyzate is a soy-based hydrolyzate.
In one embodiment, the protein that is produced is an antibody or an antigen-binding portion thereof. Examples of antibodies or antigen-binding portions thereof, which can be used in the batch feeding methods of the invention, include an anti-TNFa antibody, an anti-IL-12 antibody, an anti-IL-18 antibody, and an antibody against the EPO receptor (EPO-R).
The invention includes a batch feeding method for producing an anti-TNFa antibody, including for example, a fully human anti-TNFa antibody, such as adalimumab,
<img file="MX353340B_D0035.tif" />
comprising cultivating Chinese Hamster Ovary (CHO) cells, comprising a nucleic acid encoding the antiTNFa antibody in a cell culture comprising a cell culture production medium; and feeding the CHO cells by adding a hydrolyzate enrichment solution and a basal enrichment solution to the cell culture over a period of time, wherein the basal enrichment solution comprises a basal medium, asparagine and glucose, and where the enrichment solution Hydrolyzate comprises at least two different hydrolyzates that are not of animal origin, so that the anti-TNFa antibody is produced.
The invention also features a batch feeding method for producing an anti-TNFa antibody comprising culturing CHO cells comprising a nucleic acid encoding the anti-TNFa antibody in a cell culture, comprising a cell culture production medium comprising at least 1-5 g / L, for example 2.0 g / L glucose, where the glucose concentration is controlled by adding glucose to the cell culture production medium as required, to maintain a concentration of at least 1-5 g / L, for example 2.0 g / L glucose; and feeding the CHO cells by adding a hydrolyzate enrichment solution and a basal enrichment solution to the cell culture over a period of time, wherein the basal enrichment solution comprises a basal medium, asparagine and glucose, and where the enrichment solution hydrolyzate comprises at least two different hydrolyzates that do not
MEXICAN INSTITUTE OF INDUSTRIAL UNITY - they are of animal origin, so that the anti-TNFa antibody is produced.
In one embodiment, the invention further includes recovering the anti-TNFa antibody.
In yet another embodiment, the cell culture is grown at a temperature in the range of about 32 to 38 ° C, for example 35 ° C.
In one embodiment, the cell culture production medium is maintained with an amount of between 20 and 65% dissolved oxygen, for example at about 30% dissolved oxygen.
In one embodiment, the osmolarity of the cell culture production medium is maintained throughout the culture, at no more than 500 mOsm.
In one embodiment, the hydrolyzate enrichment solution comprises a first hydrolyzate that is not derived from a plant or an animal, and a second plant-based hydrolyzate. In yet another embodiment, the hydrolyzate that is not derived from a plant or animal and a plant-based hydrolyzate is a yeast-based hydrolyzate. In yet another embodiment, the plant-based hydrolyzate is a soy-based hydrolyzate. In one embodiment, the hydrolyzate enrichment solution consists essentially of approximately 50-280 g / kg, for example 250 to 280 g / kg, of a soy-based hydrolyzate and approximately 75-300 g / kg, for example 150 to 180 g / kg, of a yeast-based hydrolyzate. In one embodiment, the hydrolyzate enrichment solution comprises about 50-280 g / kg, for example 250 to 280
IMPIAS
MUUCANO INSTITUTE.
ΖΟ Dt LA moríίBAO
INDUSTRIAL ^ L * g / kg, of a soy-based hydrolyzate and approximately 75-300 g / kg, for example 150 to 180 g / kg, of a yeast-based hydrolyzate.
In one embodiment, the basal medium is PF CHO.
In one embodiment, the basal enrichment solution has a pH of approximately 9.0 to 10.5.
In yet another embodiment, the time period of the batch feeding method is between about 9 to 15 days; or approximately 12 days.
In yet another embodiment, the basal enrichment solution is added to the cell culture production medium on at least one of the following days of the time period: day 4, day 6, day 9, and day 11. In one embodiment, the Hydrolyzate enrichment solution is added to the cell culture production medium on day 4, day 7, or day 4 and day 7 of the time period.
In yet another embodiment, batch feeding methods further comprise adjusting the pH of the cell culture production medium in accordance with a linear decrease in pH, wherein the linear decrease in pH comprises starting from a pH of about 6.5-8. , for example 7.1 to 7.2 and ending with a final pH of approximately 6.5-7.0, for example 6.9. In one embodiment, the linear decrease in pH is adjusted over a period of at least about 24 hours. In another embodiment, the linear decrease in pH is adjusted over a period of at least about 48 hours. In yet another embodiment, the
<img file="MX353340B_D0036.tif" />
1JLVA.L.
MEXICAN INSTITUTE .... I heard the linear decrease in pH is adjusted with respect to<sup>IN</sup>U7Fó<sup>l</sup>er¡othjCía approximately 72 hours. . ------——
The invention also includes using the cell culture media described herein, in the batch feeding method, for example, the cell culture production medium comprising a modified basal medium that excludes the following components: sodium bicarbonate, solution regulator, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; approximately 8 to 10 mL / kg or 110 to 130 mg / L of ferric citrate; approximately 4 to 8 mL / kg or 10 to 14 mg / kg of recombinant human insulin; about 5 to 9 g / kg of anhydrous glucose; about 0.1 to 1 g / kg L-glutamine; about 1 to 3 g / kg of sodium bicarbonate; about 1 to 3 g / kg of HEPES; about 2 to 3 g / kg of NaCI; about 0.1 to 2 g / kg Pluronic F-68; approximately 0.01 to 0.1 g / kg NaH<sub>2</sub>PO<sub>4</sub>«H<sub>2</sub>OR; about 0.1 to 0.1 g / kg Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR; approximately 8 to 12 g / kg of yeast-based hydrolyzate; and approximately 6 to 8 g / kg of plant-based hydrolyzate. In one embodiment, the cell culture production medium comprises a modified basal medium; approximately 10.0 mL / kg or 122.45 mg / L of ferric citrate; approximately 6.0 mL / kg or 12 mg / kg of recombinant human insulin; approximately 7.0 g / kg of anhydrous glucose;
about 0.58 to 0.59 g / kg L-glutamine; approximately
IMPI
<img file="MX353340B_D0037.tif" />
1.6 g / kg of sodium bicarbonate; anrnximadamantR 1.8 g / kg
HEPES; about 2.45 g / kg NaCI; about 1.0 g / kg Pluronic F-68; about 0.03 to 0.04 g / kg of
NaH<sub>2</sub>PO<sub>4</sub>»H<sub>2</sub>OR; approximately 0.43 to 0.44 g / kg Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR;
approximately 10.7 g / kg of yeast-based hydrolyzate; and approximately 6.9 to 7.0 g / kg of plant-based hydrolyzate.
The invention also provides a batch feeding method for producing an anti-IL-12 antibody, such as for example, a fully human anti-IL-12 antibody (eg ABT-874), which comprises culturing CHO cells comprising a nucleic acid encoding the antibody in a cell culture comprising a cell culture production medium, feed the CHO cells by adding a hydrolyzate enrichment solution and a basal enrichment solution to the cell culture over a period of time, where the basal enrichment solution comprises a basal medium, asparagine and glucose, and where the enrichment solution of Hydrolyzate comprises at least two different hydrolyzates that are not of animal origin, for the anti-IL-12 antibody to be produced.
In one embodiment, the hydrolyzate enrichment solution further comprises glucose.
In one embodiment, the invention also includes recovering the anti-IL-12 antibody.
In one embodiment, the cell culture is grown at a temperature in the range of about 32 to 38 ° C, eg, 'i-ü-x'-n-f. .
<sup>1</sup> i
<img file="MX353340B_D0038.tif" />
about 33 ° C. LÍX-arÍimn · .. ·· .. ........
In one embodiment of the invention, the cell culture production medium is maintained with an amount of between 20-65% dissolved oxygen, for example, about 40% dissolved oxygen.
In yet another embodiment, the cell culture production medium has a pH of about 6.7 to 7.2.
In a further embodiment of the invention, the hydrolyzate enrichment solution comprises a hydrolyzate that is not derived from a plant or an animal, and a plant-based hydrolyzate. In one embodiment, the hydrolyzate that is not derived from a plant or animal is a yeast based hydrolyzate. In another embodiment, the plant-based hydrolyzate is a soy-based hydrolyzate. In yet another embodiment, the hydrolyzate enrichment solution consists essentially of about 50-225 g / kg, eg, 150 to 180 g / kg of a soy-based hydrolyzate; about 75-300, for example 250 to 280 g / kg of a yeast based hydrolyzate; and about 1-5 g / L, for example 2 to 3 g / L glucose. In yet another embodiment, the hydrolyzate enrichment solution comprises approximately 50-225 g / kg, for example 150 to 180 g / kg of a soy-based hydrolyzate, approximately 75-300, for example 250 to 280 g / kg of a yeast-based hydrolyzate, and about 1-5 g / L, for example 2 to 3 g / L glucose. In one embodiment, the basal enrichment solution comprises a basal medium, asparagine, and
<img file="MX353340B_D0039.tif" />
glucose.
In yet another embodiment, the basal enrichment solution has a pH of about 9-10, for example about 9.7, and an osmolarity of about
1400 at 1500 mOsm. In a further embodiment, the basal medium in the basal enrichment solution is PF CHO.
In one embodiment, the time period of the batch feeding method is between 14-15 days.
In one embodiment, the basal enrichment solution is added to the cell culture production medium every third day, starting on day 5 of the time period.
In one embodiment of the invention, the hydrolyzate enrichment solution is added to the cell culture production medium daily, beginning on day 6 of the time period. In yet another embodiment, the basal enrichment solution and the hydrolyzate enrichment solution are added to the cell culture production medium daily, beginning on day 5 of the time period.
The invention also includes using the cell culture media described herein, in the batch feeding method, for example, the cell culture production medium comprising a modified basal medium, excluding the following components: sodium bicarbonate, solution regulator, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide;
: 3 «I · - * '·<sup>1</sup> approximately 8 to 12 mL / kg or 110 a
130
MEXICAN INSTITUTE &
dua «oreDAC INDUSTRIAL ------ mg / L of ferric citrate;
approximately 5 to 8 mL / kg or 11 mg / kg of recombinant human insulin; approximately 9 g / kg anhydrous glucose; about 0.1 to 1 g / kg of
L-glutamine;
about 1 to 2 g / kg of sodium bicarbonate, about 1 to 2 g / kg of HEPES; about 2 to 3 g / kg NaCI; about 0.1 to 2 g / kg Pluronic F-68; approximately 0.01 to 0.1 g / kg NaH<sub>2</sub>PO<sub>4</sub>-H<sub>2</sub>OR; approximately
0.1 to 1 g / kg of Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR; approximately 6 to 12 g / kg of yeast-based hydrolyzate; and approximately 6 to 8 g / kg of plant-based hydrolyzate. In one embodiment, the cell culture production medium comprises approximately 10 mL / kg or 122.45 mg / L of ferric citrate; approximately 6.5 mL / kg or 13 mg / kg of recombinant human insulin; approximately 7.0 g / kg of anhydrous glucose; about 0.58 to 0.59 g / kg Lglutamine; about 1.6 g / kg of sodium bicarbonate; about 1.8 g / kg HEPES; about 2.45 g / kg NaCI; about 1.0 g / kg Pluronic F-68; approximately 0.03 to 0.04 g / kg NaH<sub>2</sub>PO<sub>4</sub>-H<sub>2</sub>OR; approximately 0.43 to 0.44 g / kg Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR; approximately 10.7 g / kg of yeast-based hydrolyzate; and approximately 6.9 to 7.0 g / kg of plant-based hydrolyzate.
In one embodiment, the invention features methods for culturing cells on a large scale. In one embodiment, large-scale cell culture is greater than about 10 L. In another embodiment,
<img file="MX353340B_D0040.tif" />
<img file="MX353340B_D0041.tif" />
• A · *** IMPI
INSTITUTO MEXiCAN ^ delafromedad IND'.JSTMAL the large-scale cell culture is approximately 13 L.
The invention also provides combination feeding solutions that are advantageous because these solutions provide a combination of nutrients in a single solution. The invention includes a combined feeding solution comprising glucose; a basal medium; a different amino acid from glutamine; and at least two different hydrolyzates that are not of animal origin. The invention also includes a combined feeding solution consisting essentially of glucose; a basal medium; a different amino acid from glutamine; and at least two different hydrolyzates that are not of animal origin.
In one embodiment, the feed solution has a pH of about 6.0 to 8.0.
In one embodiment, the combined feeding solution comprises about 100 to 250 g / kg of glucose. In one embodiment, the combined feeding solution comprises the amino acid asparagine, for example about 1.0 to 15.0 g of asparagine; or about 3.0 to 5.0 g / kg asparagine.
In one embodiment, the at least two different non-animal hydrolyzates in the combined feed solution are a plant-based hydrolyzate and a non-animal or plant-based hydrolyzate. In one embodiment, the hydrolyzate that is not animal based or plant based is a yeast based hydrolyzate. In one embodiment, the plant-based hydrolyzate is a soy-based hydrolyzate.
<img file="MX353340B_D0042.tif" />
IMPI rNSTTTUTO MEXICANO
BE LA PROP1EBAD INDUSTRIAL
<img file="MX353340B_D0043.tif" />
In one embodiment, the combined feeding solution comprises a basal medium that is either PF-CHO or a medium
DMEM / F12. In one embodiment, the basal cell medium is a modified basal medium, and excludes the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, phosphate
<td>dibasic sodium, a regulator</td><td>of</td><td colspan="2">osmolarity,</td><td>an agent</td>
<td>surfactant, glutamine and glucose.</td><td></td><td></td><td></td><td></td>
<td>In yet another mode,</td><td>the</td><td>solution</td><td>of</td><td>feeding</td>
<td>combined it also has a</td><td colspan="2">turbidity</td><td>of</td><td>less than</td>
<td>approximately 15 UTN.</td><td></td><td></td><td></td><td></td>
<td>The invention characterized</td><td>a</td><td>method</td><td>for</td><td>keep a</td>
constant glucose level of a cell culture production medium comprising adding the combined feeding solutions described herein.
Another aspect of the invention is a method of making a combined feeding solution comprising a basal medium, glucose, and at least two different non-animal hydrolyzates, comprising combining glucose and the basal cellular medium in a solution; adjust the pH of the solution of a) to about 9.5 to 10.5; add the at least two different hydrolyzates that are not of animal origin to the solution of b); and adjusting the pH of the solution in c), so that the combined feed solution has a pH of approximately 6.5 to 7.5. In one embodiment, step c) comprises adding a first hydrolyzate that is not of animal or plant-based origin, and an i
<img file="MX353340B_D0044.tif" />
IMPI
MEXICAN INSTITUTE
D5 The PRMEDAB
INDUSTRIAL second plant-based hydrolyzate. In one embodiment, the hydrolyzate that is not animal based or plant based is a yeast based hydrolyzate. In yet another embodiment, the plant-based hydrolyzate is a soy-based hydrolyzate.
The invention further provides methods of increasing the production of proteins, eg, antibody or antigen-binding portions thereof, from mammalian cell cultures. The invention provides a method of producing at least about 1.5 g / L of an antibody from a mammalian cell culture, comprising culturing mammalian cells, comprising culturing mammalian cells in a cell culture production medium; and adding a combined feeding solution having a pH of about 6.7 to 7.2 to the cell culture production medium, wherein the combined feeding solution comprises glucose; a basal cell medium; a different amino acid from glutamine; and at least two different non-animal hydrolyzates, so that at least about 1.5 g / L of the antibody is produced. In one embodiment, at least 2 g / L of the antibody is produced. In another embodiment, at least 4 g / L of the antibody is produced. In yet another embodiment, at least 5 g / L of the antibody is produced. In a further embodiment, the invention provides a method of producing approximately 6 g / L of an antibody.
In one embodiment, the combined feeding solution comprises about 100 to 250 g / kg of glucose.
<img file="MX353340B_D0045.tif" />
<img file="MX353340B_D0046.tif" />
The invention also provides a method for increasing the titer of an antibody produced from a mammalian cell culture, comprising culturing mammalian cells comprising a nucleic acid encoding the antibody in a cell culture production medium; and adding a combined feeding solution having a pH of about 6.7 to 7.2 to the cell culture production medium, wherein the combined feeding solution comprises glucose; a basal cell medium; a different amino acid from glutamine; and at least two different hydrolyzates that are not of animal origin, so that the titer of the antibody produced is at least 50% more than that of a control mammalian cell culture that is cultured according to step a) and excluding the stage b). In one embodiment, the titer of the antibody produced is at least 100% more than that of the control. In another embodiment, the titer of the antibody produced is at least 150% higher than that of the control.
In one embodiment, the combined feeding solution is added when the cell density reaches at least 2.0 x 10<sup>6 </sup>cells / mL. In one embodiment, the combined feeding solution is added when the cell density reaches at least 3.5 x 10<sup>6</sup> cells / mL.
The invention further provides a method of producing a protein, for example an antibody or antigen-binding portion thereof, in a mammalian cell culture comprising culturing mammalian cells comprising an acid.
IMPI
<img file="MX353340B_D0047.tif" />
nucleic encoding the protein, in a cell culture production medium; and adding a combined feeding solution to the cell culture production medium, using a feedback control system to monitor the concentration of a metabolic indicator in the cell culture production medium, where the combined feeding solution is added to the medium of cell culture production at a point in time, determined by the feedback control system, for the antibody to be produced. In one embodiment, the metabolic indicator is glucose or glutamine. In another embodiment, the feeding solution is a combined feeding solution comprising glucose; a basal cell medium; a different amino acid from glutamine; and at least two different hydrolyzates that are not of animal origin. In one embodiment, the antibody is an anti-TNFa antibody, an anti-IL-12 antibody, an anti-IL-18 antibody, and an antibody against the EPO receptor (EPO-R).
In one embodiment, a titer of at least 1.5 g / L of the antibody is produced using the methods of the invention. In another embodiment, a titer of at least 2 g / L is produced.
In one embodiment of the invention, the combined feeding solution comprises about 3.0 to 12.5 g / kg asparagine.
In one embodiment of the invention, the combined feeding solution comprises about 100 to 200 g / kg of glucose.
<img file="MX353340B_D0048.tif" />
MEXICAN INSTITUTE OF INDUSTRIAL PROPERTY
In yet another embodiment, the invftnr.ion additionally nnmprpndA monitor a glucose concentration in the cell culture medium, so that the glucose level is maintained between approximately 0.25 and 20.0 g / L. In one embodiment, the glucose concentration is monitored using an automated sampling apparatus.
In one embodiment, the antibody or antigen-binding portion thereof, which is produced using the methods and compositions described herein, is selected from the group consisting of an anti-TNFa antibody, an anti-IL-18 antibody, a antibody against the EPO-R receptor, and an anti-IL-12 antibody. In one embodiment, the antibody, or antigen-binding portion thereof, is a fully human antibody. In one embodiment, the anti-TNFa antibody is D2E7 (adalimumab). In one embodiment, the anti-IL-18 antibody is ABT-325. In one embodiment, the anti-IL-12 antibody is ABT-874.
The invention also provides a method of determining a feeding profile for producing a protein in a mammalian cell culture, comprising culturing mammalian cells comprising a nucleic acid encoding the antibody in a cell culture production medium; and adding a combined feeding solution to the cell culture production medium, using a feedback control system to monitor a metabolic indicator in the cell culture production medium, where the combined feeding solution is
<img file="MX353340B_D0049.tif" />
IMPI
MEXICAN INSTITUTE added to the cell culture production medium to meet a set point of the target metabolic indicator; and determining the amount of the combined feeding solution added to the cell culture production medium per day, so that the feeding profile is determined. In one embodiment, the metabolic indicator is glucose or glutamine.
The invention also includes a batch feeding method for producing a protein in a mammalian cell culture, comprising adding a combined feeding solution to the mammalian cell culture, in accordance with the determined feeding profile, using the methods of the invention.
Another aspect of the invention are improved cell culture media including sodium butyrate and / or N-acetylcysteine. The invention characterized a method of producing an antibody in a mammalian cell culture so that the titer of the antibody is at least 300 mg / L, said method comprises culturing mammalian cells comprising a nucleic acid encoding the antibody in a medium cell culture production; add sodium butyrate, N-acetylcysteine, or a combination thereof, to the cell culture medium, where sodium butyrate is added at a final concentration of about 0.1mM to 10mM, and N-acetylcysteine is added to a final concentration of about 1 mM to 80 mM, so that the antibody is produced at a titer of at least 300 mg / L. In one modality, the title of the
<img file="MX353340B_D0050.tif" />
IMPI
MUUCANO INSTITUTE
BE LA W3MEDAC
INDUSTRIAL antibody is at least about 100 mg / L.
In the modality, the antibody titer is at least about 200 mg / L. In one embodiment, the antibody titer is at least about 250 mg / L. In one embodiment, the antibody titer is at least about 300 mg / L. In one embodiment, the antibody titer is at least about 400 mg / L.
The invention also provides a method of producing an antibody in a mammalian cell culture so that the antibody titer is at least 10% higher than that of a control mammalian cell culture, said method comprising a) culturing mammalian cells. comprising a nucleic acid encoding the antibody in a cell culture production medium; and
b) adding sodium butyrate, N-acetylcysteine, or a combination thereof, to the cell culture medium, where sodium butyrate is added at a final concentration of about 0.1mM to 10mM and the N-acetylcysteine is added at a final concentration of about 1 mM to 80 mM, so that the antibody titer is at least 10% higher than that of the control, where the control mammalian cell culture comprises step a) and excludes step b) . In one embodiment, the antibody titer of the mammalian cell culture is improved by at least 29% relative to the control mammalian cell culture. In one embodiment, the antibody titer of the mammalian cell culture is improved by at least 40% relative to the mammalian cell culture of
MEXICAN INSTITUTE »f LA INDUSTRIAL CONTROL control. In one embodiment, the titer of the antiruarpn riai mammalian cell culture is enhanced by at least control mammalian cell culture.
70% with respect to
In one embodiment, the antibody titer of the mammalian cell culture is at least
90% greater than that of the control mammalian cell culture.
In one embodiment, sodium butyrate, Nacetylcysteine, or a combination thereof is added to the mammalian culture during the growth phase of the mammalian cell cell culture. In one embodiment, sodium butyrate, Nacetylcysteine, or a combination thereof is added to the mammalian cell culture between days 4 and 7 of culture time.
In one embodiment, sodium butyrate, Nacetylcysteine, or a combination thereof is added to the mammalian cell culture on day 0 of culture time.
In another embodiment, the final concentration of sodium butyrate is approximately 0.1mM to 10mM. In one embodiment, the final concentration of sodium butyrate is from about 0.1mM to 8.0mM. In one embodiment, the final concentration of sodium butyrate is from about 0.1mM to 3.0mM sodium butyrate.
In one embodiment, the final concentration of Nacetylcysteine is from about 20mM to 60mM. In one embodiment, the final concentration of the N-acetylcysteine is approximately 10mM. In one embodiment, the final concentration of the N-acetylcysteine is approximately 8mM.
\ f
IMPI
MEXICAN INSTITUTE p £ LA INDUSTRIAL WLOPTITY
<img file="MX353340B_D0051.tif" />
The invention further provides a method for nvtnnri the longevity of a mammalian cell culture at least 35% compared to a control mammalian cell culture, said method comprising a) culturing mammalian cells comprising a nucleic acid encoding the antibody in a cell culture production medium; and b) adding approximately 1mM to 80mM N-acetylcysteine to the cell medium; so that the longevity of the mammalian cell culture is extended by at least 35% compared to a control mammalian cell culture, wherein the control mammalian cell culture comprises step a) and excludes step b).
In one embodiment, the longevity of the mammalian cell culture is extended by at least about 45% compared to the control mammalian cell culture. In one embodiment, the longevity of the mammalian cell culture is extended by at least about 55% compared to the control mammalian cell culture.
In one embodiment, the method of the invention features adding a final concentration of approximately 8mM Nacetylcysteine to the cell culture production medium.
In one embodiment, the antibody, or antigen-binding portion thereof, is selected from the group consisting of an anti-TNFa antibody, an anti-IL-18 antibody (eg ABT325), and an anti-IL-12 antibody.
The invention provides a free cell culture medium
IMPI
<img file="MX353340B_D0052.tif" />
MEXICAN INSTITUTE OF INPUSTRIAL PROPERTY OF SERUM comprising Part A, Part B and Part C, where Part A consists essentially of a modified basal medium that excludes the following components: sodium bicarbonate, a regulatory solution, monobasic sodium phosphate , dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; Part B consists essentially of a source of inorganic iron; and Part C comprises a recombinant growth factor; a regulatory solution; an osmolarity regulator; a source of energy; and at least two different hydrolyzates that are not of animal origin. In one embodiment, Part C consists essentially of a recombinant growth factor; a regulatory solution; an osmolarity regulator; a source of energy; and at least two different hydrolyzates that are not of animal origin.
The invention also provides a serum-free cell culture production medium comprising a modified basal medium having a reduced vitamin content and excluding the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate , an osmolarity regulator, a surfactant, and glucose monosaccharide; approximately 10 mL / kg or 122.45 mg / L of ferric citrate; approximately 6.5 mL / kg or 13 mg / kg of recombinant human insulin; approximately 7.0 g / kg of anhydrous glucose; about 0.58 to 0.59 g / kg L-glutamine; approximately 1.6 g / kg of baking soda, approximately 1.8 g / kg of
<img file="MX353340B_D0053.tif" />
<img file="MX353340B_D0054.tif" />
<img file="MX353340B_D0055.tif" />
HEPES; about 2.45 g / kg NaCI; about 1.0 g / kg Pluronic F-68; about 0.03 to 0.04 g / kg of
NaH<sub>2</sub>PO<sub>4</sub>»H<sub>2</sub>OR; approximately 0.43 to 0.44 g / kg Na<sub>2</sub>HPO<sub>4</sub>»7H<sub>2</sub>OR;
approximately 10.7 g / kg of yeast-based hydrolyzate; and approximately 6.9 to 7.0 g / kg of plant-based hydrolyzate.
The invention also provides a serum-free cell culture medium comprising: a modified basal medium having a reduced vitamin content and excluding the following components: sodium bicarbonate, buffer, monobasic 1 q sodium phosphate, sodium phosphate dibasic, an osmolarity regulator, a surfactant, and glucose monosaccharide; approximately 150 g / kg of anhydrous glucose; about 5.0 g / kg L-asparagine monohydrate; about 1.6 g / kg of sodium bicarbonate; about 65 g / kg yeast-based hydrolyzate 15; and approximately 41 g / kg of plant-based hydrolyzate.
The invention further provides a serum free cell culture medium comprising: a modified basal medium having a reduced vitamin content and excluding the following 20 components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate , an osmolarity regulator, a surfactant, and glucose monosaccharide; approximately * 10 mL / kg or 122.45 mg / L of ferric citrate; approximately 6.5 mL / kg or 13 mg / kg of recombinant human insulin; approximately 200 g / kg of anhydrous glucose;
<img file="MX353340B_D0056.tif" />
approximately 0.58 to 0.59 g / kg l -glutamine · apmvimaHamanta 1.6 g / kg sodium bicarbonate, approximately 1.8 g / kg HEPES; about 2.45 g / kg NaCI, about 1.0 g / kg Pluronic F-68; approximately 0.03 to 0.04 g / kg NaH<sub>2</sub>PO<sub>4</sub>»H<sub>2</sub>OR; approximately 0.43 to 0.44 g / kg Na<sub>2</sub>HPO<sub>4</sub>"7H<sub>2</sub>OR; approximately 10.7 g / kg of yeast-based hydrolyzate; and approximately 6.9 to 7.0 g / kg of plant-based hydrolyzate.
The invention also provides the following improved media modalities. The invention includes an improved medium for culturing CHO cells expressing recombinant biological products comprising Parts A, B and C, wherein: Part A comprises water, amino acids, vitamins and other cofactors; Part B comprises a source of inorganic iron; and Part C comprises recombinant growth factors, regulatory solutions, an osmolarity regulator, an energy source, non-ferrous metal ions, hydrolyzates, and additional agents.
In one embodiment, Part C comprises sodium bicarbonate, HEPES, monobasic and dibasic sodium phosphates, sodium chloride, Pluronic F-68, and glucose. In another embodiment, 1.5 g / L of sodium bicarbonate are added. In an additional modality, 1.8 g / L of HEPES is added. In yet another embodiment, 0.1-0.5 g / L of monobasic and dibasic sodium phosphates are added. In yet another embodiment, 1 g / L is added to 6.5 g / L of sodium chloride. In an additional modality, 1.0 g / L of Pluronic F-68 is added. In a
INDUSTRIAL
<img file="MX353340B_D0057.tif" />
In this way, 1 g / L is added to 7 g / L of glucose. In one embodiment, the vitamins are selected from the group consisting of PABA (p-aminobenzoic acid), biotin, Calcium D-Pantothenate (vitamin B5), folic acid, l-lnositol, niacinamide, pyridoxine (vitamin B6), riboflavin ( vitamin B2), thiamine (vitamin B1), and cyanocobalamin (vitamin B12). In another embodiment, the other cofactors are selected from the group consisting of lipid factors, an alcoholamine, amino acids, and peptides. In yet another embodiment, lipid factors are selected from the group consisting of choline chloride and phosphatidylcholine. In yet another embodiment, an alcoholamine is ethanolamine. In one embodiment, amino acids are selected from the group consisting of asparagine, glutamine, and putrescine.
In one embodiment, the peptide is glutathione. In one embodiment, 0.4 mg / L is added to 1.65 mg / L glutathione.
In yet another embodiment, the source of inorganic iron in Part B is ferric citrate. In one embodiment, 10 mL / L or 122 mg / L of ferric citrate is added. In yet another embodiment, ferric citrate is maintained at a concentration of 122 mg / L. In one embodiment, the recombinant growth factor is insulin or a recombinant analog, IGF-1, or a combination of insulin and IGF-1. In one embodiment, 4 mg / L is added to 13 mg / L insulin or a recombinant analog. In another embodiment, 25 ng / L is added to 150 ng / L of IGF-1. In yet another embodiment, 50 ng / L is added to 100 ng / L of IGF-1. In yet another modality, 25 ng / L a150 are supplied
IMPI
<img file="MX353340B_D0058.tif" />
ng / L of IGF-1 to insulin. In a modality ·, · € β ·· & ΜρΙβΓη8ηΐαη 60 ng / L to 100 ng / L of IGF-1 to insulin.
In yet another embodiment, the osmolarity regulator is selected from the group consisting of NaCI, KCI, KNO<sub>3</sub>. In one embodiment, 0 g / L to 10 g / L of osmolarity regulator are added. In another embodiment, 0 g / L is added to 6.5 g / L of osmolarity regulator.
In yet another embodiment, the energy source is a monosaccharide, eg, glucose (eg, D-glucose), maltose, trickle, galactose, and fructose. In one embodiment, 1.0 to 7.0 g / L of glucose is added. In another embodiment, 1.5 to 5.0 g / L of glucose are added.
In yet another embodiment, the non-ferrous metal ions are added in the form of chloride and sulfate salts. In one embodiment, the non-ferrous metal ions are selected from the group consisting of potassium, magnesium, cupric, setenium, zinc, nickel, manganese, tin, cadmium, molybdate, vanadate, and silicate. In one embodiment, the buffer solution is selected from the group consisting of carbonates, chlorides, sulfates, and phosphates. In one embodiment, the buffer is selected from the group consisting of NaHCO<sub>3</sub>, CaCI<sub>2</sub>, MgSO<sub>4</sub>, NaH<sub>2</sub>PO<sub>4</sub>, Na<sub>2</sub>HPO<sub>4</sub>, C<sub>3</sub>H<sub>3</sub>OR<sub>3</sub>Na and N- [2-hydroxyethyl] piperazin-N '- [2-ethanesulfon] acid known as HEPES.
In one embodiment of the invention, one of the additional agents added to the methotrexate medium. In one embodiment, the
METHOTREXATE MEXICAN INSTITUTE OF PHOPIEDAO INDUSTRIAL is used to grow CHO cells that express__ anti-IL-18, anti-IL12, anti-TNF-alpha antibodies (for example, fully human anti-TNFa antibodies), or antibodies against
EPO-R. In one embodiment, 100 nM to 5000 nM are added. In one embodiment, 500 nM of methotrexate is added to the medium. In one embodiment, 100 nM of methotrexate are added. In one embodiment, 5000 nM of methotrexate are added.
In yet another embodiment of the invention, one of the additional agents is a cell protector, eg, methylcellulose or Pluronic polyol (eg, Pluronic F-68).
add
0.5 g / L to 1.0 g / L of methylcellulose.
add
Pluronic F-68 0.5 g / L to 1.0 g / L.
<td>In</td><td>a</td><td>modality,</td><td>I know</td>
<td>In</td><td>a</td><td>modality,</td><td>I know</td>
<td>In</td><td>a</td><td>modality,</td><td>I know</td>
add
Pluronic F-68 0.7 g / L to 1.2 g / L.
In yet another embodiment, the pH of Part A is increased to a maximum pH of 10. In one embodiment, the pH of the
Part A is subsequently reduced to a minimum of 7.0 as the hydrolyzates are added.
The invention also provides an improved medium for cells.
CHO expressing a fully human anti-TNF-alpha antibody, comprising: 10.0 mL / kg or 122 mg / kg of ferric citrate; 2 mL / kg or 4.0 mg / kg of recombinant human insulin;
3.5 g / kg of anhydrous glucose; 0.292 g / kg L-glutamine; 1.6 g / kg of sodium bicarbonate; 0.031 g / kg NaH<sub>2</sub>PO4-H<sub>2</sub>OR; 0.436 g / kg of
The invention also provides an improved means for
Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR; 2.0 g / kg of hydrolyzate; and 2.50 mL / kg of methotrexate.
<img file="MX353340B_D0059.tif" />
IMPI CHO cells expressing a fully human antbTNF alpha antibody, comprising: 10.0 mL / kg or 122 mg / kg of ferric citrate; 6.0 mL / kg or 12 mg / kg of recombinant human insulin; 7.0 g / kg anhydrous glucose; 0.584 g / kg L-glutamine; 1.6 g / kg of sodium bicarbonate; 1.8 g / kg HEPES; 2.45 g / kg NaCI; 1.0 g / kg Pluronic F-68; 0.031 g / kg NaH<sub>2</sub>PO<sub>4</sub>-H<sub>2</sub>OR; 0.436 g / kg of Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR; 10.7 g / kg of hydrolyzate; 6.92 g / kg of Phytone peptone; and 2.50 mL / kg of methotrexate.
Also included in the invention is an improved medium for CHO cells expressing a fully human anti-TNF-alpha antibody, comprising: 10 mL / kg or 122 mg / L ferric citrate; 3.88 mL / kg or 7.8 mg / kg of recombinant human insulin; 7.0 g / kg anhydrous glucose; 0.876 g / kg L-glutamine; 0.45 g / kg L-asparagine monohydrate; 1.6 g / kg of sodium bicarbonate; 1.8 g / kg HEPES; 2.67 g / kg NaCI; 1.0 g / kg Pluronic F-68; 0.031 g / kg NaH<sub>2</sub>PO<sub>4</sub>-H<sub>2</sub>OR; 0.436 g / kg of Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR; 10.7 g / kg of hydrolyzate; 6.92 g / kg of Phytone peptone; and 2.50 mL / kg of methotrexate.
The invention further provides an improved medium for CHO cells expressing a fully human anti-TNF-alpha antibody, comprising: 10 mL / kg or 122 mg / L ferric citrate; 3.88 mL / kg or 7.8 mg / kg of recombinant human insulin; 7.0 g / kg anhydrous glucose; 0.876 g / kg L-glutamine; 0.45 g / kg L-asparagine monohydrate; 1.6 g / kg of sodium bicarbonate; 1 g / kg HEPES; 2.67 g / kg NaCI; 1.0 g / kg Pluronic F-
<img file="MX353340B_D0060.tif" />
68; 0.031 g / kg NaH<sub>2</sub>PO<sub>4</sub>-H<sub>2</sub>OR; 0.436 g / kg of Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR; 4.0 g / kg of hydrolyzate; 2.6 g / kg peptone Phytone; and d 2.50 mL / kg of methotrexate.
Another aspect of the invention is an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 10 mL / kg or 122 mg / L of ferric citrate; 3.88 mL / kg or 7.8 mg / kg of recombinant human insulin; 7.0 g / kg anhydrous glucose; 0.876 g / kg L-glutamine; 0.45 g / kg L-asparagine monohydrate; 1.6 g / kg of sodium bicarbonate; 1.8 g / kg HEPES; 2,675 g / kg NaCI; 1.0 g / kg Pluronic F-68; 0.031 g / kg NaH<sub>2</sub>PO<sub>4</sub>-H<sub>2</sub>OR; 0.436 g / kg of Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR; 4.0 g / kg hydrolyzed yeast source; 2,579 g / kg of Phytone peptone; and 2.50 mL / kg of methotrexate.
The invention provides an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 10 mL / kg or 122 mg / L of ferric citrate; 6.5 mL / kg or 13 mg / kg of recombinant human insulin; 7.0 g / kg anhydrous glucose; 0.584 g / kg Lglutamine; 1.6 g / kg of sodium bicarbonate; 1.8 g / kg HEPES; 2.45 g / kg NaCI; 1.0 g / kg Pluronic F-68; 0.031 g / kg NaH<sub>2</sub>PO<sub>4</sub>-H<sub>2</sub>OR; 0.436 g / kg of Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR; 10.7 g / kg of yeast hydrolyzate; and 6.92 g / kg of Phytone peptone.
The invention provides an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 150.0 g / kg anhydrous glucose; 5.0 g / kg L-asparagine monohydrate; 65.0 g / kg of yeast hydrolyzate; and 41.0 g / kg of Phytone peptone.
<img file="MX353340B_D0061.tif" />
so IMPI
MEXICAN INSTITUTE
OF THE PROPERTY
INDUSTRIAL
The invention also provides an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 10 mL / kg or 122 mg / kg of ferric citrate; 6.5 mL / kg or 13 mg / kg of recombinant human insulin; 200.0 g / kg anhydrous glucose; 0.584 g / kg L-glutamine; 1.6 g / kg of sodium bicarbonate; 1.8 g / kg HEPES; 2.45 g / kg NaCI; 1.0 mL / kg Pluronic F-68; 0.031 g / kg NaH<sub>2</sub>PO<sub>4</sub>-H<sub>2</sub>OR; 0.436 g / kg of Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR; 10.7 g / kg of yeast hydrolyzate; and 6.92 g / kg of Phytone peptone.
The invention includes an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 10 mL / kg or 122 mg / kg of ferric citrate; 2 mL / kg or 4 mg / kg of recombinant human insulin; 3.5 + 1.5 g / kg of anhydrous glucose; 0.292 g / kg L-glutamine; 1.6 g / kg of sodium bicarbonate; 2 g / kg of yeast hydrolyzate; and 0.25 mL / kg of methotrexate.
The invention includes an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 10 mL / kg or 122 mg / kg of ferric citrate; 2 mL / kg or 4 mg / kg of recombinant human insulin; 3.5 + 1.5 g / kg of anhydrous glucose; 0.292 g / kg L-glutamine; 1.6 g / kg of sodium bicarbonate; 11 g / kg of yeast hydrolyzate; and 0.250 mL / kg of methotrexate.
The invention includes an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 10 mL / kg or 122 mg / kg of ferric citrate; 2 mL / kg or 4 mg / kg of recombinant human insulin; 200 g / L anhydrous glucose; 0.292 g / kg Lglutamine; 1.6 g / kg of sodium bicarbonate; 8 g / kg hydrolyzate of
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yeast; and 0.250 mL / kg of methotrexate.
The invention includes an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 10 mL / kg or
122 mg / kg of ferric citrate; 3.88 mL / kg or 7.76 mg / L of recombinant human insulin; 7.0 g / L dextrose anhydrous; 0.876 g / L of Lglutamine; 1.6 g / kg of sodium bicarbonate; 1.8 g / L HEPES; 2.67 g / L NaCI; 1.0 g / L Pluronic; 0.031 g / L NaH<sub>2</sub>PO<sub>4</sub>«H<sub>2</sub>OR; 0.436 g / L Na<sub>2</sub>HPO4 «7H<sub>2</sub>OR; 4.0 g / L of yeastolate; 2,579 g / L peptone Phytone; 0.05 mL / kg of methotrexate; 3.5 mL / L of 2N NaOH; and 2.91 g / L of 2N HCI; which results in a final pH of 7.10 to 7.20 and a final osmolarity of 373 to 403 mOsm / kg.
The invention includes an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 10 mL / kg or 122 mg / kg of ferric citrate; 13 mg / L of recombinant human insulin; 7.0 g / L dextrose anhydrous; 0.584 g / L L-glutamine; 1.6 g / kg of sodium bicarbonate; 1.8 g / L HEPES; 2.45 g / L of NaCI; 1.0 g / L Pluronic; 0.031 g / L NaH<sub>2</sub>PO<sub>4</sub>»H<sub>2</sub>OR; 0.436 g / L of Na<sub>2</sub>HPO<sub>4</sub>»7H<sub>2</sub>OR; 10.7 g / L yeastolate; 6.92 g / L Peptone Phytone; 0.05 mL / kg of methotrexate; 5.67 mL / L of 2N NaOH; and 2.5 g / L of 2N HCI; which results in a final pH of 7.10 to 7.20 and a final osmolarity of
373 at 403 mOsm / kg.
The invention includes an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 10 mL / kg or 122 mg / kg of ferric citrate; 4 mg / kg of recombinant human insulin; 1.5 g / kg dextrose anhydrous; 0.292 g / kg L-glutamine; 1.6
<img file="MX353340B_D0063.tif" />
IMPI
ΙΝϊΤΠνΤΟ MEXICAN
OF THE PROPERTY
INDUSTRIAL g / kg of sodium bicarbonate; 2.0 g / L of yeastelate · and O.ff IIIL / Ky'fl'g methotrexate; which results in a final pH of 7.10 to 7.30 and a final osmolarity of 300 to 340 mOsm / kg.
The invention includes an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 10 mL / kg or 122 mg / kg of ferric citrate; 13 mg / kg of recombinant human insulin; 7.0 g / kg dextrose anhydrous; 0.584 g / kg L-glutamine; 1.6 g / kg of sodium bicarbonate; 1.8 g / kg HEPES; 2.45 g / kg NaCI; 1.0 g / kg Pluronic F-68; 0.031 g / kg NaH<sub>2</sub>PO<sub>4</sub>»H<sub>2</sub>OR; 0.436 g / kg of Na<sub>2</sub>HPO<sub>4</sub>»7H<sub>2</sub>OR; 10.7 g / L yeastolate; and 6.92 g / kg of Phytone peptone; 5.67 mL / kg NaOH; and 2.5 mL / kg of HCI; which results in a final pH of 7.10 to 7.20 and a final osmolarity of 373 to 403 mOsm / kg.
The invention includes an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 10 mL / kg or 122 mg / kg of ferric citrate; 7.76 mg / kg of recombinant human insulin; 7.0 g / L dextrose anhydrous; 0.876 g / kg L-glutamine; 1.6 g / kg of sodium bicarbonate; 1.8 g / kg HEPES; 2.67 g / kg NaCI; 1.0 g / kg Pluronic F-68; 0.031 g / kg NaH<sub>2</sub>PO<sub>4</sub>* H<sub>2</sub>OR; 0.436 g / kg of Na<sub>2</sub>HPO<sub>4</sub>»7H<sub>2</sub>OR; 4.0 g / L of yeastolate; and 2,579 g / L of Phytone peptone; 0.05 mL / L of methotrexate; 3.5 mL / kg NaOH; and 2.91 mL / kg of HCI; which results in a final pH of 7.10 to 7.20 and a final osmolarity of 373 to 403 mOsm / kg.
The invention includes an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 10 mL / kg or
IMPI «Mexican NSTmrro □ £ LA monedad 'tNaiKTMAL
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122 mg / kg of ferric citrate;
mg / kg of recombinant human insulin; 7.0 g / L dextrose anhydrous; 0.584 g / kg L-glutamine; 1.6 g / kg of sodium bicarbonate; 1.8 g / kg HEPES; 2.45 g / kg NaCI;
1.0 g / kg Pluronic F-68; 0.031 g / kg NaH<sub>2</sub>PO<sub>4</sub>«H<sub>2</sub>OR; 0.436 g / kg of
Na<sub>2</sub>HPO<sub>4</sub>* 7H<sub>2</sub>OR; 10.7 g / L yeastolate; and 6.92 g / L of peptone
Phytone; 0.05 mL / L of methotrexate; 5.67 mL / kg NaOH; and 2.5 mL / kg of HCI; which results in a final pH of 7.10 to 7.20 and a final osmolarity of 373 to 403 mOsm / kg.
The invention includes an improved medium for CHO cells expressing an anti-IL-18 antibody comprising: 10 mL / kg or 122 mg / kg of ferric citrate; 13 mg / kg of recombinant human insulin; 7.0 g / L dextrose anhydrous; 0.584 g / kg L-glutamine; 1.6 g / kg of sodium bicarbonate; 1.8 g / kg HEPES; 1.0 g / kg Pluronic F-68; 0.031 g / kg NaH<sub>2</sub>PO4 »H<sub>2</sub>OR; 0.436 g / kg of
Na<sub>2</sub>HPO<sub>4</sub>»7H<sub>2</sub>OR; 14.27 g / L yeastolate; 9.23 g / L Peptone Phytone; 0.05 mL / L of methotrexate; 8.95 mL / kg NaOH; and 4.1 mL / kg of HCI; which results in a final pH of 7.10 to 7.20 and a final osmolarity of 373 to 403 mOsm / kg.
The invention also features a method of increasing the productivity of a CHO cell line that produces an IgG1 antibody, by increasing the final titer, which comprises: adding sodium butyrate and adding N-acetylcysteine. In one embodiment, the IgG1 antibody is an anti-IL-18 antibody.
In one modality, the increase in productivity is measured by an increase in the final title. In one modality, the increase in
<img file="MX353340B_D0065.tif" />
final title is achieved by adding
IMPI
INSTITUTO MEXICANO DE LA KOHEDAΓ industrial sodium butyrate at a concentration of 0.1 mM to 10 mM.
In one embodiment, the sodium butyrate concentration is 0.1 mM to 8.0 mM.
In one embodiment, the concentration of sodium butyrate is 0.1 mM to 3.0 mM. In one embodiment, the concentration of sodium butyrate is
0.125 mM to 2.0 mM. In one embodiment, the butyrate concentration
<td colspan="4">sodium is 0</td><td>.125 mM.</td><td>In</td><td>a</td><td>modality,</td><td>the</td><td>increase</td><td>in</td><td>the</td>
<td>Title</td><td>fine'</td><td>is</td><td>of</td><td> 10-80%.</td><td>In</td><td>a</td><td>modality,</td><td>the</td><td>increase</td><td>in</td><td>the</td>
<td>Title</td><td>final</td><td>is</td><td>of</td><td> 20-60%.</td><td>In</td><td>a</td><td>modality,</td><td>the</td><td>increase</td><td>in</td><td>the</td>
<td>Title</td><td>final</td><td>is</td><td>of</td><td> 35-55%.</td><td>In</td><td>a</td><td>modality,</td><td>the</td><td>increase</td><td>in</td><td>the</td>
<td>Title</td><td>final</td><td>is</td><td>of</td><td>40%. In</td><td>a</td><td colspan="6">modality, the longevity of the crop</td>
<td colspan="4">improved cell</td><td>is achieved</td><td colspan="2">through</td><td>the addition</td><td>of</td><td colspan="2">N-acetylcysteine</td><td>to</td>
a concentration of 0.1 mM to 10 mM. In one embodiment, the increase in cell culture longevity is 5-50%.
The invention also provides a cell culture medium that increases the productivity of a CHO cell line that produces an IgG1 antibody by increasing the final titer, comprising: SR-371 medium and sodium butyrate. In one embodiment, the IgG1 antibody is an anti-IL-18 antibody. In one embodiment, the increase in productivity is measured by increasing the final anti-IL-18 titer by 10-80%. In one embodiment, the increase in productivity is measured by increasing the final anti-IL-18 titer by 20-60%. In one embodiment, the increase in productivity is measured by increasing the final anti-IL-18 titer by 35-55%. In one modality, the increase in productivity is
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MEXICAN INSTITUTE OF INDUSTRIAL CKOHIDAD Xe,
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measured by 40% increase in final titer of anti, n -1 «. In one embodiment, the concentration of the added sodium butyrate is 0.125 mM to 8.0 mM. In one embodiment, the concentration of the added sodium butyrate is 0.2 mM to 3.0 mM. In one embodiment, the concentration of the added sodium butyrate is 0.3 mM to 2.0 mM. In one embodiment, the concentration of the added sodium butyrate is 0.125 mM. In one embodiment, the concentration of the added N-acetylcysteine is 1mM to 10mM. In one embodiment, the concentration of the added N-acetylcysteine is 5mM to 10mM. In one modality, the average final title is increased by 5-50%. In one modality, the average final title is increased by 15-35%. In one modality, the average final title is increased by 25-35% Description of the Figure
Figure 1 is a graph showing the growth titer of ABT-874 as a function of viable cell density at seeding. The results of the titration on day 15 are strongly correlated with the density of viable cells at seeding. A polynomial fit to the above data suggests that the optimal feed density occurs at about 3.5 x 10<sup>6</sup> cells / mL. The process parameters were pH = 6.9, T = 35 ° C, DO = 40%, inoculum ratio 1: 5 or 1: 4 in 4X medium; feeding started at the specified density, 1% initial volume for 10 days.
Detailed description of the invention
Definitions
IMPI
<img file="MX353340B_D0069.tif" />
While the terminology used herein
Application is customary within the art, definitions of certain terms are provided herein to ensure clarity and specificity to the meaning of the claims.
The term antibody, as used herein, is intended to refer to immunoglobulin molecules comprised of four polypeptide chains, two heavy (H) chains, and two light (L) chains interconnected by disulfide bonds. Each heavy chain is comprised of a heavy chain variable region (abbreviated herein as HCVR or VH) and a? constant region of heavy chain. The heavy chain constant region is comprised of three domains, CH1, CH2 and
CH3. Each light chain is comprised of a light chain variable region (abbreviated herein as LCVR or VL) and a light chain constant region. The light chain constant region is comprised of the CL domain. The VH and VL regions may further be subdivided into regions of hypervariability, called complementarity determining regions (CDRs), interspersed with regions that are more conserved, framework regions (FRs). Each VH and VL region is composed of three CDRs and four FRs, arranged from the amino-terminal end to the carboxy-terminal end, in the following order: FR1, CDR1, FR2, CDR2, FR3, CDR3, FR4. Examples of antibody that can be produced using the methods and compositions of the invention include tumor necrosis factor alpha (TNF) -a antibodies (also referred to as anti-TNFa antibodies)
IMPIOS
Mexican INSTITUTE
OS LA FROPIÍUAI) \ '
INO'JSTR.IAL antibodies against interleukin (IL) -12 (also referred to as anti-IL-12 antibodies), antibodies against interleukin (IL) -18 (also referred to as anti-IL18 antibodies), and anti-EPO / R antibodies (also referred to herein as antibodies against EPO / R). Antibodies to TNFa that can be produced using the invention are described in greater detail in US Patent Nos. US 6,090,382; 6,258,562; and 6,509,015, each of which is incorporated herein by reference, in its entirety.
The invention can also be used to produce antibody fragments. The term antigen-binding portion or antigen-binding fragment of an antibody (or simply antibody portion), as used herein, refers to one or more fragments of an antibody that retain the ability to specifically bind to an antigen (eg hTNFa). It has been shown that some fragments of a full-length antibody can perform the antigen-binding function of an antibody. Examples of binding fragments encompassed within the term antigen-binding portion of an antibody, include (i) a Fab fragment, a monovalent fragment consisting of the VL, VH, CL and CH1 domains; (ii) an F (ab ') 2 fragment, a divalent fragment comprising two Fab fragments linked by a disulfide bridge to the hinge region; (iii) an Fd fragment consisting of the VH and CH1 domains; (iv) an Fv fragment consisting of the single arm VL and VH domains of an antibody, (v) a
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IMPI
MEXICAN INSTITUTE • FIA PROPERTY
INDUSTRIAL fragment dAb (Ward et al. (1989) Nature 341: 544-546), consisting of the VH or VL domain; (vi) an isolated complementarity determining region (CDR); and (vii) a dual variable domain antibody (DVD). Furthermore, although the two domains of the Fv fragment, VL and VH are encoded by genes separately, they can be linked, using recombinant methods, by means of a synthetic linker that allows them to be manufactured as a single protein chain, in which the pair of VL and VH regions form single-chain monovalent FV (scFV) molecules, see eg Bird et al. (1988) Science 242: 423-426; and Huston et al. (1988) Proc. Nati. Acad. Sd. USA 85: 5879-5883). Such single-chain antibodies are also encompassed within the term antigen-binding portion of an antibody. Other forms of single chain antibodies, such as diabodies are also encompassed. Diabodies are bispecific dival ntes antibodies, where the VH and VL domains are expressed in a single polypeptide chain, but using a linker that is too short to allow pairing between the two domains in the same chain, so that The domains are thus forced to pair with the complementary domains of another chain, and creating two antigen binding sites (see for example Holliger et al. (1993) Proc. Nati. Acad. Sd. USA 90: 6444-6448; Poljak et al. (1994) Structure 2: 1121-1123). Examples of antibody portions that can be produced by the methods of the invention are described in more detail in the Patents.
<img file="MX353340B_D0071.tif" />
North American Nos. US 6,090,382, 6,258,562, 6,509,015, each of which is incorporated herein by reference, in its entirety. The production of antibody fragments or portions using the methods and compositions of the invention are also included within the scope thereof.
The term recombinant human antibody, as used herein, is intended to include all human antibodies that are prepared, expressed, created and isolated by recombinant means, such as antibodies expressed, using a recombinant expression vector transfected into a cell. host, antibodies isolated from a combinatorial recombinant human antibody library (described below), antibodies isolated from an animal (eg mouse), that is transgenic for human immunoglobulin genes (see, for example, Taylor et al. (1992) Nucí. Acids Res. 20: 6287) or antibodies prepared, expressed, created or isolated by any other means involving the splicing of gene sequences of human immunoglobulin with other DNA sequences. Such recombinant human antibodies have variable and constant regions derived from human germline immunoglobulin sequences. In certain embodiments, however, such recombinant human antibodies are subjected to in vitro mutagenesis (or, when a transgenic animal is used for human Ig sequences, somatic mutagenesis in vivo) and thus the amino acid sequences of the VH regions. and VL of the
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<sup>60</sup> IMPI * MEXICAN INSTITUTE • DE LA ΡΚΟΗΕΟΑΓ
INDlfSTRlAL recombinant antibodies are sequences that, as long as they are derived from and related to human germline VH and VL sequences, may not naturally exist within the human antibody line repertoire, in vivo.
An isolated antibody, as used herein, is intended to refer to an antibody that is substantially free of other antibodies that have different antigenic specificities (eg, an isolated antibody that specifically binds hTNFa, is substantially free of antibodies that specifically bind to antigens other than hTNFa). An isolated antibody that specifically binds hTNFa may, however, have cross-reactivity with other antigens, such as TNFa molecules from other species. Furthermore, an isolated antibody can be substantially free of other cellular and / or chemical materials.
The term basal medium refers to any medium that is layer. to support cell growth. The basal medium supplies standard inorganic salts, such as zinc, iron, magnesium, calcium, and potassium, as well as trace elements, vitamins, an energy source, a regulatory system, and essential amino acids. Examples of basal media include, but are not limited to, Dulbecco's Modified Eagle's Medium (DMEM), DME / F12, Minimum Essential Medium (MEM), Eagle's Basal Medium (MBE), RPMI 1640, F-10, F- 12,
Minimum Essential Medium a (MEM-a), Minimum Essential Medium of
Glasgow (MEM-G), PF CHO (SAFO Biosciences) and Dulbecco's Medium
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<sup>61</sup> IMPI
MEXICAN INSTITUTE
DF. THE PROPERTY
INDUSTRIAL
Modified by Iscove.
The term modified basal medium, as used herein, refers to a basal medium from which at least one standard ingredient, component, or nutrient (i.e., at least one ingredient, component, or nutrient found in a medium basal formulated in a manner customary in the art) has been excluded, decreased or increased. The term modified, as used in the context of the term modified basal medium, can also refer to changes in the proportions between the individual components within the basal medium. In a preferred embodiment of the invention, a modified basal medium excludes at least one of the following components: sodium bicarbonate, a buffer, sodium phosphate (monobasic and / or dibasic), an osmolarity regulator, a surfactant, and glucose, for example, monosaccharide glucose.
As used herein, the terms cell culture medium, culture medium, and medium formulation refer to a nutrient solution for the maintenance, growth, propagation, or expansion of cells in an artificial in vitro medium outside of a multicellular organism or tissue. The cell culture medium can be optimized for a specific cell culture use, including, for example, cell culture growth medium which is formulated to promote cell growth, or cell culture production medium, which is formulated to promote Recombinant protein production s. The terms
<img file="MX353340B_D0074.tif" />
nutrient, ingredient and component, it
IMPI
INSTITUTO MEXICANO DE LA RKONEDAD INDUSTRIAL is used interchangeably herein to refer to the components that constitute a cell culture medium.
The terms "cell culture production medium" or "production medium," as used herein, refers to a cell culture medium designed for use during the production phase of a cell culture. In a preferred embodiment, the production medium is designed for expression of recombinant proteins during the production phase. Examples of means of production are provided herein, including Tables 27 of the Examples Section.
The terms batch-fed cell culture and batch-fed culture, as used herein, refer to a cell culture in which cells, preferably mammalian cells and the culture medium, are supplied to the container of culture initially, and additionally nutrients are fed continuously or in discrete increments to the culture during the culture phase, with or without periodic harvesting of cells and / or product before the end of the culture.
A batch feeding method refers to a method by which a batch feeding cell culture is provided with additional nutrients. For example, a batch feeding method may comprise adding supplemental media in accordance with a given feeding scheme within a given period of time.
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IMPI
MEXICAN INSTITUTE OF INDUSTRIAL PROPERTY
As used herein, the term "feed" refers to any addition of any substance made for a culture after inoculation. Feeding can be one or more additions.
As used herein, the terms "feeding solution and feeding medium" refers to a medium containing one or more nutrients that is added to the culture, starting sometime after inoculation. In one embodiment, the feed solution is a combination feed comprising a basal medium and at least one hydrolyzate, for example a soy-based hydrolyzate, a yeast-based hydrolyzate, or a combination of the two types of hydrolyzates. In another embodiment of the invention, a feed solution can include only a basal medium, such as a concentrated basal medium, or can include only hydrolyzates, or concentrated hydrolyzates.
As used herein, the term feedback control system refers to a process for monitoring a given parameter, whereby an additional agent is added or a modification of the cell culture environment is made, with the in order to fulfill a set point of a desired parameter. In one embodiment, the given parameter is the glucose concentration of a mammalian cell culture, whereby the glucose concentration is used to determine when a feeding solution, eg, a combined feeding solution, should be added to cell culture. You can use a
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IMPI
<img file="MX353340B_D0076.tif" />
feedback control system to maintain the nutritional components necessary to optimize protein production in a mammalian cell culture.
As used herein, the term "feeding profile" refers to a scheme for supplementing a mammalian cell culture with a feeding solution, for example a combined feeding solution. A feed profile is preferably generated using a feedback control system.
Cells can be engineered, to express a specific polypeptide or protein, when the recombinant nucleic acid sequences that allow expression of the polypeptide have been introduced into cells using genetic engineering methods, such as viral infection with a virus. recombinant, transfection, transformation or electroporation. See Kaufman et al. (1990), Meth. Enzymol. 185: 487-511; Current Protocols in Molecular Biology, Ausubel et al., Eds. (Wiley & Sons, New York, 1988, and quarterly updates). The methods and vectors for cells and / or cell lines engineered to express a protein of interest are well known to those of skill in the art. Genetic engineering techniques include, but are not limited to, vectors and expression, homologous targeted recombination and gene activation (see for example US Patent No. 5,272,071 to Chappel) and transactivation by transcription factors.
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engineered (see for example Segal et al., 1999 ,.
Proc. Nati. Acad. Sci. USA 96 (6): 2758-63). Optionally, the polypeptides are expressed under the control of a heterologous control element such as for example a promoter that does not naturally direct the production of that polypeptide. For example, the promoter can be a strong viral promoter (for example CMV,
SV40), which directs the expression of a mammalian polypeptide. The host cell may or may not normally produce the polypeptide.
For example, the host cell may be a CHO cell that has been engineered to produce a human polypeptide, meaning that the nucleic acid encoding the human polypeptide has been introduced into the CHO cell. Alternatively, the host cell may be a human cell that has been engineered to produce increased concentrations of a human polypeptide normally present only at very low concentrations (eg, by replacing the endogenous promoter with a strong viral promoter).
The term growth phase, as used herein, refers to the period during which cultured cells divide rapidly and increase in number. During the growth phase, cells can generally be cultured in a medium and under conditions designed to maximize cell proliferation.
The term hydrolyzed includes any digesting enzyme, particularly a specialized type of extract.
<img file="MX353340B_D0079.tif" />
prepared by treating the substance to be exti dfefa (pui — example, components of plants or yeast cells), with at least one enzyme capable of breaking down the components of the substance in simpler forms (eg, in a preparation comprising monosaccharides or disaccharides and / or monotripeptides or tripeptides). A hydrolyzate can also be enzymatically digested, for example by papain, and / or formed by autolysis, thermolysis and / or plasmolysis. In a preferred embodiment of the invention, the hydrolyzate is not prepared from an animal source; that is, it is not of animal origin. Examples of hydrolyzates that are not of animal origin include plant-based hydrolyzates, eg, the hydrolyzate is not prepared from an animal source, that is, it is not of animal origin. Examples of preferred non-animal origin hydrolyzates include plant-based hydrolyzates, eg, a soy-based hydrolyzate, and hydrolyzates that are not derived from plants or animals, eg, a yeast-based hydrolyzate.
The terms hydrolyzate enrichment solution and hydrolyzate enrichment medium, refers to a medium containing a hydrolyzate or a combination of hydrolyzates, i.e. hydrolyzates extracted from different sources, as a main ingredient that is added to the cell culture. The hydrolyzate enrichment solution can, for example, be added to the cell culture to enhance protein production. Similarly, the terms basal and medium enrichment solution of
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basal enrichment, refers to a queseen medium that has a basal medium (or combination of basal media) as the main ingredient. In one embodiment, a hydrolyzate enrichment solution or a basal enrichment solution or a combination of the two enrichment solutions is added to a cell culture to increase the productivity of a cell culture in the production of a protein.
The production of a protein is increased by adding an additional agent or altering a parameter of the protein production process, if the amount of polypeptide produced in a culture that contains the additional agent or altered parameter of the protein production process is greater than the amount of polypeptide produced in another identical culture that does not contain the additional agent or altered parameter of the protein production process. Examples of alterations to the protein production process include, but are not limited to, addition of supplemental media, increases in the amount of supplemental media, variations in culture temperature, and the oxygen concentration at which cells are cultured. An additional agent can be provided to the cell culture, using a supplemental solution, such as a feed solution.
The term ingredient refers to any compound, if it is of chemical or biological origin, that can be used in cell culture media to maintain or promote the growth of
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IMPI Mexican iNjrrruTo
SAY THE PROPERTY
INDUSTRIAL proliferation of cells. The terms component, nutrient and
..................
Ingredients are used interchangeably and are all intended to refer to such components. Typical ingredients that are used in cell culture media include amino acids, salts, metals, sugars, lipids, nucleic acids, hormones, vitamins, fatty acids, proteins, and the like. Other ingredients that promote or maintain ex vivo cell culture can be selected by those skilled in the art, within the scope of the invention, and in accordance with particular need.
As used herein, the term "inoculation" refers to the addition of cells to a medium to initiate culture.
The term production phase refers to a period during which cells are producing maximum amounts of a recombinant polypeptide or protein. A production phase is characterized by less cell division than during the growth phase, and may also include the use of a culture medium and conditions designed to maximize polypeptide production.
A recombinant polypeptide or recombinant protein is a polypeptide or protein resulting from the genetic engineering process. In a preferred embodiment, the recombinant proteins are obtained from the culture of cells that express said proteins in a cell culture.
The term transition phase means a period of cell culture between a growth phase and a production phase. During the transition phase, the medium and the ΙΜΡΓΟ3
INSTITUTO MEXICANO DE LA PkONEDAD environmental conditions can be modified from dlsenáflás to maximize proliferation with respect to those designed to maximize polypeptide production.
The present invention provides new compositions and processes for the production of proteins, preferably a recombinant protein, for example mammalian antibodies, for example cultures of Chinese Hamster Ovary (CHO) cells. The cell culture media and processes described herein have been used for the production of recombinant proteins, particularly the production of a recombinant monoclonal antibody (fully human, humanized, or chimeric). The media and processes have been modified with respect to numerous antibody production lines to incorporate various improvements and advances, leading to increased growth and productivity of mammalian cells, for example CHO cells. Aspects of the compositions and improved methods of the invention are provided in detail below.
II. Proteins of Interest
Generally, the methods and compositions of the invention are useful for the production of recombinant proteins. Recombinant proteins are produced by the genetic engineering process. Particularly preferred proteins for production in accordance with the methods and compositions of the invention are protein-based therapeutics, also known as biologics. Proteins preferably
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IMPI
THE INDUSTRIAL NORITY O »are secreted as extracellular products.
Proteins that can be produced by the methods and compositions of the invention include, but are not limited to, antibodies or antigen-binding fragments thereof. Numerous techniques are known in the field whereby DNA encoding antibody molecules can be manipulated to produce DNAs capable of encoding recombinant proteins, such as single-chain antibodies, antibodies with enhanced affinity, or other antibody-based polypeptides (see Example Larrick et al., 1989, Biotechnology 7: 934-938; Reichmann et al., 1988, Nature 332: 323-327; Roberts et al., 1987, Nature 328: 731734; Verhoeyen et al., 1988, Science 239: 1534-1536; Chaudhary et al., 1989, Nature 339: 394-397, each of which is incorporated herein by reference). Recombinant cells that produce fully human antibodies (such as those prepared using transgenic animals, and optionally further modified in vitro), as well as humanized antibodies can also be used in the invention. The term humanized antibody also encompasses single chain antibodies. See, for example, Cabilly et al., US Patent No. 4,816,567; Cabilly et al., European Patent No. 0.125,023 B1; Boss et al., US Patent No. 4,816,397; Boss et al., European Patent No. 0.120,694 B1¡ Neuberger, MS et al.,
International Patent Publication WO 86 / 0.1533; Neuberger, MS et al., European Patent No. 0.194,276 B1; Winter, Patent ϊ Μ P1
MBXICANu INSTITUTE
OF THE PROFIEDAL '
North American No. 5,225,539; Winter, Paterif® '<sup>!</sup>'<sup>T</sup>'EurCl> S & ^ * No.
0.239,400 Β1; Queen et al., European Patent Nu. 0 451 216 D1¡ and
Padlan, EA et al., Patent EP 0 519 596 A1, each of which is incorporated herein by reference. For example, the invention can be used in the production of human and / or humanized antibodies that (
immunospecifically recognize specific cell targets, for example any of the aforementioned proteins, the human EGF receptor, the antigen
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Prostate Specific (AMEP), CD5, CD11a, CD18,
NGF, CD20,
CD45, CD52, Ep-cam, other cell surface cancer molecules, TNF-alpha, TGF-b1, vascular endothelial growth factor (FCEV), other cytokines, alpha 4 beta 7 integrin, IgEs, viral proteins (eg cytomegalovirus) . Examples of antibodies that can be produced using the compositions and methods of the invention include, but are not limited to, anti-TNFa antibody, anti-IL-12 antibody, anti-IL-18 antibody, and antibody against EPO receptor. (EPO-R). In one embodiment, the antiTNFa antibody is a fully human anti-TNFa antibody, for example adalimumab / D2E7 (see US Patent
No.
6,090,382, incorporated herein by reference; Humira®;
Abbott Laboratories). In one embodiment, the anti-IL-12 antibody is a fully human anti-IL-12 antibody, for example ABT874 (Abbott Laboratories; see US Patent No.
6,914,128, incorporated herein by reference). In a
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INSTITUTO MÍ XIOw.
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In the embodiment, the anti-IL-18 antibody is a fully human IL-18 antibody (eg ABT-325), eg see also the antibodies described in US Patent No. US20050147610 A1. In one embodiment, the antibody against EPO / R (also referred to as ABT-007), is a fully human antibody, similar to that described in US Patent Publication No. US 20060018902 A1, which is incorporated herein by reference.
Another example of the type of protein that can be produced using the methods and compositions of the invention include fusion proteins. A fusion protein is a protein or domain or a protein (eg, a soluble extracellular domain) fused to a heterologous protein or peptide. Examples of such fusion proteins include proteins expressed in the form of fusion with a portion of an immunoglobulin molecule, proteins expressed as fusion proteins with a zipper portion, and novel polyfunctional proteins, such as a fusion protein of a cytokine and a factor. of growth (ie GM-CSF and IL-3, MGF and IL-3). International Patent Publications WO 93/08207 and WO 96/40918 describe the preparation of various soluble oligomeric forms of a molecule referred to as CD40L, including an immunoglobulin fusion protein and a zipper fusion protein, respectively; the techniques discussed there are applicable to other proteins. Another fusion protein is a recombinant TNFR: Fc, also known as etanercept. The
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MEXICAN INSTITUTE
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INDUSTRIAL etanercept or Enbrel®; Amgen / Wyeth) is a dimer of two molecules of the extracellular portion of the TNF-α receptor p75, each molecule consisting of a 235 amino acid TNFR-derived polypeptide that is fused to a 232 amino acid Fe portion of human lgG1. In fact, any molecule can be expressed as a fusion protein including, but not limited to, the extracellular domain of a cellular receptor molecule, an enzyme, a hormone, a cytokine, a portion of an immunoglobulin molecule, a domain of zipper and an epitope.
III. Cell Culture Media of the Invention
The present invention provides cell culture media for use in mammalian cell cultures for the production or expression of recombinant proteins, eg, antibodies or antigen-binding portions thereof. The various cell culture media described herein can be used separately or together to improve cell culture, including increased protein production and the extension of cell longevity. In a preferred embodiment, the cell culture media of the invention are serum free, which means that the medium does not contain serum (for example, fetal bovine serum (SFB), horse serum, goat serum, or any other serum derived from an animal known to a person skilled in the art).
In a first aspect, the invention provides a mammalian cell culture medium that includes, in whole or in part, a modified basal medium. Basal cellular media
IMPI
<img file="MX353340B_D0084.tif" />
Modified can be derived from standards known in the art. Suitable basal media include but are not limited to Dulbecco's Modified Eagle's Medium (DMEM), DME / F12, Minimum Essential Medium (MEM), Eagle's Basal Medium (MBE), RPMI 1640, F-10, F-12, Minimum Essential Medium a (MEM-a), Glasgow Minimum Essential Medium (MEM-G), PF CHO (see for example CHO protein free medium) (Sigma) or
PF CHO EXCELL ™ 325 Serum Free Medium for protein-free CHO cells (SAFC Biosciences), and Dulcocco's Medium Modified by Iscove. Other examples of basal media that can be used in the invention include BME Basal Media (Gibco-Nitrogen; see also Eagle, H (1965) Proc. Soc. Exp. Biol. Med. 89, 36); Dulbecco's Modified Eagle's Medium (DMEM, powder) (Gibco-lnvitrogen (# 31600); see also Dulbecco and Freeman (1959) Virology 8, 396; Smith et al. (1960) Virology 12, 185. Tissue Culture Standards Commitee, In Vitro 6: 2, 93); CMRL 1066 Medium (Gibco-lnvitrogen (# 11530); see also Parker RC et al (1957) Special Publications, NY Academy of Sciences, 5, 303).
The basal medium can be modified in order to remove certain non-nutritional components found in the standard basal medium, such as various organic and inorganic buffer solutions, surfactants, and sodium chloride. The removal of such components from the basal cell medium allows a higher concentration of the remaining nutritional components, and improves all cell growth and protein expression, as described in
MEXICAN INSTmCT
ΙΑ ΛΟΛΜί.ΧΓ '!? «? ·. · »Ν »ί AL ΣΞ— this. Furthermore, the omitted components can be added back to the cell culture medium containing the modified basal cell medium, in accordance with the requirements of the cell culture conditions. As described below, it has been found that separating certain ingredients from the basal cell medium, i.e. adding modified basal cell medium as an ingredient in a cell culture medium, and subsequently adding the ingredient back to the cell culture medium as a separate ingredient, provides advantageous properties for cell culture growth and protein production.
The modified basal medium of the invention excludes any, if not all, of the following ingredients: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide. These ingredients are commonly found in commercially available basal cell media.
The exclusion of components, for example, sodium bicarbonate, a buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and / or glucose monosaccharide, can be performed by commercial services, for example SAFO Pharma ™. A person skilled in the art will appreciate that the modified basal media can be obtained, in one embodiment, using a commercial cell culture media service, that is, a custom prepared culture media service. Examples of custom-made culture media services are provided by companies such as SAFO (viz. JRH Bioscience), Invitrogen®, Atlanta
Biologicals®, and Lonza.
<img file="MX353340B_D0085.tif" />
Alternatively, one skilled in the art can prepare the modified basal cell medium of the invention in accordance with standard methods, to prepare basal cell media, where the specific ingredients described herein are omitted (see eg Freshney (2005) Culture of Animal Cells: A Manual of Basic Technique; BD Bionutrients Technical Manual, (2006), Third Edition; Jenkins, ed. (1999), Animal Cell Biotechnology, Methods and Protocols, Humana Press; Doyle and Griffiths, eds., (1997) Essential Techniques: Mammalian Cell Culture, John Wiley and Sons; Butler, ed. (1991) Mammalian Cell Biotechnology: A Practical Approach Oxford University Press; Darling and Morgan (1994) Animal Cells: Culture and Media, John Wiley and Sons; Freshney, ed. (1992), Animal Cell Culture: A Practical Approach (2nd ed), Oxford University Press; Pollard and Walker (1997), Basic Cell Culture Protocols (2nd Ed), Humana Press, (Part of Methods in the Molecular Biology series, Volume 75), each of which is incorporated herein by reference).
In one embodiment, the cell culture medium of the invention contains a modified basal cell medium, a source of iron (preferably inorganic, eg, ferric citrate), a recombinant growth factor; a regulatory solution; a source of surfactant; an energy; and at least two
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MEXICAN INSTITUTE OF PROPERTY, osmolarity regulator;<sup>NI, L</sup>a<sup>L</sup> Different hydrolyzes two ττβ'ΒΌΠ of üTtggTT · animal. Furthermore, the modified basal cell medium may optionally contain amino acids, vitamins, or a combination of both amino acids and vitamins.
As used herein, the term iron means a non-animal source of iron used to supplement the medium. The iron source in the cell culture medium is preferably inorganic. The preferred iron source is inorganic, and includes, for example, ferric salts and ferrous salts, such as ferric citrate or ferrous sulfate. Chelated salts such as ferric citrate and ferric ammonium citrate are preferred. However, other sources of iron may be used that are not isolated from an animal source, for example chemical iron chelators or iron carriers of recombinant protein that provide equivalent amounts of iron. Iron chelating components that can be used include, but are not limited to, iron chelates of ethylenediaminetetraacetic acid (AEDT), ethylene glycol-bis (betaaminoethyl ether) -N, N, N ', N'-tetraacetic acid (EGTA) , desferoxamine mesylate, dimercaptopropanol, diethylene triamine pentaacetic acid (ADPA) and trans-1,2-diaminocyclohexan-N, N, Ν ', N'-tetraacetic acid (CDTA), as well as a ferric citrate chelate and a ferrous sulfate chelate . A particularly preferred source of iron is ferric citrate, which is preferably present in the final volume of the
<img file="MX353340B_D0086.tif" />
IMPI
MiXtCANO INSTITUTE
OF THE RRORfEBAD
INDUSTRIAL cell culture medium at a concentration of 0.1-1 mM. In one embodiment, the concentration of ferric citrate is approximately 0.5 mM. In another embodiment, the concentration of ferric citrate is 100-150 mg / L, for example, 122 mg / L. Intermediate numbers of the above mentioned mM concentrations, for example 0.1, 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, and 1.0 mM, and mg / L, for example, 100, 110, 120, 130, 140, and 150, are also intended to form part of the present invention.
Non-limiting examples of growth factors that can be included in the cell culture medium are insulin or a recombinant analog thereof, IGF-1, and a combination of insulin and IGF-1. A particularly preferred recombinant growth factor is insulin, or a recombinant analog thereof, which is preferably present in the final volume of the cell culture medium in a concentration of between about 4 mg / L to 13 mg / L. Intermediate numbers of the aforementioned concentrations of insulin are also intended to form part of the invention, eg 4, 4.5, 5, 5.5, 6, 6.5, 7, 7.5, 8, 8.5, 9, 9.5, 10, 10.5 , 11, 11.5, 12, 12.5, and 13.
The cell culture medium can also include a buffer solution. In a preferred embodiment, a regulatory solution is excluded from the modified basal cell medium, but added as a separate component to the cell culture medium (to which the modified basal cell medium is also added). Regulatory solutions for use in the culture medium
<img file="MX353340B_D0087.tif" />
Cellular IMPIS are known in the art.
e regulatory solutions that may include § ^ ftiufil ~ 4nWKe-tte ^ nrtttVTr cellular are phosphate buffer, HEPES, and sodium bicarbonate. In one embodiment, sodium bicarbonate is added as a buffer solution to the cell culture medium at a final concentration of approximately 0.1-3 g / L. In one embodiment, sodium bicarbonate is added as a buffer solution to the cell culture medium at a final concentration of approximately 1.6 g / L. In one embodiment, HEPES is added as a buffer solution to the cell culture medium at a final concentration of approximately 0.1-3 g / L. In another embodiment, HEPES is added as a buffer solution to the cell culture medium at a final concentration of 1.8 g / L. In one embodiment, a phosphate buffer solution, for example, monobasic and dibasic sodium phosphate, is added to the cell culture medium at a final concentration of between 0.01 and 0.5 g / L. Intermediate numbers of the aforementioned concentrations are also intended to form part of the invention, for example, sodium bicarbonate or HEPES concentration of 0.1, 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1.0, 1.1 , 1.2, 1.3, 1.4, 1.5, 1.6, 1.7, 1.8, 1.9, 2.0, 2.1, 2.2, 2.3, 2.4, 2.5, 2.6, 2.7, 2.8, 2.9, and 3.0 or the phosphate buffer solution concentration of 0.01, 0.02, 0.03, 0.04, 0.05, 0.06, 0.07, 0.08, 0.09, 0.1, 0.12, 0.14, 0.16, 0.18, 0.2, 0.22, 0.24,
0.26, 0.28, 0.3, 0.32, 0.34, 0.36, 0.38, 0.4, 0.42, 0.44, 0.46, 0.48, and
0.5 g / L.
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<img file="MX353340B_D0088.tif" />
The buffer is included to help maintain the cell culture medium at a desired pH. In one embodiment, the pH of the cell culture medium ranges from 6.0 to 8.0; 6.5 to 7.5; or 7.1 a
7.2. Intermediate numbers of these pH values, for example 6.1,
6.2, 6.3, 6.4, 6.5, 6.6, 6.7, 6.8, 6.9, 7.0, 7.1, 7.2, 7.3, 7.4, 7.5, 7.6,
7.7, 7.8, 7.9, and 8.0, as well as other numbers mentioned herein, are also intended to form part of the present invention. The ranges of values, using a combination of any of the values mentioned above as upper and / or lower limits, are intended to be included within the scope of the invention.
The cell culture medium can also include an osmolarity regulator, such as NaCI. In one embodiment, NaCI is added to the cell culture medium at a final concentration of between about 1.0 to 6.5 g / L. In one embodiment, the osmolarity of the cell culture medium ranges from 260 to 450 mOsm / kg. In one embodiment, the osmolarity of the cell culture medium ranges from 320 to 450 mOsm / kg. Intermediate numbers to the mentioned NaCI concentrations and mOsm / kg values, for example NaCI concentration of 1, 1.5, 2, 2.5, 3, 3.5, 4, 4.5, 5, 5.5, 6, and 6.5 or a range of mOsm / kg of 260, 270, 280, 290, 300, 310, 320, 330, 340, 350, 360, 370, 380, 390, 400, 410, 420, 430, 440, 450, as well as intermediate numbers thereof , are also intended to form part of the present invention. The ranges of values, using a combination of any of the values s mentioned above as upper limits and / or are included in the scope of the invention.
An energy source, also of cell culture, of the invention. Of
<img file="MX353340B_D0089.tif" />
can be added to the medium preference, the energy source is a monosaccharide. Examples of monosaccharides that can be used in the cell culture medium include glucose (eg, D-glucose), maltose, trickle, galactose and fructose. In one embodiment, glucose is added to the cell culture medium at a final concentration that varies in the range of 3.5 - 7.0 g / L. In one embodiment, glucose is added to the cell culture medium at a final concentration of not more than 7.0 g / L. In one embodiment, glucose is added to the cell culture medium at a final concentration of approximately 7.0 g / L. Intermediate numbers at the glucose concentrations mentioned, for example 3.5, 3.6, 3.7,
3.8, 3.9, 4, 4.2, 4.4, 4.6, 4.8, 5, 5.2, 5.4, 5.6, 5.8, 6, 6.2, 6.4, 6.6,
6.8, and 7, as well as intermediate numbers thereof, are also intended to form part of the present invention. The ranges of values, using a combination of any of the aforementioned values as upper and / or lower limits, are also intended to be included within the scope of the invention.
An important ingredient in the cell culture medium of the invention is the addition of a hydrolyzate. The cell culture medium of the invention may include a hydrolyzate derived from a single source, for example yeast or soy, or may include a combination of hydrolyzates, for example hydrolyzates based on
IΜ PI
MEXICAN INSTITUTE οε u tnoustaiai property.
yeast and soy. Preferably, the hydrolyzates used in the cell culture media of the invention are not of animal origin.
Examples of hydrolyzates that are not of animal origin include plant-based hydrolyzates and non-plant-based hydrolyzates, eg, yeast-based hydrolyzates, tryptone, casein hydrolyzate, yeast extract, or papain-digested soybean peptone. Hydrolyzates used in the media of the invention are commercially available, including, for example, HyPep 1510.RTM, Hy-Soy.RTM., Hy-Yeast 412.RTM and H¡Yeast 444.RTM., From sources such as Quest International, Norwich,
NY, OrganoTechnie, SA France, Deutsche Hefewerke GmbH, Germany, or DMV Intl. Delhi, NY Sources of yeast extracts and soy hydrolyzates are also described in International Patent Publications WO 98/15614, WO 00/03000, WO 01/23527 and in US Patent No. 5,741,705. Examples of a yeast based hydrolyzate which can also be used in the invention include TC Yeastolate (BD Diagnostic) and Yeastolate UF (SAFC Biosciences), while examples of plant based hydrolyzates include Soy Hydrolysate UF (SAFC Biosciences) and HyQ ® I am Hydrolysate (HyClone Media).
In one embodiment, the cell culture medium of the invention further includes glutamine, eg, L-glutamine. Suitable sources of L-glutamine are commercially available from various sources, such as Gibco (Cat. No. 25030-081).
<img file="MX353340B_D0090.tif" />
IMPI
INSTITUTO MEXICANO DE LA FRUPIEDAD INDUSTRIAL Optionally, the cell culture medium including those described below in the Examples Section may include methotrexate.
Examples of amounts of methotrexate used in cell culture media to grow CHO cells, include approximately 100 nM to 5000 nM of methotrexate.
Intermediate methotrexate molar numbers, for example, 100, 200, 300, 400, 500, 600, 700, 800, 900, 1000, 1200, 1400, 1600, 1800, 2000, 2200, 2400, 2600, 2800, 3000, 3200, 3400, 3600, 3800, 4000, 4200, 4400, 4600, 4800, and 5000 nM, as well as intermediate numbers thereof, are also intended to form part of the present invention. The ranges of values, using a combination of any of the aforementioned values as upper and / or lower limits, are also intended to be included within the scope of the invention.
In large-scale bioreactors, CHO cells are particularly susceptible to shear forces arising from bubbling of gases in the container and mixing with the paddle. Therefore, the cell culture media of the invention may also optionally include a cell protector. The term cell protector as used herein means a substance that protects eukaryotic cells from damage. Such damage can be caused, for example, by tensile forces or the effects of gas bubbling in a bioreactor. To minimize the presence of cellular damage, it is advantageous for the medium to have a cellular protector, such as methyl cellulose, polyethylene glycol, polyvinyl alcohols, or
<img file="MX353340B_D0091.tif" />
<img file="MX353340B_D0092.tif" />
Pluronic polyols. Of these, pcHTUl Γ0Ρ Pliirn »¡c RTM is preferred. (polyol, BASF Wyandotte Corp.), since unlike polyvinyl alcohols this is a non-toxic substance and unlike polyethylene glycols, it does not interfere with downstream purification.
The cell culture medium of the invention can also include non-ferrous metal ions. Examples of non-ferrous metal ions include, but are not limited to, chloride and sulfate, potassium, magnesium, cupric, selenium, zinc, nickel, manganese, tin, cadmium, molybdate, vanadate, and silicate salts.
The cell culture medium of the invention can also include vitamins and enzyme cofactors. Examples of such vitamins and enzyme cofactors include, but are not limited to, PABA (p-aminobenzoic acid), Vitamin K (Biotin), Vitamin B5 (Calcium DPanthenate), folic acid, l-lnositol, Niacinamide (Nicotinic acid amide ), Vitamin B6 (Pyridoxine Hydrochloride) and (Pyrodoxal Hydrochloride), Vitamin B2 (Riboflavin), Vitamin B1 (Thiamine), and Vitamin B12 (Cyanocobalamin). Alternatively, vitamin C (L-ascorbic acid) can be added to the media. Choline chloride can also be added, which is generally considered a vitamin, but it can also be considered as a lipid factor.
Additionally, the cell culture medium of the invention may also include lipid-like factors. Examples of lipid factors include choline chloride and phosphatidylcholine. An auxiliary may also be included in lipid production, for
<img file="MX353340B_D0093.tif" />
<img file="MX353340B_D0094.tif" />
For example, an ethanolamine-like alcoholamine.
In the methods and compositions of the invention, the cells are preferably grown in serum-free media. The term serum-free, as applied to the media, includes any serum-free mammalian cell culture medium, such as fetal bovine serum.
Also included within the scope of the invention are mammalian cells, for example CHO cells, in any of the improved cell culture media described herein.
In one aspect of the invention, formulations for cell culture media optimized for the production of a certain antibody are provided. Examples of optimized formulations include cell culture media for the growth or protein production of CHO cells expressing an anti-TNFa antibody, an anti-IL-12 antibody, an anti-IL-18 antibody, and an antibody against the EPO receptor. (EPO-R).
Included in the invention are cell culture media for mammalian cells, for example CHO cells expressing anti-TNFa antibodies, including fully human antiTNFa antibodies. In a preferred embodiment, the fully human anti-TNFa antibody is adalimumab (also referred to as D2E7 and Humira®: Abbott Laboratories). The characteristics of adalimumab, including nucleic acid and amino acid sequences, are described in the Patent
<img file="MX353340B_D0095.tif" />
IMPI
North American No. 6,090,382, which is incorporated herein by reference. Adalimumab can be produced by culturing mammalian cells, eg, CHO cells comprising a nucleic acid encoding the protein, eg, adalimumab, in a cell culture growth medium, transferring the cell culture to the culture production medium. cell and isolating the protein from the cell culture production medium.
In one embodiment, the invention provides a cell culture growth medium optimized for CHO cells, comprising a nucleic acid encoding adalimumab. The serum-free cell culture growth medium formulation optimized for CHO cells expressing adalimumab includes a basal medium; ferric citrate (for example, about 8-12 mL / kg, about 10.0 mL / kg or 122 mg / L); recombinant human insulin (eg, about 2-6 mg / kg or 4.0 mg / kg); anhydrous glucose (eg 2-5 g / kg, approximately 3.5 g / kg); L-glutamine (eg, about 0.29 g / kg); sodium bicarbonate (for example, about 1.6 g / kg); NaH<sub>2</sub>PO<sub>4</sub>* H<sub>2</sub>Or (for example, about 0.03 g / kg); Na<sub>2</sub>HPO<sub>4</sub>»7H<sub>2</sub>Or (for example, about 0.43 to 0.44 g / kg); and yeast-based hydrolyzate (eg, about 2.0 g / kg). Another example of a serum free cell culture growth medium optimized for CHO cells expressing adalimumab, includes the following ingredients: a modified basal medium that excludes the following
<img file="MX353340B_D0096.tif" />
IMPI
MEXICAN INSTITUTE
OF THE PROPERTY
INDUSTRIAL components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; ferric citrate (for example, about 10.0 mL / kg or 122.45 mg / kg); recombinant human insulin (eg, about 3.8 to 3.9 mL / kg or 7.8 mg / kg); anhydrous glucose (eg, about 7.0 g / kg); L-glutamine (eg, about 0.8 to 0.9 g / kg); sodium bicarbonate (for example, about 1.6 g / kg); HEPES (eg about 1.8 g / kg); NaCI (eg, about 2.6 to 2.7 g / kg); Pluronic F-68 (eg, about 1.0 g / kg); NaH<sub>2</sub>PO<sub>4</sub>«H<sub>2</sub>Or (for example, about 0.03 to 0.04 g / kg); Na<sub>2</sub>HPO<sub>4</sub>"7H<sub>2</sub>Or (for example, about 0.43 to 0.44 g / kg); Lasparagine monohydrate (eg, about 0.45 g / kg); yeast-based hydrolyzate (eg, about 4.0 g / kg); and plant-based hydrolyzate (eg, about 2.6 g / kg). The cell culture growth medium for expressing adalimumab may further include methotrexate, for example about 1-5 mL / kg or about 2.50 mL / kg.
In one embodiment, the invention provides an optimized cell culture production medium for CHO cells expressing an antibody including, for example, an anti-human TNFa antibody (eg, adalimumab) or an erythropoietin receptor antibody (EPO-R). Examples of antibodies against
<img file="MX353340B_D0097.tif" />
EPO / R are described in US Patent No. 20040071694, which is incorporated herein by reference. The serum-free cell culture production medium formulation optimized for CHO cells expressing antibody, such as adalimumab or an antibody against EPO / R, includes a modified basal medium that excludes the following components: sodium bicarbonate, buffer, phosphate monobasic sodium, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; ferric citrate (for example, about 10.0 mL / kg or 122.45 mg / L); recombinant human insulin (eg, about 6.0 mL / kg or 12 mg / kg); anhydrous glucose (eg, about 7.0 g / kg); L-glutamine (for example, about 0.58 to 0.59 g / kg); sodium bicarbonate (for example, about 1.6 g / kg); HEPES (eg, about 1.8 g / kg); NaCI (eg, about 2.4 to 2.5 g / kg); Pluronic F-68 (eg, about 1.0 g / kg); NaH<sub>2</sub>PO4 * H<sub>2</sub>Or (for example, about 0.03 to 0.04 g / kg); Na<sub>2</sub>HPO4 »7H<sub>2</sub>Or (for example, about 0.43 to 0.44 g / kg); a yeast-based hydrolyzate (eg, about 10.7 g / kg); and plant-based hydrolyzate (eg, about 6.9 to 7.0 g / kg). In one embodiment, the cell culture production medium has a pH in the range of about 7.1 to 7.2 and an osmolarity in the range of 373 to 403 mOsm / kg. Intermediate numbers of the above values, for example, the mentioned insulin, pH, or osmolarity values,
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MLXICANe K <INSTITUTE<sup>day3</sup>Kí5 * '<^
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INDUSTRIAL is also intended to form part of the present invention.
Another aspect of the invention relates to cell culture media that are optimized by the production of anti-interleukin-12 (IL-12) antibodies, eg, fully human IL-12 antibodies, produced by CHO cells. In a preferred embodiment, the fully human anti-IL-12 antibody is ABT-874. The characteristics of ABT-874, including nucleic acid and amino acid sequences, are described in US Patent No. 6,914,128, incorporated herein by reference.
In one embodiment, a serum-free cell culture growth medium optimized for the growth of CHO cells expressing ABT-874, includes the following: a modified basal medium, which excludes the following components: sodium bicarbonate, buffer, phosphate monobasic sodium, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; ferric citrate (for example, about 10 mL / kg or 122.45 mg / L); recombinant human insulin (eg, about 3.8 to 3.9 mL / kg or 7.8 mg / kg); anhydrous glucose (eg, about 7.0 g / kg); Lglutamine (eg, about 0.87 to 0.88 g / kg); Lasparagine monohydrate (eg, about 0.45 g / kg); sodium bicarbonate (for example, about 1.6 g / kg); HEPES (eg, about 1.8 g / kg); NaCI (eg, about 2.67 to 2.68 g / kg); Pluronic F-68 (for example,
IMPI ^
MEXICAN INSTITUTE
OF INDUSTRIAL RRORltDA ----- approximately 1.0 g / kg); NaH<sub>2</sub>PO<sub>4</sub>«H<sub>2</sub>Or (for example, about 0.03 to 0.04 g / kg); Na<sub>2</sub>HPO<sub>4</sub>»7H<sub>2</sub>Or (for example, about 0.43 to 0.44 g / kg); yeast-based hydrolyzate (eg, about 4.0 g / kg); and plant-based hydrolyzate (eg, about 2.6 g / kg).
In one embodiment, a serum-free cell culture production medium for the expression of ABT-874 includes the following: a modified basal medium that has a reduced vitamin content and excludes the following components: sodium bicarbonate, buffer solution , monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; ferric citrate (eg, approximately 10 mL / kg or 122.45 mg / L); recombinant human insulin (eg, approximately 6.5 mL / kg or 13 mg / kg); anhydrous glucose (eg, about 7.0 g / kg); L-glutamine (for example, about 0.58 to 0.59 g / kg); baking soda (eg, about 1.6 g / kg); HEPES (eg, approximately 1.8 g / kg); NaCI (eg, approximately 2.45 g / kg); Pluronic F-68 (eg, about 1.0 g / kg); NaH<sub>2</sub>PO<sub>4</sub>«H<sub>2</sub>Or (for example, about 0.03 to 0.04 g / kg); Na<sub>2</sub>HPO<sub>4</sub>»7H<sub>2</sub>Or (for example, about 0.43 to 0.44 g / kg); yeast-based hydrolyzate (eg, about 10.7 g / kg); and a plant-based hydrolyzate (eg, about 6.9 to 7.0 g / kg).
In one embodiment, the invention provides serum-free cell culture growth medium for CHO cells that
<img file="MX353340B_D0098.tif" />
IMPI (Mexican NsrmrTO <sup>z</sup> from the FXOrlEUAD
INDUSTRIAL express antibodies, for example, anti-ll 1_2 antibodies - antibodies against EPO / R, comprising the following:
a basal medium; ferric citrate (for example, about 10 mL / kg or
122.45 mg / L);
recombinant human insulin (eg, approximately mg / kg); anhydrous glucose (for example, about
1.5 g / kg);
L-glutamine (eg, about 0.29 to 0.30 g / kg); sodium bicarbonate ((eg, about 1.6 g / kg); and yeast-based hydrolyzate (eg, at least about 2 g / kg). In one embodiment, the cell culture growth medium for CHO cells expressing antibodies eg, anti-IL12 antibodies and antibody against EPO / R, has a pH of about 7.10 to 7.30 and an osmolarity of about 300 to 340 mOsm / kg. The cell culture medium can also contain a yeast-based hydrolyzate (eg, at least about 8 g / kg).
Another aspect of the invention relates to cell culture media optimized for the production of anti-interleukin-18 (IL-18) antibodies, eg, fully human IL-18 antibodies, produced by CHO cells. Examples of fully human IL18 antibodies that can be produced using the methods and compositions of the invention are described in PCT Publication WO 01/058956, incorporated herein by reference.
In one embodiment, a cell culture growth medium optimized for the production of the IL-18 antibody in cells
CHO, includes the following
<img file="MX353340B_D0099.tif" />
INSTITUTO MEXICANO DE LA RUOTISPAO INDUSTRIAL____ ingredients: a modified basal medium that excludes the following components: sodium bicarbonate;
buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and mL / kg monosaccharide or glucose; ferric citrate (for example, about
122.45 mg / L); recombinant human insulin (eg, about 3.8 to 3.9 mL / kg or 7.8 mg / kg); anhydrous glucose (eg, about 7.0 g / kg); L-glutamine (for example, about 0.87 to 0.88 g / kg); L-asparagine monohydrate (eg, about 0.45 g / kg);
sodium bicarbonate (for example, about 1.6 g / kg);
HEPES (eg, about 1.8 g / kg); NaCI (eg, about 2.67 g / kg); Pluronic F-68 (eg, about 1.0 g / kg); NaH<sub>2</sub>PO<sub>4</sub>* H<sub>2</sub>Or (for example, about 0.03 to 0.04 g / kg); Na<sub>2</sub>HPO<sub>4</sub>»7H<sub>2</sub>Or (for example, about 0.43 to 0.44 g / kg); yeast-based hydrolyzate (eg, about 4.0 g / kg); and a plant-based hydrolyzate (eg, about 2.6 g / kg). The cell culture medium for the growth of cells expressing fully human IL-18 antibodies can have a pH of 7.10 to 7.20 and an osmolarity of 373 to 403 mOsm / kg. Intermediate numbers of the above values, eg, insulin, pH, or osmolarity values quoted, are also intended to form part of the present invention.
An example of a cell culture production medium
<img file="MX353340B_D0100.tif" />
IMPI optimized for IL-18 antibody production in ^ m-in._ cell includes the following ingredients: a modified basal medium, which is modified to remove the following components: sodium bicarbonate, HEPES buffer, monobasic sodium phosphate , dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose monosaccharide; ferric citrate (for example, about 10 mL / kg or 122.45 mg / L); recombinant human insulin (eg, about 6.0 mL / kg or 12 mg / kg); anhydrous glucose (eg, about 7.0 g / kg); Lglutamine (for example, about 0.58 to 0.59 g / kg); sodium bicarbonate (for example, about 1.6 g / kg);
HEPES (eg, about 1.8 g / kg); NaCI (eg, about 2.45 g / kg); Pluronic F-68 (eg, about 1.0 g / kg); NaH<sub>2</sub>PO<sub>4</sub>* H<sub>2</sub>Or (for example, about 0.03 to 0.04 g / kg); Na<sub>2</sub>HPO<sub>4</sub>"7H<sub>2</sub>Or (for example, about 0.43 to 0.44 g / kg); yeast-based hydrolyzate (eg, about 10.7 g / kg); and a plant-based hydrolyzate (eg, about 6.9 to 7.0 g / kg). Another example of a cell culture production medium to produce fully human anti-IL-18 antibodies, includes a modified basal medium, which excludes the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate , an osmolarity regulator, a surfactant, and glucose monosaccharide; ferric citrate (for example, about 10 mL / kg or 122.45 mg / L); insulin
IMPI
<img file="MX353340B_D0101.tif" />
recombinant human (eg, at about 6 5 ml / kg-to-13 mg / kg); anhydrous glucose (eg, about 7.0 g / kg); L-glutamine (for example, about 0.58 to 0.59 g / kg); sodium bicarbonate (for example, about 1.6 g / kg); HEPES (eg, about 1.8 g / kg); NaCI (eg, about 2.45 g / kg); Pluronic F-68 (eg, about 1.0 g / kg); NaH<sub>2</sub>PO<sub>4</sub>* H<sub>2</sub>Or (for example, about 0.03 to 0.04 g / kg); Na<sub>2</sub>HPO<sub>4</sub>"7H<sub>2</sub>Or (for example, about 0.43 to 0.44 g / kg); yeast-based hydrolyzate (eg, about 14.2 to 14.3 g / kg); and a plant-based hydrolyzate (eg, about 9.2 to 9.3 g / kg). Cell culture medium for CHO cells that produce fully human IL-18 antibodies can have a pH of 7.10 to 7.20 and an osmolarity of 373 to 403 mOsm / kg. Intermediate numbers of the above values, eg, insulin, pH or osmolarity values quoted, are also intended to form part of the present invention.
Other examples of media within the scope of the invention are described below in relation to batch feeding methods and supplemental media that enhance antibody production, in addition to the example media in the Examples section.
The media of the present invention can be used to perform appropriate cell cultures by bringing the media or its components into contact with all or part of the cell population.
<img file="MX353340B_D0102.tif" />
The media can be contacted with the cells by mixing, adding, combining, seeding, or shaking one or more cells with one or more compounds, solutions, media, and so on. The media can also be contacted with all cells at once, gradually or step by step, for example by feeding, to replace or supplement the medium in which the cells are grown, as described in greater detail below. .
IV. Methods and compositions for improved protein production
The methods of the compositions of the invention relate to mammalian cell cultures. In one embodiment, the mammalian cell used is the CHO cell.
Established methods for introducing DNA into mammalian cells have been described. Kaufman, RJ, Large Scale Mammalian Cell Culture, 1990, pp. 15-69. Additional protocols can be used using commercially available reagents, such as the Lipofectamine ™, lipofectamine ™ -2000, or Lipofectamine ™ -plus cationic lipid reagents (which
Invitrogen), to transfect cells.
Nati. Acad. Sci. USA 84: 7413-7417.
can be purchased from
Feigner et al. (1987), Proc.
Furthermore, electroporation or bombardment with nucleic acid coated microprojectiles can be used to transfect mammalian cells, using procedures such as those described in Sambrook et al.,
Molecular Cloning: A Laboratory Manual, 2a. Ed. Vol. 1-3, Coid
MEXICAN INSTITUTE
OE LA ÍHOWEBao
<img file="MX353340B_D0103.tif" />
Spring Harbor Laboratory Press (1989) and Fitzpatrick-McElligotí<sup></sup>(1992), Biotechnology (NY) 10 (9): 1036-40. The selection of stable transformants can be carried out using methods known in the art, such as for example resistance to cytotoxic drugs. Kaufman et al. ((1990), Meth. In Enzymology 185: 487-511), describes various selection schemes, such as resistance to dihydrofolate reductase (DHFR). A suitable host strain for DHFR selection may be the DX-B11 strain of CHO cells, which is deficient in DHFR. Urlaub and Chasin (1980), Proc. Nati. Acad. Sci. USA 77: 4216-4220. A plasmid expressing the DHFR cDNA can be introduced into the DXB11 strain, and only cells containing the plasmid can grow on the appropriate selective media. Other examples of selection markers that can be incorporated into an expression vector include cDNAs that confer resistance to antibiotics, such as G418 and hygromycin B. Cells that host the vector can be selected based on resistance to these compounds.
Additional control sequences shown to enhance the expression of heterologous mammalian expression vector genes include such elements as the expression enhancing sequence elements (ESAE) derived from CHO cells (Morris et al., In Animal Cell Technology, pp. 529-534 (1997); North American Patents Nos. 6,312,951 B1, 6,027,915, and 6,309,841 B1) and the tripartite leader sequence (LTP) and RNAs of the VA gene of adenovirus 2 (Gingeras et al. (1982), J. Bioj Chem. 257: 1347513491). Virally derived internal ribosome entry site (SERI) sequences allow dicistronic mRNAs to be translated efficiently (Oh and Sarnow (1993), Current Opinion in
<img file="MX353340B_D0104.tif" />
Genetics and Development 3: 295-300; Ramesh et al. (1996), Nucleic
Acids Research 24: 2697-2700). Expression of a heterologous cDNA as part of a dicistronic mRNA followed by the gene for a selectable marker (eg DHFR), has been shown to improve host transfectability and expression of the heterologous cDNA (Kaufman et al. (1990), Methods in Enzymol. 185: 487-511). Example expression vectors employing dicistronic mRNAs are pTR-DC / GFP described by Mosser et al., Biotechniques 22: 150-161 (1997), and p2A5l described by Morris et al., In Animal Cell Technology, pp. 529-534 (1997).
A highly useful expression vector, pCAVNOT, has been described by Mosley et al. ((1989), Cell 59: 335-348). Other expression vectors for use in mammalian host cells can be constructed as described by Okayama and Berg ((1983), Mol. Cell. Biol. 3: 280). A useful system for the expression at a highly stable level of mammalian cDNAs in C127 murine mammalian epithelial cells, can be constructed substantially as described by Cosman et al. ((1986), Mol. Immunol. 23: 935). A highly useful expression vector, PMLSV N1 / N4, described by Cosman et al. ((1984), Nature 312: 768), has been deposited with ATCC 39890. Expression vectors of
IMPI
<img file="MX353340B_D0105.tif" />
Additional useful mammals are described in European Patent EP
No. -A-0 367 566 and in the International Patent Publication WO
01/27299 A1. Vectors can be derived from retroviruses. In place of the native signal sequence, a heterologous signal sequence may be added, such as one of the following sequences: the signal sequence for IL-7 described in US Patent No. 4,965,195; the signal sequence for the IL-2 receptor described in Cosman et al. (Nature 312: 768 (1984));
the IL-4 signal peptide described in European Patent EP No. 0
367 566; the IL-1 receptor signal peptide described in US Patent No. 4,968,607; and the type II IL-1 receptor signal peptide described in European Patent EP No. 0 460 846.
The polypeptides can be produced recombinantly in eukaryotic cells, and are preferably secreted by host cells adapted to grow in cell culture. Host cells for use in the invention are preferably mammalian cells. Cells can also be engineered to express a gene of interest, which can be the production of mammalian cells adapted to grow in cell culture, and / or can be homogeneous cell lines. Examples of such cells commonly used in industry are VERO, BHK, HeLa, CV1 (including
Cos), MDCK, 293, 3T3, myeloma cell lines (eg.
NSO, NS1), PC12, WI38 cells, and Hamster Ovary cells
<img file="MX353340B_D0106.tif" />
Jp 1 NfflTUTOM ERICA Nv Λ}
Chinese (CHO), which are widely <sup>D</sup>u ¥ W «? & Sas ^^ aiáí ^ ía production of various re-combining polypeptides®.-complexes., __ for example, cytokines, coagulation factors and antibodies (Brasel et al. (1996), Blood 88: 2004-2012; Kaufman et al. (1988), J. Biol. Chem. 263: 6352-6362; McKinnon et al. (1991), J Mol Endocrinol 6: 231-239; Wood et al. (1990), J. Immunol. 145: 3011-3016). Dihydrofolate reductase (DHFR) deficient mutant cell lines (Urlaub et al. (1980), Proc Nati Acad Sci USA 77: 4216-4220 (which is incorporated by reference), DXB11 and DG-44, are desirably host CHO cell lines, due to efficient selectable DHFR and amplifiable gene expression system allowing a high level of recombinant polypeptide expression in these cells (Kaufman RJ (1990), Meth Enzymol 185: 537-566, which is incorporated by reference). Furthermore, these cells are easy to manipulate as adherent cultures or suspension cultures, and exhibit relatively good genetic stability. CHO cells and the recombinant polypeptides expressed in them have been extensively characterized and have been approved for use in commercial clinical manufacturing by regulatory agencies. The methods of the invention can also be practiced using hybridoma cell lines that produce an antibody. Methods for preparing hybridoma lines are well known in the art. See See eg Berzofsky et al. in Paul, ed., Fundamental Immunology, Second Edition, pp. 315-356, at 347-350, Raven Press Ltd., New York (1989). Cell lines derived from lines
<img file="MX353340B_D0107.tif" />
100
IMPI fNSTnVTU MEXICANO DE LA PROREDAD INDUSTRIAL mentioned above are also suitable for practicing the invention.
After transformation of a suitable mammalian host cell, for example the CHO cell, with polynucleotide sequences encoding a recombinant protein, cells that demonstrate stable expression of the recombinant protein are identified and isolated. Stable expression of a recombinant protein is achieved by transfection of appropriate DNA vectors into dihydrofolate reductase (DHFR) deficient Chinese Hamster Ovary cells (CHO AM-1 / D, US Patent No. 6,210,924), followed by isolation and testing of individual clones demonstrating higher expression of recombinant protein, in accordance with methods known in the art. Based on growth and production in small-scale agitators and larger-scale bioreactors, a specific cell line is chosen as the cell line to manufacture the recombinant protein.
Cells that produce the highest levels of recombinant protein can be cloned by methods well known in the art, by multiple rounds of limiting dilution in 96-well and / or 24-well plates, under serum-free conditions, using culture media. cell phone of the present invention. Clones are selected based on production and growth characteristics in various suspension vessels. Enzyme immunoassays (IEE) can be performed to select the clone that
<img file="MX353340B_D0108.tif" />
<img file="MX353340B_D0109.tif" />
101 produce the highest level of protein rpcnmhinantP j growth characteristics, including double times and densities, can be measured by growing the clones in various shakers or shake flasks and bioreactors in the range of 100 mL to 3 L. An optimal clone is selected, for example a clone with the fastest doubling time that reaches the highest density in culture, and is selected as the cell line for use in the production of recombinant proteins. In one embodiment, the production of recombinant protein is for commercial purposes, and is carried out using a large-scale bioreactor.
Typically, cell culture is carried out under sterile atmospheric and controlled temperature conditions, in tissue culture plates (for example 10 cm plates, 96-well plates, etc.) or other adherent culture (for example on how many microcarriers ) or in suspension cultures, such as in bottles. Cultures can be grown in shake flasks, small-scale bioreactors, and / or large-scale bioreactors. A bioreactor is an apparatus used to grow cells, where environmental conditions such as temperatures, atmosphere, agitation, and / or pH can be monitored, adjusted, and controlled. The methods, including the batch feeding methods and compositions of the invention, can be used in large-scale mammalian cell culture, for example 10L, 11L, 12L, 13L, 14L, etc. In one modality, the cultivation methods
102
IMPI
<img file="MX353340B_D0110.tif" />
Large-scale cell and compositions of the invention are suitable for the cultivation of CHO cells and the production of antibodies.
In accordance with the present invention, a mammalian host cell is cultured under conditions that promote the production of the polypeptide of interest, which may be an antibody or a recombinant polypeptide. Those skilled in the art may choose to use one or more of the cell culture media described herein, which have been developed to maximize cell growth, cell viability, and / or recombinant polypeptide production, in a cultured host cell. particular. Alternatively, the methods and compositions according to the present invention can be used in combination with commercially available cell culture media.
Suitable culture conditions for mammalian cells are known in the art (see for example Animal cell culture: A Practical Approach, D. Rickwood, ed., Oxford University Press, New York (1992)), and can be combined with the improved methods of the invention. Mammalian cells can be grown in suspension or attached to a solid substrate. In addition, mammalian cells can be grown, for example, in fluidized bed bioreactors, hollow fiber bioreactors, spinning bottles, shake flasks, or in shake tank bioreactors, with or without microcarriers, and operated in a manner by
-Μ ·· batches, batch feed,
103 mode
<img file="MX353340B_D0111.tif" />
MEXICAN tNSTnUTD
HE T Λ nONEDAC INDUmiAl continuous,
<img file="MX353340B_D0112.tif" />
semi-continuous or perfusion.
The methods according to the present invention can be used to improve the production of recombinant polypeptides, both in single phase and in multiple phase culture processes. In a single phase process, cells are inoculated in a culture environment, and the methods described are during the single production phase. In a multi-stage process, cells are grown in two or more different stages. For example, cells can be cultured first in a growth phase, under environmental conditions that maximize cell proliferation and viability, then transferred to a production phase, under conditions that maximize polypeptide production. Growth and production phases can be preceded by, or separated by, one or more transition phases. In multiple phase processes, the methods according to the present invention are employed at least during the production phase.
For the purposes of understanding, even without limitation, it should be appreciated by those skilled in the art, that cell cultures and culture processes for protein production can include three general types; namely, continuous culture, batch culture, and batch feed culture. In a continuous culture, for example, a fresh supplement to the culture medium (i.e., a feeding medium) is provided to the cells, during the period
104
IMPIgsi ^ j WnVKIMU »*.
of culture, while a culture medium me'rTal ^ tresCT ^ Ass removed daily and the product is coseEñádfi, poi — exemplary? daily or continuously. In continuous culture, the feeding medium can be added daily or continuously, that is, by drip or infusion. For continuous culture, cells can remain in the culture as long as desired, as long as the cells remain alive and culture and environmental conditions are maintained.
In batch culture, cells are initially grown in the medium, and this medium is either removed, replaced, not supplemented, that is, the cells are not fed with a new medium, during or before the end of the culture process. . The desired product is harvested at the end of the cultivation process.
For batch-fed cultures, the culture process time is increased by supplementing the culture medium one or more times daily (or continuously) with nutrient solutions during the process, that is, the cells are fed with a culture medium. feeding during the cultivation period. Batch feed cultures can include various feeding regimes and times as described below, for example, daily, every third day, every other day, etc., more than once per day or less than once per day. , etc. In addition, batch feed crops can be continuously fed with the feed medium. The desired product is subsequently harvested at the end of the cultivation /
<img file="MX353340B_D0113.tif" />
<sub>105</sub> IMPI mrnTvro méxicanc
Dt LA PRORIÍDAU
INDUSTRIAL production. The present invention preferably encompasses batch feeding cell cultures, where the feeding uses optimized feeding solutions that increase protein production and can extend the protein production phase.
Improved Batch Feed Culture: Hydrolyzate and Basal Enrichment Solutions
One aspect of the invention characterizes methods and compositions for increasing protein production, using an improved batch feeding method in combination with supplemental hydrolyzate and basal solutions. The improved batch feeding method, in part, is based on the addition of two enriched solutions, i.e. a hydrolyzate enrichment solution and a basal enrichment solution, both of which are added to the cell culture medium over a period of time during protein production. The hydrolyzate enrichment solution used in the batch feeding method of the invention comprises a first hydrolyzate that is not derived from a plant or an animal, and a second plant-based hydrolyzate. An example of a hydrolyzate that is not derived from a plant or animal and a plant-based hydrolyzate is a yeast-based hydrolyzate. An example of a plant-based hydrolyzate which can be used in the enriched hydrolyzate solution is a soy-based hydrolyzate. The basal enrichment solution includes a basal medium, eg PF CHO, gg! »
<img file="MX353340B_D0114.tif" />
asparagine and glucose, and the pnrignarim solution<sub>IO</sub>Hydrolyzate nfn includes at least two different hydrolyzates that are not of animal origin. The hydrolyzate and basal enrichment solutions are added to the cell culture at intervals over a period of time, for example at daily intervals over a period of 11 to 15 days, and can be added on the same day or on different days.
The invention features a batch feeding method for producing an anti-TNFa antibody, eg adalimumab / D2E7, which comprises culturing Chinese Hamster Ovary (CHO) cells comprising a nucleic acid encoding the anti-TNFa antibody, in a cell culture at a culture temperature in the range of 32 to 38 ° C. In one embodiment, the culture temperature is 35 ° C. CHO cells are fed with a hydrolyzate enrichment solution and a basal enrichment solution to take care of, for example solving or correcting nutritional deficiencies to maximize productivity. Hydrolyzate and basal enrichment solutions are added to the cell culture. In one embodiment, the cell culture production medium comprises between 20 and 65% dissolved oxygen, for example, about 30% dissolved oxygen. In one embodiment, the cell culture production medium contains a glucose concentration necessary for protein production, for example, at least about 15 g / L glucose. In one embodiment, the means of production of
107
IMPI
<img file="MX353340B_D0115.tif" />
Cell culture contains approximately 1.5-2.5 g / L of glucose.
In a further embodiment, the cell culture production medium contains approximately 2.0 g / L glucose. Glucose concentration can be controlled during protein production of the culture process, adding glucose to the cell culture production medium as required, to maintain a given concentration, for example at least 2.0 g / L glucose. In one embodiment, the hydrolyzate enrichment solution used in the batch feeding method for an anti-TNFa antibody, comprises of about 50-280 g / L of a soy-based hydrolyzate (including ranges and numbers therein, by example, 100-225, 50225, 255-275, and 265 g / L), and approximately 75-300 g / L of a yeast-based hydrolyzate (including ranges and numbers therein, for example, 100-250, 150 -200, 145-175, and 165 g / L).
A basal enrichment solution optimized for use in a batch feeding method for the production of an anti-TNFa antibody, for example, adalimumab / D2E7, in CHO cells, has a pH of approximately 9.0 to 10.5 (including ranges and numbers in the same, e.g. 9.1, 9.2, 9.3, 9.4, 9.5, 9.6, 9.7, 9.8, 9.9, 10, 10.1, 10.2, 10.3, 10.4, 10.5). The period of time during which the hydrolyzate enrichment solution and the basal enrichment solution are added is between 9 to 15 days, for example 12 days. In one embodiment, the basal enrichment solution is added to the cell culture medium on at least one of the following days of the time period: day 4, day 6,
108
<img file="MX353340B_D0116.tif" />
day 9, and day 11, and the hydrolyzate enrichment solution is added to the cell culture medium on day 4, day 7, or day 4 and day 7 of the time period. Intermediate numbers of the above values are also intended to form part of the present invention.
In another alternative embodiment, the batch feeding method for the production of an anti-TNFa antibody, eg adalimumab / D2E7, may include adjusting the pH of the cell culture medium, in accordance with a linear decrease in pH, which comprises starting from a pH of about 6.5-8, for example, from 7.1 to 7.2, and ending at a final pH of about 6.9. In one embodiment, the linear decrease in pH is adjusted over a period of at least about 24 hours, 48 hours, or 72 hours.
The invention also features a batch feeding method for producing an anti-IL-12 antibody, eg ABT-874, which comprises culturing Chinese Hamster Ovary (CHO) cells comprising a nucleic acid encoding the anti-IL-12 antibody. IL12 in a cell culture at a culture temperature ranging from 32 to 38 ° C, for example 33 ° C. The hydrolyzate enrichment solution used for the production of the IL-12 antibody may also contain glucose. In one embodiment, CHO cells are grown at a pH of about 6.9. CHO cells are fed with a hydrolyzate enrichment solution and an enrichment solution
<img file="MX353340B_D0117.tif" />
109
IMPI
MEXICAN INSTTTVrO.
nr 'λ t. i í
DE LA MONEDAD IN ^ ISTEIAt basal, in order to maintain nutritional deficiencies to maximize productivity. Hydrolyzate and basal enrichment solutions are added to the cell culture. In one embodiment, the cell culture production medium comprises between 20 and 65% dissolved oxygen, for example, about 40% dissolved oxygen. In one embodiment, the hydrolyzate enrichment solution used in the batch feeding method for an anti-IL-12 antibody comprises approximately 50-280 g / L of a soy-based hydrolyzate (including ranges and numbers therein, by example, 100-225, 50-225, 255-275, and 265 g / L), approximately 75-300 g / L of a yeast-based hydrolyzate (including ranges and numbers therein, for example, 100-250, 150 - 200, 145-175 and 165 g / L), and approximately 2-3 g / L of glucose, for example 2.4 g / L glucose. The basal enrichment solution for use in a batch feeding method for the expression of an anti-IL-12 antibody, eg ABT-874, in CHO cells, has a pH of approximately 9.7 and an osmolarity of approximately 1480 mOsm . The period of time during which the hydrolyzate enrichment solution and the basal enrichment solution are added is between 14 to 15 days, for example 12 days. In one embodiment, the basal enrichment solution is added to the cell culture production medium every third day, starting on day 5 of the time period, and the hydrolyzate enrichment solution is added to the cell culture production medium daily , starting on day 6 of
110
MEXICAN INSTITUTE • í Ι.Λ FRoriEOAii <Ύ- M .á INOUSTttAl> <* * period of time. Alternatively, the basal enrichment solution and the hydrolyzate enrichment solution can be added to the cell culture production medium daily, starting on day 5 of the time period. Intermediate numbers from the above value ranges are also intended to form part of the present invention.
Stable, high concentration feed solution
One aspect of the invention features methods and compositions that relate to an improved stable high concentration feed solution, to improve protein productivity. The improved feeding solution can be used to supplement a cell culture production medium, in the production of an antibody. The feeding solution includes glucose (for example, from 100 to 250 g / kg); a basal medium; an amino acid other than glutamine, eg, asparagine (eg, 1.0 to 15.0 g / kg; 3-12.5 g / kg, or 3-5 g / kg); and at least two different hydrolyzates that are not of animal origin. Also, the feed solution has a pH of about 6.0 to 7.5. The two different hydrolyzates that are not of animal origin can include a plant-based hydrolyzate, for example soy-based hydrolyzate, and a hydrolyzate that is not animal-based or plant-based, for example, a yeast-based hydrolyzate. Any basal medium known in the art can be used in the improved feeding solution including, but not limited to, PF CHO or DMEM / medium
111
<img file="MX353340B_D0118.tif" />
MEXICAN INSTITUTE OI LA MUOMtDAI 'iNOüjni.iAi
F12. A basal medium may also be used. '^ ETrnrfTsrTmytiialitt ^ d'r the basal cell medium excludes the following components: sodium bicarbonate, buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, glutamine and glucose. The improved feed solution is stable, having a turbidity of less than about 15 UTN. The invention also includes maintaining a constant glucose level of the cell culture production medium, adding the feed solution. Intermediate numbers from the above value ranges are also intended to form part of the present invention, eg 3.0, 3.1, 3.2, 3.3, 3.6, 3.8, 4, 4.2, 4.4, 4.6, 4.8 and 5 g / kg of asparagine.
Also included in the invention is a method of making a feeding solution comprising glucose and at least two different hydrolyzates that are not of animal origin. The method of making the feeding solution includes combining glucose and a basal cell medium to a combined solution, and adjusting the pH of the combined solution to approximately 9.5 to 10.5. Subsequently, at least two different non-animal hydrolyzates are added to the solution, and the pH is adjusted again so that the resulting feed solution has a pH of approximately 6.5 to 7.5. Intermediate numbers from the above value ranges are also intended to form part of the present invention, eg pH of 6.6, 6.7, 6.8, 6.9, 7.0, 7.1, 7.2, 7.3, 7.4, 7.5.
112
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IMPI
The feed solution of the invention can be used to achieve high levels of recombinant protein production, eg, antibody production, from mammalian cell culture. In one embodiment, the invention features a method of producing at least 1.5 g / L of an antibody from a mammalian cell culture, comprising culturing mammalian cells comprising a nucleic acid encoding the antibody, in a medium. of cell culture production.
Subsequently, a feeding solution having a pH of approximately 6.7 to 7.0 is added to the cell culture production medium. The feeding solution includes glucose (eg, about 100 to 250 g / kg); a basal cell medium; a different amino acid from glutamine; and at least two different hydrolyzates that are not of animal origin. In one embodiment, such a process results in the production of at least 2 g / L of an antibody, at least 4 g / L of an antibody; at least about 5 g / L of the antibody; and at least 6 g / L of the antibody. Intermediate numbers from the above value ranges are also intended to form part of the present invention, for example 1.5, 1.6, 1.7, 1.8, 1.9, 2.0, 2.1, 2.2, 2.3, 2.4,
2.5 g / L of the antibody.
When using a feeding solution that has a pH of approximately 6.7 to 7.2 and including the following components: glucose; a basal cell medium; about a different amino acid than glutamine; and at least two different hydrolyzates that don't
<img file="MX353340B_D0120.tif" />
113 are of animal origin, the'-tfTtrfu of the anttcwrprr produced from a mammalian cell culture can be increased. In one embodiment, by adding the feed solution to a cell culture production medium for mammalian cells comprising a nucleic acid encoding the antibody, an increase of at least 50% more than that of a mammalian cell culture is obtained. control, which is grown without the addition of the feed solution. In one embodiment, the addition of the feed solution results in an increased titer of at least<sup>n</sup>100% more than the control. In one embodiment, the addition of the feed solution results in a titer increase of at least 150% more than that of the control. The supplemental feeding solution can be added to the cell culture at a certain cell density, for example when the cell density reaches at least 2.0 x 10<sup>6</sup> cells / mL or cell density reaches at least 3.5 x 10<sup>6</sup> cells / mL. Numbers intermediate to the range of values above, are also intended to form part of the present invention. Range of values, using a combination of any of the values mentioned above as upper and / or lower limits, are intended to be included within the scope of the invention.
Since the batch feeding methods of the invention serve to take care of, for example solving or correcting, certain nutritional requirements of a cell culture for the production of a protein, for example an antibody, it can be
114
IMPIAS Mexican Institute
M LA KROHÍOA »C» JIM advantageous to monitor certain ingredients. The incp'eWen te> -T ^ í ^ can be monitored include any metabolic indicator ·, that is, an indicator of cellular metabolism. In one embodiment, the batch feeding method of the invention comprises monitoring the glucose concentration in the cell culture medium, including monitoring the glucose concentration to be maintained at between 0.25-20 g / L. In one embodiment, the glucose concentration is maintained at 0.5 to 5.5 g / L or 4 .0-5.5 g / L. By monitoring glucose levels, cellular metabolism can be indirectly monitored. As described in Example 3, glucose can be used as a metabolic indicator. In one embodiment, a cell culture can be supplemented with a nutritional component or components, eg, a hydrolyzate, based on glucose concentration. Methods for monitoring glucose concentrations are known in the art and may include monitoring using an automated sampling apparatus. Another example of a metabolic indicator that can be used is glutamine. Numbers intermediate to the above ranges, as well as other numbers mentioned herein, are also intended to form part of the present invention. Range of values, using a combination of any of the values mentioned above as upper and / or lower limits, are intended to be included within the scope of the invention.
A feedback control system can be used to monitor the concentration of an indicator
115 metabolic in the
<img file="MX353340B_D0121.tif" />
cell culture production medium. In one embodiment, in order to meet a set point of a desired parameter, for example a predetermined glucose concentration, a combined feed solution is added to the cell culture production medium, as determined by the feedback control system .
The feedback control system can also be used to determine a feeding profile for a given mammalian cell culture, and the production of a protein of interest. In one embodiment, a method of determining a feeding profile for producing a protein in a mammalian cell culture, comprises culturing mammalian cells comprising a protein-encoding nucleic acid, and adding a feeding solution, eg, a Combined feeding solution to the cell culture medium, using a feedback control system to monitor a metabolic indicator. The feed solution is added to the cell culture production medium to meet a set point of a target metabolic indicator, for example, a glucose concentration. After completion of cell culture, the amount of the feed solution added to the cell culture production medium per day is determined, and a feed profile of when a feed solution should be added to the cell culture is provided. Once a feeding profile is established, it is no longer necessary to monitor the metabolic indicator for a culture of
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116 mammalian cells since it produces a protein of interest. A feeding profile has many advantages, including a decreased risk of contamination, since frequent sampling is no longer required.
Methods and compositions of N-acetylcysteine and sodium butyrate
As described above, the cell culture process of the present invention advantageously achieves an increased antibody titer. Another aspect of the invention to achieve protein productivity in a mammalian cell culture is by adding sodium butyrate, N-acetylcysteine, or a combination thereof, to the cell culture medium. In one embodiment, the invention characterized a method of producing an antibody, adding sodium butyrate (eg, 0.1mM to 10mM), N-acetylcysteine (eg, 1mM to 80mM), or a combination of the themselves to the cell culture medium. In one embodiment, the antibody titer is at least about 100 mg / L; at least about 150 mg / L; at least about 200 mg / L; at least about 250 mg / L; at least about 300 mg / L; at least about 350 mg / L; or at least about 400 mg / L.
The invention also features a method of producing an antibody in a mammalian cell culture, so that the antibody titer is improved by at least 10% relative to a control mammalian cell culture, by adding sodium butyrate (eg, final concentration of 0.1 mM to 10 mM), N-acetylcysteine
<img file="MX353340B_D0123.tif" />
117 (eg, final concentration of 1 mM at Έ0 ”'7ηΚ * ί),' or a nail 'combination thereof, to the cell culture medium (accordingly, the control lacks sodium butyrate, Nacetylcysteine, or the combination thereof). In one embodiment, the antibody titer of the mammalian cell culture is improved by at least 29% relative to the control mammalian cell culture; at least 40% relative to control mammalian cell culture; at least 70% with respect to control mammalian cell culture; or at least 90% more than that of the control mammalian cell culture. Sodium butyrate, N-acetylcysteine, or a combination thereof, can be added to the mammalian cell culture during the growth phase of the mammalian cell culture. In one embodiment, sodium butyrate, Nacetylcysteine, or a combination thereof, is added to the mammalian cell culture between days 4 and 7 of culture time. In one embodiment, N-acetylcysteine is added, either alone or in combination with sodium butyrate, in an amount in the range of a final concentration of 5mM to 80mM, for example, 20-60mM, or approximately 10mM .
The invention also features a method of extending the longevity of a mammalian cell culture to at least about 45% compared to a control mammalian cell culture, adding about 0.1 mM to 10 mM of N-acetylcysteine to the cell medium (the control culture lacks this addition). In one embodiment, the longevity of the cell culture —1 <ι iHfc »* ·
118
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of mammal is widespread at least approximate<sup>1</sup>· Comparison with control mammalian cell culture; or at least about 55% compared to control mammalian cell culture.
It should be noted that the cell culture media and improved culture methods described herein can be used separately or in combination with each other.
After cultivation, using the methods and compositions of the invention, the resulting expressed protein can subsequently be recovered or collected. Furthermore, the protein can be purified or partially purified from said culture or component (for example, from the culture medium or cell extracts or intracellular fluid), using known processes. Fractionation procedures may include, but are not limited to one or more stages of filtration, centrifugation, precipitation, phase separation, affinity purification, gel filtration, ion exchange chromatography, hydrophobic interaction chromatography (CIH, using such resins such as phenyl ether, butyl ether or propylether), HPLC or some combination of the above.
For example, purification of the polypeptide may include an affinity column containing agents that will bind to the polypeptide; one or more column steps on such affinity resins as concavalin A-agarose, HEPARIN-TOYOPEARL (chromatographic medium) or Cibacrom blue 3GA SEPHAROSE (agarose beads); one or more stages involving elution; me
119
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immunoaffinity chromatography. The patipepHete — rprretre — SST expressed in a form that facilitates purification. For example, it can be expressed as a fusion polypeptide, such as maltose binding polypeptides (PUM), glutathione-S-transferase (GST), or thioredoxin (TRX). Packages for the expression and purification of such fusion polypeptides are commercially available from New England BioLab (Beverly, Mass.), Pharmacia (Piscataway, NJ.) And InVitrogen, respectively. The polypeptide can be labeled with an epitope and subsequently purified using a specific antibody directed at such an epitope. One such epitope, FLAG (epitope brand), is commercially available from Kodak (New Haven, Conn.). It is also possible to use an affinity column comprising a polypeptide-binding polypeptide, such as a monoclonal antibody to the recombinant protein, to affinity purify the expressed polypeptides. Other types of affinity purification steps may be a protein A or G column, whose affinity agents bind to proteins containing Fe domains. Polypeptides can be removed from an affinity column using conventional techniques, for example in a high salt content elution solution and subsequently dialysed in a lower salt content buffer, for use or by changing the pH or other components depending of the affinity matrix used, or they can be competitively removed using the naturally occurring substrate of the affinity portion. In a
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120 In the modality, the antibodies produced using the methods and compositions of the invention are purified in accordance with the methods described in North American Patent Application No. 11/732918, incorporated herein by reference.
The desired degree of final purity depends on the intended use of the polypeptide. The methods and compositions of the invention are suitable for therapeutic uses of the protein of interest. Therefore, a relatively high degree of purity is desired, when the polypeptide is to be administered in vivo. In such a case, the polypeptides are purified in such a way that the non-polypeptide bands that correspond to other polypeptides are detectable when analyzed by polyacrylamide gel electrophoresis are DSS (EGPA-DSS). A person skilled in the art will recognize, in the pertinent field, that the multiple bands corresponding to the polypeptide can be visualized by EGPA-DSS, due to differential glycosylation, differential post-translational processing and the like. More preferably, the polypeptide of the invention is purified to substantial homogeneity, as indicated by a single polypeptide band when analyzed by EGPA-DSS. The polypeptide band can be visualized by plant staining, Coomassie blue staining or (if the polypeptide is radiolabeled), by autoradiography.
Optionally, the invention also encompasses protein formulation. The term formulation means that proteins can be exchanged in regulatory solutions,
<img file="MX353340B_D0127.tif" />
<sub>121</sub> ΙΜΡΙ <sup>1</sup> X- <sup>1</sup> MEXICAN INSTITUTE
OF THE FROHEDAD
INDUSTRIAL sterilized, packed in bulk and / or packed., For.-uo final. Such compositions may comprise an effective amount of the protein, in combination with other components such as a pharmaceutically acceptable diluent, vehicle, or excipient. The term "physiologically acceptable" means a non-toxic material that does not interfere with the effectiveness of the biological activity of the active ingredient or ingredients.
It should be noted that, with respect to the numbers cited herein, numbers that are intermediate to the above ranges, as well as other numbers cited herein, are also intended to form part of the present invention. Range of values, using a combination of any of the values mentioned above as upper and / or lower limits, are intended to be included within the scope of the invention.
Examples
The following Examples show improved methods and compositions for culturing mammalian cells, including improved methods and compositions for the expression of biologics in mammalian cells. An improved biochemically defined medium for culturing Chinese Hamster Ovary (CHO) cells, used to express various recombinant biologics, is described below. In addition, media processes for culturing cells in large-scale bioreactors under various configurations and scales, containing the same components but with different balance, are also exemplified.
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of components and enriched, to allow greater cell growth and an increase in the expression of the product.
EXAMPLE 1: IMPROVED MEANS TO CULTIVATE CELLS OF
MAMMAL
Typically, mammalian cell culture media, eg, Chinese Hamster Ovary (CHO), are based on commercially available media formulations, such as DMEM, Ham's F12, or combinations of these media types. For the preparation of proteins in mammalian cells, a cell culture medium must be sufficiently enriched to support the increase in both cell growth and expression of the biological product. The following examples describe an improved biochemically defined medium for culturing mammalian cells, eg, Chinese Hamster Ovary (CHO) cells, to express various recombinant biologics, including antibodies.
Dihydrofolate reductase [dhfr (-) j deficient Chinese Hamster Ovary (CHO) cells were adapted to grow in suspension in the absence of serum or any other material derived from an animal source. Cells were grown in the absence of hypoxanthine and thymidine, in a cell defined culture medium obtained from a commercial source, JRH PF-CHO (Catalog # 67147). Although the cell line was not deficient in glutamine synthetase, additional glutamine was added to the culture medium.
CHO cell lines expressing
<img file="MX353340B_D0129.tif" />
<img file="MX353340B_D0130.tif" />
123 biological products, such as corrtrartrn übj ^ tivml'crd'O * antibodies, 'by using molecular biology techniques known in this field. Briefly, an expression vector capable of expressing the antibody of interest and capable of expressing the dhfr enzyme gene, was introduced into CHO cells using methods known in the art. The transfected cells of interest were obtained by selecting the cells in the presence of hypoxanthine and thymidine. The selected transformants were further cultured in increasing concentrations of methotrexate, to amplify the transfected genes and increase the yield of the expressed proteins. The improved cell culture medium used to cultivate CHO cells is described below.
Example 1.1: Cell Culture Medium for Chinese Hamster Ovary Cells (CHO)
Generally, the CHO cell culture media formulations consisted of three parts, designated Parts A, B, and C. Part A was a basal medium and comprised of water, amino acids, vitamins, inorganic metal salts, trace elements, ethanolamine, putrescine , a surface active agent, sodium pyruvate, glutathione and 2-mercaptoethanol. Part B comprised an inorganic iron source; and Part C comprised recombinant growth factors, buffers, an osmolarity regulator, an energy source, various non-ferrous metal ions, a surfactant, and hydrolyzed js. The components of the medium were mostly
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inorganic or came from a source rp ^ e-mbinant<sup>0</sup> and highly purified pstahan. The media contained no proteins, lipids, or carbohydrates from animal sources. Complexes were obtained from highly processed yeast sources and plants.
Part A of the medium included protein-free CHO (PF CHO) medium (JRH-SAFC Biosciences; JRH Cat # 67147 - also referred to as Part A Original). Thus, Part A included a basal medium, including water, amino acids, and vitamins. The basal medium (PF CHO) was selected to effect modifications and reformulation to support further increases in cell growth and in the productivity of the expressed protein. PF CHO medium was modified to remove certain components, including sodium bicarbonate, HEPES buffer, monobasic sodium phosphate, dibasic sodium phosphate, an osmolarity regulator, a surfactant, and glucose as a monosaccharide (the modified PF CHO medium is referred to herein as a Party
A modified (also called JRH Catalog # 67411)). These modifications were also made to facilitate the conditions for improvement in the cell culture process in large-scale bioreactors.
The Part B (JRH) component consisted of a concentrated ferric citrate solution, which was added separately.
The concentration of the Part B component was kept constant in all CHO cell culture projects.
<img file="MX353340B_D0132.tif" />
growth, for example insulin, the aminoarnto — glutairnird ·; —TC yeastolate and soybean phyton hydrolyzate, with methotrexate being necessary to retain the selective pressure, and the NaOH base and HCI acid were used to adjust the pH after the media were hydrated during their preparation.
The formulations of the improved cell culture media were performed as follows. First, CHO cells were originally grown in PF-CHO medium (SAFC-JRH Catalog # 67147), obtained from JRH. PF-CHO medium (Catalog # 67147) was further modified for use with the CHO cell lines to be described later. This modified media was designed by JRH, with a new Catalog # 67411. The goal of the modifications was to allow the concentrations of Part A of the cell culture medium to be increased, so that neither osmolarity nor pH was affected. The original Part A (Catalog # 67147) also stated the manufacturer (JRH) that it contained no sodium bicarbonate, glutamine, and was protein-free (without insulin or other proteins or peptide growth factors). These omitted components, then, were added to Part A formulations 67147 and 67411 independently, specifically for CHO cell lines when proven effective. These were some of the components that are described in detail below as the Part
C.
i. · *.
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<img file="MX353340B_D0134.tif" />
126
Table 1: Composition of the original cell culture formulation formulation (Part A 67147), with modified culture medium formulation (Part A 67411 modified)
<td>Component</td><td>Cell culture medium containing 67147 (RM-003) (original Part A)</td><td>Cell culture medium containing 67411 (RM-230) modified (Part A modified) at 1X, 2X, 3X, and 4X g / L</td>
<td>Part A</td><td></td><td></td>
<td>Original Part A, Powder: JRH Source. 1X concentration only</td><td>16.45g / L.</td><td>NA</td>
<td>Part A Modified: JRH Special Source. Selected components without sodium bicarbonate, HEPES, and the monobasic and dibasic sodium phosphates, the sodium chloride osmolarity regulator, the Pluronic F-68 surfactant, and the glucose monosaccharides</td><td>NA</td><td>2.63,526,789 and10.52 g / L</td>
<td>Part b</td><td></td><td></td>
<td>Part B: Ferric Citrate JRH, concentrated solution</td><td>10 mL / L (0.5 mM)</td><td>10 mL / L (0.5 mM)</td>
<td>Part c</td><td></td><td></td>
<td>Growth factor, monosaccharide, energy source-amino acid: multiple levels</td><td></td><td></td>
<td>Human insulin</td><td>2-4 mg / L</td><td>4-13 mg / L</td>
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127 ΐΜΡυ
INSTITUTO Mexicano ¿E LA FROFliDAO INO 'ISTXIAL
<td rowspan="2">Component</td><td rowspan="2">Cell culture medium containing 67147 (RM-003) (original Part A)</td><td>Culture medium</td>
<td>67411 (RM-230) modified (Part A modified) at 1X, 2X, 3X, and 4X g / L</td>
<td>recombinant</td><td></td><td></td>
<td>Glucose</td><td>1.5-3.5 g / L</td><td>Up to 7.0 g / L max.</td>
<td>L-glutamine</td><td>0.292 g / L</td><td>0.584 g / L</td>
<td>Shock absorbers: keep at a single concentration</td><td></td><td> •</td>
<td>Sodium bicarbonate</td><td>16 g / L</td><td>1.6g / L</td>
<td>HEPES</td><td>NA</td><td>1.8g / L</td>
<td>NaH<sub>2</sub>PO<sub>4</sub>-H<sub>2</sub>OR</td><td>NA</td><td>0.031 g / L</td>
<td>Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR</td><td>NA</td><td>0.436 g / L</td>
<td>Regulator Osmolarity: Levels Multiple per Line Product</td><td></td><td></td>
<td>NaCI</td><td>NA</td><td>0-6.5 g / L</td>
<td>Hydrolyzed: Multiple Levels per Product Line</td><td></td><td></td>
<td>Bacto TC Yeastolate</td><td>NA</td><td>2.0-10.7 g / L</td>
<td>Peptona BD Phytone (soy)</td><td>NA</td><td>0-6.92 g / L</td>
<td>Primatone</td><td>NA</td><td>2-8 g / L</td>
<td>Others / Additional Agents</td><td></td><td></td>
<td>Selective pressure (dhfr system): Multiple Levels per Product Line</td><td></td><td></td>
<td>Methotrexate</td><td>At the required level of amplification</td><td>At the required level of amplification</td>
<td>Cut Protective Surfactant: Single Level</td><td></td><td></td>
<td>Pluronic F-68</td><td>1.0 g / L</td><td>10 g / L</td>
<img file="MX353340B_D0136.tif" />
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128 Mexican rrsTm'To DE LA MONEDAD fNnUSTPlAl.
<td rowspan="2">Component</td><td rowspan="2">Cell culture medium containing 67147 (RM-003) (original Part A)</td><td>Culture medium ----—</td>
<td>cell phone containing 67411 (RM-230) modified (Part A modified) at 1X, 2X, 3X, and 4X g / L</td>
<td>Acid-Base for pH adjustment</td><td></td><td></td>
<td>NaOH</td><td>As necessary</td><td>As necessary</td>
<td>HCI</td><td>As necessary</td><td>As necessary</td>
<td>Target Solutions</td><td></td><td></td>
<td>final pH</td><td> 7.2-7.4</td><td> 7.1-7.3</td>
<td>Final osmolarity</td><td> 280-320</td><td> 280-320</td>
Part A of Cell Culture Medium to Grow CHO Cells
As described above, Part A of the improved cell culture medium contained a modified version of the basal medium, ie PF-CHO medium. The PF-CHO medium (Catalog No. 67147) obtained from JRH, was modified by removing the sodium bicarbonate, HEPES and monobasic and dibasic phosphate buffers, the sodium chloride osmolarity regulator, the Pluronic F-68 surfactant, and the monosaccharide glucose, from. Part A. These components were added back to Part A at various concentrations, depending on the needs of the specific cell culture project. This allowed the buffer concentration to remain constant, and the surfactant concentration to remain below levels toxic to cells, while allowing osmolarity and carbon substrate levels to be manipulated to increase the growth of the cells. cells and increase the production of antibodies. Once
<img file="MX353340B_D0137.tif" />
these components were separated from the formulation-Aoriginal Part of JRH, the increase in the concentration of the remaining components in JRH Part A was facilitated, as observed in the modified cell culture medium (modified PF CHO -referred as # 67411 in Table 1), thus allowing an increase in cell growth and antibody expression, determined by antibody titration. The individual components of the modified Part A (67411) powder formulation, including amino acids, vitamins, trace elements, and other miscellaneous component fractions, were increased up to four-fold from the concentration in the original formulation, without having to change the volume of the means, medium. A comparison of the original Part A formulation using 67147 and the formulation using 67411 was previously described in Table 1.
By definition, JRH's original PF CHO Basal Medium (Catalog # 67147) was also a glutamine-free and sodium bicarbonate-free PF CHO Basal Medium. The original glucose concentration in Part 1 was 1.5 mg / L.
Part B of Cell Culture Medium to Grow CHO Cells
The Part B component of the cell culture medium comprised a concentrated solution of ferric citrate, which was the same as the Part B component of the PF-CHO medium (Catalog No. 67147) obtained from JRH, and was added separately.
Inorganic iron sources, such as ferrous and ferrous salts, particularly ferric citrate and ferrous sulfate, are
<img file="MX353340B_D0138.tif" />
130 added to basal medium, for example Part A or modified Part A ^ Although a small amount of ferrous sulfate (0.2-0.8 mg / L) and unhydrated ferric nitrate (0.025-0.11 mg / L) were added, chelated salts were preferred , such as ferric citrate. Ferric citrate was added in higher concentration as a liquid supplement, and was included in the cell culture medium as PF-CHO Part B. Although the concentration of the other components of the medium could change and have a greater concentration range, ferric citrate was maintained at a single concentration of 122 mg / L. This was due to the formation of superoxides and free radicals that cause cellular damage, and to the formation of unwanted compounds in the basal medium.
Part C of Cell Culture Medium to Grow CHO Cells
Part C of the cell culture medium mainly comprised recombinant growth factors, regulatory solutions, an osmolarity regulator, an energy source, and hydrolyzates. Additional compounds added to the cell culture medium that are not included in the usual groups of amino acids, vitamins and cofactors, inorganic salts and buffers, trace elements or minerals, in the course of development, were described in Table 1 above as Part C. With respect to Part C mentioned in Table 1, it should be noted that the ingredients identified in Part C can be added separately or in combination.
Recombinant growth factors
The peptide hormone insulin, or alternatively a
<img file="MX353340B_D0139.tif" />
<sub>131</sub> IMPI
I 5 I MEXICAN INSTITUTE
PE THE PROPERTY industrial recombinant analog, was added to the environment do icultive ^ oiniar <= »<sub>n</sub> or<sub>n </sub>concentration range of 4-13 mg / L. IGF-1 can also be added by substituting or supplementing insulin, to the cell culture medium, at a concentration of 50-100 ng / L.
Osmolarity regulator
The osmolarity of the various cell culture media was in the range of 260 to 460 mOsm. Osmolarity regulation was carried out through salts, especially NaCI, KCI and KNO<sub>3</sub>, although all amino acids and hydrolyzates contribute considerably to change osmolarity.
Power source
The most abundant monosaccharide in the culture medium was glucose (D-glucose) and it was supplemented as necessary. The initial concentration of the cell culture medium varied within the range of 3.5 to 7.0 g / L. Other sugars can also be supplemented as metabolites or as protectors, these can include maltose, mannose, galactose or fructose.
Hydrolyzed
Hydrolyzates are considered as an additional source of free amino acids, along with dipeptides and tripeptides. PH maintenance (buffer)
Various buffers were used to keep the pH of the cell culture medium within a range of 6.5 to 7.5. Inorganic buffers (or buffer systems) used in the media included carbonates (NaHCO<sub>3</sub>), chlorides (CaCI<sub>2</sub>),
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sulfates (MgSO<sub>4</sub>) and phosphates (NaH<sub>2</sub>PO<sub>4</sub> v Na-, ΗΡΩΐ ι ns organic buffers also include Sodium Pyruvate (C<sub>3</sub>H<sub>3</sub>OR<sub>3</sub>Na) and N- [2-hydroxyethyl] piperazin-N '- [2-ethanesulfonic] acid, also known as HEPES.
Glutamine
Glutamine was also included in Part C, as it was omitted from the original Part A and modified Part A. Glutamine was included in Part C, for example at a rate of 0.2 to 0.4 (0.29) g / L in the cell culture medium containing the original Part A, and at a rate of 0.3 to 0.7, for example 0.58 in the medium of cell culture containing the modified Part A (see Table 1 above).
Other Components of Cell Culture Medium to Grow CHO Cells
Additional components that can be added to the cell culture medium are provided below. It should be noted that the additional components that can be added are not limited to the examples provided below.
Additional peptides
Putrescine HCI salt, which helps to maintain the structure of the endoplasmic reticulum and the specific growth for CHO cell lines, which was added at a rate of 0.4 to 1.65 mg / L to the basal medium.
Glutathione (a tripeptide) was added in amounts ranging from 0.5 to 2.0 mg / L. Also added 2
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<img file="MX353340B_D0142.tif" />
133 mercaptoethanol at 3.6 mg / L, acting as an act — Foduotor — to maintain sulfhydryl groups and to bind and transport various metals, such as copper. Reduces dehydroascorbate and cystine, and regenerates ascorbate and cysteine.
Methotrexate
Methotrexate concentrations differed between product lines, depending on the final amplification levels to be achieved. Using a concentrated solution with a 2mM concentration, the addition volumes and the final concentrations are: 0.250 mL / kg produces 500 nM final for anti-IL-12 and anti-EPO-R; 0.5 mL / kg produce a final concentration of 100 nM for anti-IL-18¡ and finally, 2.5 mL / kg produce a final concentration of 5000 nM for anti-TNF alpha.
Cellular Protector / Surfactant
The media described in this example were used to culture CHO cells in suspension, on all scales of reactors, bottles, and flasks, both under agitation and under bubbling, which created high shear forces. To minimize cell damage, a cell protector such as pluronic polyols, specifically Pluronic F-68, was added at a concentration of approximately 1 g / L medium. Other cutting mitigants included methylcellulose at a concentration less than or equal to 1 g / L, and certain hydrolyzates or plant extracts, at varying concentrations, up to amounts of grams per liter.
Amino acids
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134
The cell culture medium had a number of various amino acids, as described herein. Two amino acids, asparagine and glutamine, were added in higher initial concentrations than the other amino acids, as these rapidly become limiting nutrients during the course of CHO cell culture. Asparagine in particular constitutes approximately 0.4 to 0.5 g / kg of the basal medium.
While asparagine was a component of Part A (including the original and modified PF CHO), the concentration of asparagine was increased by adding it to the cell culture medium.
The cell culture medium was able to support the growth of CHO cells from very low initial densities to more than 1.0 * 10<sup>7</sup> cells / mL, for a number of days, depending on the concentration of the components with purpose and cellular effect of the desired medium. The CHO process additionally included a growth phase and a production phase, as will be described in other sections, and required different ranges of components. However, the proportions and identities of the cell culture medium formulation remained the same.
Final preparation of CHO cell medium
Preparation of the improved cell culture medium required the addition of various components in a particular order, with pH adjustments using a base or an acid at particular times. The base was added as NaOH as the basal concentration of Part A increased, to help
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<img file="MX353340B_D0144.tif" />
dissolve amino acids in the formulation up to a maximum pH of
10. The pH was lowered to a minimum of 7.0, as the hydrolyzates were added, using an acid in the form of HCI. Other adjustments to a particular pH were carried out using NaOH or HCI, as necessary.
The following examples describe cell culture media based on the above, for the expression of various specific antibodies.
Example 1.2: Cell Culture Medium to Grow CHO Cells Expressing Anti-TNF Alpha Antibody
CHO cell lines expressing a complete human antibody against TNFa (eg adalimumab; D2E7) were grown in the cell culture media described in Table 2.
Table 2: Cell Culture Media for Culturing CHO Cells Expressing Complete Human Anti-TNF Alpha Antibody
<td>Media Components</td><td rowspan="2">Raw Materials Specification #</td><td>AFD2-E71XP</td><td>AFD2E7- 1XP</td><td>AF and AY- D2E7</td><td>AY-D2E7- 2XP</td><td>AY-D2E7</td>
<td>Component List: JRH Part A and Part B</td><td>SR243Crecim. +</td><td>SR-250 Growth + MT X</td><td>SR-286 Production proad_3XP</td><td>SR-332 I grew up. one</td><td>SR-333 I grew up. 2</td>
<td>ABC components added</td><td>final pH</td><td> 7.2 ±0.1</td><td> 7.2 ±0.1</td><td> 7.2 ±0.1</td><td> 7.2 ±0.1</td><td> 7.2 ±0.1</td>
<td></td><td>Final osmolarity:</td><td> 280-320</td><td> 280-320</td><td> 370-390</td><td> 320-360</td><td> 320-360</td>
<td>Part A: unmodified -original commercially available</td><td>RM-003</td><td> 16.45</td><td> 16.45</td><td>NA</td><td>NA</td><td>NA</td>
<td>Part A Special (Modified): Salt Free</td><td>RM-230</td><td>NA</td><td>NA</td><td>7.89 g / kg</td><td>5.26 g / kg</td><td>5.26 g / kg</td>
<td>Part B: ferric citrate: source of chelated fiemo</td><td>RM-004</td><td>10 mL / kg</td><td>10 mL / kg</td><td>10 mL / kg</td><td>10 mL / kg</td><td>10 mL / kg</td>
<td>Part C:</td><td></td><td></td><td></td><td></td><td></td><td></td>
<td>Insulin HUR: Recombinant Glucose Protein Regulator</td><td>SR-055</td><td>2.0 mL / kg (4mg / kg)</td><td>2.0 mL / kg (4 mg / kg)</td><td>6.0 mL / kg (12mg / kg)</td><td>3.88 mL / kg (8 mg / kg)</td><td>3.88 mL / kg (8 mg / kg)</td>
<td>Anhydrous glucose: carbon source</td><td>RM-011</td><td>3.5 g / kg</td><td>3.5 g / kg</td><td>7.0 g / kg</td><td>7.0 g / kg</td><td>7.0 g / kg</td>
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<td rowspan="2">Media Components</td><td rowspan="2">Raw Materials Specification #</td><td rowspan="2">AFD2-E71XP</td><td rowspan="2">AFD2E71XP</td><td>AF and AY-</td><td>AY-D2E7-</td><td rowspan="2">AY-D2E7</td>
<td>D2E7</td><td>2XP<sup>-</sup> '</td>
<td>L-glutamine: amino acid and energy source</td><td>RM-071</td><td>0.292 g / kg</td><td>0.292 g / kg</td><td>0.584 g / kg</td><td>0.876 g / kg</td><td>0.876 g / kg</td>
<td>NaH2P04 «H20: phosphate buffer</td><td>RM-200</td><td>Part A: 0.031 g / kg</td><td>Part A: 0.031 g / kg</td><td>0.031 g / kg</td><td>0.031 g / kg</td><td>0.031 g / kg</td>
<td>Na2HPO4 «H2O: phosphate buffer</td><td>RM-233</td><td>Part A: 0.436 g / kg</td><td>Part A: 0.436 g / kg</td><td>0.436 g / kg</td><td>0.436 g / kg</td><td>0.436 g / kg</td>
<td>Bacto TC Yeastolate: yeast</td><td>RM-216</td><td>2.0 g / kg</td><td>2.0 g / kg</td><td>10.7 g / kg</td><td>4.0 g / kg</td><td>4.0 g / kg</td>
<td>Peptone Phytone: hydrolyzed plant soy source</td><td>RM-238</td><td>NA</td><td>NA</td><td>6.92 g / kg</td><td>2.6 g / kg</td><td>2.6g / kg</td>
<td>Sodium bicarbonate: buffer: CCk-pH regulator</td><td>RM-077</td><td>1.6 g / kg</td><td>1.6 g / kg</td><td>1.6 g / kg</td><td>1.6 g / kg</td><td>1.6 g / kg</td>
<td>HEPES: organic buffer</td><td>RM-090</td><td>NA</td><td>NA</td><td>1-8 g / kg</td><td>1.8 g / kg</td><td>1.8 g / kg</td>
<td>NaCI (salt): osmolarity regulator</td><td>RM-174</td><td>Part A: 6.5 g / kg</td><td>Part A: 6.5 g / kg</td><td>3.45 g / kg</td><td>2.67 g / kg</td><td>2.67 g / kg</td>
<td>Other components</td><td></td><td></td><td></td><td></td><td></td><td></td>
<td>L-asparagine monohydrate: amino acid</td><td>RM-284</td><td>NA</td><td>NA</td><td>NA</td><td>0.45 g / kg</td><td>0.45 g / kg</td>
<td>Pluronic F-68 (Poloxamer 188 NF): surfactant, vehicle</td><td>RM-188</td><td>NA</td><td>NA</td><td>1.0 g / kg</td><td>1.0 g / kg</td><td>1.0 g / kg</td>
<td>Methotrexate: Selective in the DHFR CHO Amplification System</td><td>SR-133</td><td>2.50 mL / kg</td><td>2.50 mL / kg</td><td>2.50 mL / kg</td><td>2.50 mL / kg</td><td>2.50 mL / kg</td>
<td>2N NaOH: Base</td><td>SR-288</td><td>As necessary</td><td>As necessary</td><td>5.67 mL / kg</td><td>3.5 mL / kg</td><td>3.5 mL / kg</td>
<td>HCI2N: Acid</td><td>SR-287</td><td>As necessary</td><td>As necessary</td><td>2.5 mL / kg</td><td>2.91 mL / kg</td><td>2.91 mL / kg</td>
Example 1.3: Composition of the Media to Grow CHO Cells Expressing the Antibody Against IL-12
The CHO cell line expressing a complete human antibody against IL-12 was grown in a culture medium described in Table 3.
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<img file="MX353340B_D0146.tif" />
_ _ _ _ _<sub>β Λ</sub> INDUSTRIAL
Table 3: Media to Grow CHO Cells Expressing the
Complete Human Anti-lLi2 Antibody (ABT-874)
<td></td><td rowspan="2">Specification of Raw Material #</td><td>ABT-874</td><td>ABT-874</td><td>ABT-874</td><td>ABT-874</td><td>ABT-874</td><td>ABT-874</td><td>ABT-874</td>
<td>Name of the medium</td><td>SR-383 Increase</td><td>SR-352 Production</td><td>SR-468 Feeding</td><td>SR-351 Alim. Glu</td><td>SR-274</td><td>SR-273</td><td>SR-272</td>
<td>Final pH:</td><td></td><td></td><td></td><td></td><td></td><td> 65-6.9</td><td> 6.5-6.9</td><td> 6.5-6.9</td>
<td>Final osmolarity:</td><td></td><td></td><td></td><td></td><td></td><td> 2.65-2.82</td><td> 2.65-2.82</td><td> 2.65-2.82</td>
<td>Part A: Unmodified - commercially available original</td><td>RM-003</td><td>NA</td><td>NA</td><td>NA</td><td>NA</td><td>16.45 g / kg</td><td>16.45 g / kg</td><td>16.45 g / kg</td>
<td>Part A (modified): salt free</td><td>RM-230</td><td>5.26 g / kg</td><td>NA</td><td>NA</td><td>NA</td><td>NA</td><td>NA</td><td>NA</td>
<td>Part A (modified) ·, free of salt and reduced in vitamins</td><td>RM-322</td><td>NA</td><td>7.89 g / kg</td><td>21.0 g / kg</td><td>7.89 g / kg</td><td>NA</td><td>NA</td><td>NA</td>
<td>Part B: citrate iron: source of chelated iron</td><td>RM-004</td><td>10 mL / kg</td><td>10 mL / kg</td><td>NA</td><td>10 mL / kg</td><td>10 mL / kg</td><td>10 mL / kg</td><td>10 mL / kg</td>
<td>Part C:</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>
<td>Bovine transfer: source of animal faith, vehicle</td><td>SR-057</td><td>NA</td><td>NA</td><td>NA</td><td>NA</td><td>NA</td><td>NA</td><td>NA</td>
<td>Recombinant Human Insulin: Recombinant Glucose Protein Regulator</td><td>SR-055</td><td>3.88 mL / kg</td><td>6.5 mL / kg</td><td>NA</td><td>6.5 mL / kg (13 mg / kg)</td><td>2 mL / kg (4 mg / L)</td><td>2 mL / kg (4 mg / L)</td><td>2 mL / kg (4 mg / L)</td>
<td>Anhydrous glucose: carbon source</td><td>RM-011</td><td>7.0 g / kg</td><td>7.0 g / kg</td><td>150 g / kg</td><td>200 g / kg</td><td>3.5 + 1.5 g / kg</td><td>3.5 + 1.5 g / kg</td><td>200 g / L</td>
<td>L-glutamine: amino acid and energy source</td><td>RM-071</td><td>0.876 g / kg</td><td>0.584 g / kg</td><td>NA</td><td>0.584 g / kg</td><td>0.292 g / kg</td><td>0.292 g / kg</td><td>0.292 g / kg</td>
<td>Sodium bicarbonate: buffer: C02-pH regulator</td><td>RM-077</td><td>1.60 g / kg</td><td>1.60 g / kg</td><td>NA</td><td>1.6 g / kg</td><td>1.6 g / kg</td><td>1.6 g / kg</td><td>1.6 g / kg</td>
<td>HEPES: organic buffer</td><td>RM-090</td><td>1.80 g / kg</td><td>1.80 g / kg</td><td>NA</td><td>1.8 g / kg</td><td>NA</td><td>NA</td><td>NA</td>
<td>MaCI (salt): osmolarity regulator</td><td>RM-174</td><td>2,675 g / kg</td><td>2.45 g / kg</td><td>NA</td><td>2.45 g / kg</td><td>NA</td><td>NA</td><td>NA</td>
<td>MaH2PO4-H2O: phosphate buffer</td><td>RM-200</td><td>0.031 g / kg</td><td>0.031 g / kg</td><td>NA</td><td>0.031 g / kg</td><td>NA</td><td>NA</td><td>NA</td>
<img file="MX353340B_D0147.tif" />
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<td rowspan="2">Na2HPO<sub>4</sub>H2O: phosphate buffer</td><td rowspan="2">RM-233</td><td rowspan="2">0.436 g / kg</td><td rowspan="2">0.436 g / kg</td><td rowspan="2">NA</td><td>0.436 g / kg</td><td>NA</td><td>NA</td><td>NA</td>
<td></td><td></td><td></td><td></td>
<td>Bacto TC Yeastolate: hydrolyzed yeast source</td><td>RM-216</td><td>4.0 g / kg</td><td>10.7 g / kg</td><td>65.0 g / kg</td><td>10.7 g / kg</td><td>2 g / kg</td><td>11 g / kg</td><td>8 g / kg</td>
<td>Peptone Phytone: hydrolyzed plant soy source</td><td>RM-238</td><td>2,579 g / kg</td><td>6.92 g / kg</td><td>41.0 g / kg</td><td>6.92 g / kg</td><td>NA</td><td>NA</td><td>NA</td>
<td>Oreos Components</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>
<td>Pluronic F-68 (Poloxámera 188 NF): surfactant, vehicle</td><td>RM-188</td><td>1.00 g / kg</td><td>1.00 g / kg</td><td>NA</td><td>1.0 mL / kg</td><td>NA</td><td>NA</td><td>NA</td>
<td>L-asparagine monohydrate: amino acid</td><td>RM-284</td><td>0.450 g / kg</td><td>NA</td><td>5.0 g / kg</td><td>NA</td><td>NA</td><td>NA</td><td>NA</td>
<td>Primatote: hydrolyzed animal source-Res</td><td>RM-149</td><td>NA</td><td>NA</td><td>NA</td><td>NA</td><td>NA</td><td>NA</td><td>NA</td>
<td>Methotrexate: Selective in the DHFR CHO Amplification System</td><td>SR-133</td><td>0.250 mL / kg</td><td>NA</td><td>NA</td><td>NA</td><td>0.250 mL / kg</td><td>0.250 mL / kg</td><td>0.250 mL / kg</td>
<td>2N NaOH: Base</td><td>SR-288</td><td>3.50 mL / kg</td><td>5.67 mL / kg</td><td>As necessary</td><td>5.67 mL / kg</td><td>As necessary</td><td>As necessary</td><td>As necessary</td>
<td>HCI2N: Acid</td><td>SR-287</td><td>2.91 mL / kg</td><td>2.5 mL / kg</td><td>As necessary</td><td>2.5 mL / kg</td><td>As necessary</td><td>As necessary</td><td>As necessary</td>
With respect to the modified salt-free basal medium with a reduced vitamin content previously mentioned, the amount of vitamins was reduced by a third in relation to the unmodified basal medium, previously described as RM-003, or the free modified basal medium of salt, previously described as RM230. Thus, a basal medium with reduced vitamin content, as described above, has a third of the amount of vitamins as the RM-003 and RM-230 media. When used in the amounts given in the table above, the
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<img file="MX353340B_D0148.tif" />
final concentration of vitamins in
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MEXICAN INSTITUTE M LA PROPBOAU C .. INDUSTRIAL. 'means was reduced to a third, in contrast to what was υίίΙΐΖΤΤΈΤΓΙΌ ^' ΊτΓθΒϊδβ'RM003 or RM-230. However, it should be noted that, if necessary, media production and feed can also be used using RM-230.
Example 1.4: Composition of Media to Grow CHO Cells Expressing Antibodies Against IL-18 and EPO / R
Table 4 provides a summary of the growth and production media used to express antiIL18 and anti-EPO / R antibodies. Additional details regarding the means to express these antibodies can be found in Table 5 (anti-IL-18) and Table 6 (anti-EPO / R).
Table 4: Medium for culturing CHO cells expressing complete human anti-IL18 and anti-EPO / R antibodies
<td>Components of the Medium</td><td rowspan="2">Raw Material Specification #</td><td>Anti-IL-18 2XP</td><td>Anti-IL-18 3ΧΡ</td><td>Anti-IL-18 4XP</td><td>anti-EPO-R 1XP</td><td>anti-EPO-R 3XP</td>
<td>Component List: JRH Part A and Part B</td><td>SR-371 growth</td><td>SR-372 production</td><td>SR-382 production</td><td>SR-274 growth</td><td>SR-286 production</td>
<td>ABC components added</td><td>Final pH:</td><td> 7.0 ±0.1</td><td> 6.9 ± 0.05</td><td> 7.0 ± 1.0</td><td> 7.2 ±0.1</td><td> 7.2 ±0.1</td>
<td></td><td>Final osmolarity:</td><td> 280-300</td><td> 373-403</td><td> 360-400</td><td> 280-320</td><td> 370-390</td>
<td>Part A: UnmodifiedOrigin - Commercially Available</td><td>RM-003</td><td>NA</td><td>NA</td><td>NA</td><td> 16.45</td><td>NA</td>
<td>Part A special (modified): salt free</td><td>RM-230</td><td>5.26 g / kg</td><td>7.89 g / kg</td><td>10.52 g / kg</td><td>NA</td><td>7.89 g / kg</td>
<td>Part B: ferric citrate: source of chelated iron</td><td>RM-004</td><td>10 mL / kg</td><td>10 mL / kg</td><td>10 mL / kg</td><td>10 mL / kg</td><td>10 mL / kg</td>
<td>Part C:</td><td></td><td></td><td></td><td></td><td></td><td></td>
<td>Recombinant Human Insulin: Recombinant Glucose Protein Regulator</td><td>SR-055</td><td>3.88 mL / kg (8 mg / kg)</td><td>6.0 mL / kg (12 mg / kg)</td><td>6.5 mL / kg (12 mg / kg)</td><td>2.0 mL / kg (4 mg / kg)</td><td>6.0 mL / kg (12 mg / kg)</td>
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<td rowspan="2">Anhydrous glucose: carbon source</td><td rowspan="2">RM-011</td><td rowspan="2">7.0 g / kg</td><td rowspan="2">7.0 g / kg</td><td>7.0 g / kg</td><td>1.5 g / kg</td><td>7.0 g / kg</td>
<td></td><td></td><td></td>
<td>L-glutamine: amino acid and energy source</td><td>RM-071</td><td>0.876 g / kg</td><td>0.584 g / kg</td><td>0.584 g / kg</td><td>0.292 g / kg</td><td>0.584 g / kg</td>
<td>Sodium bicarbonate: buffer: CO regulator<sub>2</sub>-pH</td><td>RM-077</td><td>1.6 g / kg</td><td>1.6 g / kg</td><td>1.6 g / kg</td><td>1-6 g / kg</td><td>1.6 g / kg</td>
<td>HEPES: organic buffer</td><td>RM-090</td><td>1.8 g / kg</td><td>1.8 g / kg</td><td>1.8 g / kg</td><td>NA</td><td>1.8 g / kg</td>
<td>NaCI (salt): osmolarity regulator</td><td>RM-174</td><td>2.67 g / kg</td><td>2.45 g / kg</td><td>2.45 g / kg</td><td>Part A: 6.5 g / kg</td><td>2.45 g / kg</td>
<td>NaH2PO4 «H2O: faith damper</td><td>RM-200</td><td>0.031 g / kg</td><td>0.031 g / kg</td><td>0.031 g / kg</td><td>Part A: 0.031 g / kg</td><td>0.031 g / kg</td>
<td>Na2HPO<sub>4</sub>«H2O: phosphate buffer</td><td>RM-233</td><td>0.436 g / kg</td><td>0.436 g / kg</td><td>0.436 g / kg</td><td>Part A: 0.436 g / kg</td><td>0.436 g / kg</td>
<td>Bacto TC Yeastolate: yeast</td><td>RM-216</td><td>4.0 g / kg</td><td>10.7 g / kg</td><td>14.27 g / kg</td><td>2.0 g / kg</td><td>10.7 g / kg</td>
The CHO cell line expressing IL-18 was grown in 2xP culture medium (SR-371), and the antibody was subsequently produced in 3xP production medium (SR-372), for a final titer of approximately 1 g / L. The high titer process used 4xP (SR-382) as the production medium, to achieve a final titer of approximately 2 g / L. The production medium used for the production of anti-EPO / R, was identical to SR-286, but a 1xP medium (SR-274) was used for cell growth. All means are described in Tables 4 and 5.
Example 1.5: Cell Culture Processes to Produce Antibodies in Mammalian Cells
The medium described above was also developed on two production platforms used in two projects to cultivate mammalian cells, for example CHO cells. The first<sub>141</sub> IMPI
PE IA «OHS'JAD U>« a »aeLíSr iNOLrtTWAL platform was developed using the composition of-me ^ Uo-eimíla-r o · - that described in the modified production medium described in Tables 2-4 above, with the only difference from a different temperature used for cell growth. This platform was used for the production of the anti-IL18 antibody, as well as for the production of the antibody against the erythropoietin receptor (antiEPO / R). The second media platform further strengthened the nutritional components, and was used for the production of high titers of the anti-IL-18 antibody, to achieve higher volumetric antibody productivity.
All antibodies, including anti-IL-12, anti-IL-18, and anti-EPO / R, were complete human IgG1 antibodies expressed by dhfr (-) transfected CHO cell lines, as previously described. These cell lines were grown in suspension and without the aid of a bovine serum source or other animal materials.
To produce anti-IL 18 antibodies, the CHO cell line expressing anti-IL-18 was grown in a growth medium, referred to herein as SR-371. SR-371 medium was used to support high cell productivity, with moderate cell growth. Once the cell density reached the transfer criteria, the cells were transferred to the production medium (SR-372), to start the production stage.
<img file="MX353340B_D0149.tif" />
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Table 5: Cultivm6Trtft ~! * Iuuusu A Anti-IL-18 Media Compositions
SR-371 growth medium was used in the training and seeding reactors. SR-372 production medium was used in the 3000 liter production bioreactor.
<td>Component</td><td>Source of Increase SR-371</td><td>Production Medium SR-372</td>
<td>PFCHO Part A, special salt-free formulation</td><td>5.26 g / L</td><td>7.89 g / L</td>
<td>PFCHO Part B (conc. Ferric citrate solution)</td><td>10 mL / L</td><td>10 mL / L</td>
<td>Recombinant human insulin</td><td>7.76 mg / L</td><td>13 mg / L</td>
<td>Anhydrous dextrose</td><td>7.0 g / L</td><td>7.0 g / L</td>
<td>L-glutamine</td><td>0.876 g / L</td><td>0.584 g / L</td>
<td>Sodium bicarbonate</td><td>1.6 g / L</td><td>1.6 g / L</td>
<td>HEPES</td><td>1.8 g / L</td><td>1.8 g / L</td>
<td>NaCI</td><td>2.67 g / L</td><td>2.45 g / L</td>
<td>Pluronic F-68 (Poloxamer 188 NF)</td><td>1.0 g / L</td><td>1.0 g / L</td>
<td>NaH<sub>2</sub>PO<sub>4</sub>H<sub>2</sub>OR</td><td>0.031 g / L</td><td>0.031 g / L</td>
<td>Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR</td><td>0.436 g / L</td><td>0.436 g / L</td>
<td>Bacto TC Yeastolate</td><td>4.0 g / L</td><td>10.7 g / L</td>
<td>Peptona Phytone</td><td>2,579 g / L</td><td>6.92 g / L</td>
<td>2mM Methotrexate</td><td>0.05 mL / L</td><td>0.05 mL / L</td>
<td>2N NaOH</td><td>3.5 mL / L</td><td>5.67 mL / L</td>
<td>HCI 2N</td><td>2.91 g / L</td><td>2.5 g / L</td>
<td>final pH</td><td> 7.10-7.20</td><td> 7.10-7.20</td>
<td>Final osmolarity (mOsm / kg)</td><td> 373-403</td><td> 373-403</td>
The temperature was maintained at 35 ° C during cultivation. An additional 4 g / L of glucose was added, when the glucose level
<img file="MX353340B_D0150.tif" />
<img file="MX353340B_D0151.tif" />
INSTtTVTX? MÍXICANO DI LA rtOttWAO
143 cell culture was below —---—---- A similar process was also employed for the production of the anti-EPO / R antibody. However, this medium (SR-274) was used for cell growth at seeding. The SR-286 medium, which is the same used for the Humira production, was used in the production stage of the anti-EPO / R antibody (Table 6). SR-274 growth medium was used in the training and seeding reactors. SR-286 production medium was used in the 3000 liter production bioreactor.
Table 6: Compositions of culture media in the antiEPO / R process
<td>Component</td><td>Growth medium SR-274</td><td>Production Medium SR-286</td>
<td>PFCHO Part A, RM-003</td><td>16.45 g / kg</td><td>N7A</td>
<td>PFCHO Part A, RM-230 (salt free)</td><td>N / A</td><td>7.89 g / kg</td>
<td>PFCHO Part B (conc. Solution of ferric citrate)</td><td>10 mL / kg</td><td>10 mL / kg</td>
<td>Recombinant human insulin</td><td>4 mg / kg</td><td>13 mg / kg</td>
<td>Anhydrous dextrose</td><td>1.5 g / kg</td><td>7.0 g / kg</td>
<td>L-glutamine</td><td>0.292 g / kg</td><td>0.584 g / kg</td>
<td>Sodium bicarbonate</td><td>1.6 g / kg</td><td>1 6 g / kg</td>
<td>HEPES</td><td>N / A</td><td>1.8 g / kg</td>
<td>NaCI</td><td>N / A</td><td>2.45 g / kg</td>
<td>Pluronic F-68 (Poloxamer 188 NF)</td><td>N / A</td><td>1-0 g / kg</td>
<td>NaH<sub>2</sub>PO<sub>4</sub>H<sub>2</sub>OR</td><td>N / A</td><td>0.031 g / kg</td>
<td>Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR</td><td>N / A</td><td>0.436 g / kg</td>
<td>Bacto TC Yeastolate</td><td>2.0 g / kg</td><td>10.7 g / kg</td>
<td>Peptona Phytone</td><td>N / A</td><td>6.92 g / kg</td>
<img file="MX353340B_D0152.tif" />
<img file="MX353340B_D0153.tif" />
144
<td>2mM Methotrexate</td><td>0.25 mL / kg</td><td>N / A</td>
<td>2N NaOH</td><td>As needed</td><td>5.67 mL / kg</td>
<td>HCI 2N</td><td>As needed</td><td>2.5 mL / kg</td>
<td>final pH</td><td> 7.20 ± 0.10</td><td> 7.15 ± 0.05</td>
<td>Final osmolarity (mOsm / kg)</td><td> 320 ± 20</td><td> 388 + 15</td>
SR-286 and SR-372 production media consisted of media components similar to those listed in Tables 5 and 6, but with different MTX levels (0 nM for the SR-286 and 100 nM for the SR-372 ).
An improved process for the production of anti-IL-18 was developed to obtain higher productivity. This new process, called Process B, introduced a new means to extend the longevity of cell culture and increase the volumetric productivity of antibodies. The production medium (SR-382) was different from the previous production means in the amount of nutrients used in the production stage. The complete composition of SR-382 medium is described in Table 7. In the new process for the production of anti-IL-18, although the cells were still cultured in SR-371 medium during the seeding stage, the SR-372 medium was used in the one-stage seeding bioreactor before the stage of production. The cells were then grown in SR-382 medium in the production stage, with a temperature change of 35 to 33 ° C, to prolong the longevity of the cell culture and therefore extend the effects of the SR145 medium.
<img file="MX353340B_D0154.tif" />
382 on cells.
The growth medium SR-Í37Í was used in shake flasks, Wave bag, and the 100 liter seed bioreactor. Low fill SR-372 medium was used in the initial 575 liter culture stage in the 3000 liter production bioreactor. SR-382 production medium was used in the 3000 liter production bioreactor only.
Table 7: Composition of the culture media in Process B anti-IL-18
<td>Component</td><td>Growth medium SR-274</td><td>Production Medium SR-286</td><td>Production Medium SR-382</td>
<td>PFCHO Part A, special salt-free formulation</td><td>5.26 g / L</td><td>7.89 g / L</td><td>10.52 g / L</td>
<td>PFCHO Part B (conc. Solution of ferric citrate)</td><td>10 mL / L</td><td>10 mL / L</td><td>10 mL / L</td>
<td>Recombinant human insulin</td><td>7.76 mg / L</td><td>13 mg / L</td><td>13 mL / L</td>
<td>Anhydrous dextrose</td><td>7.0 g / L</td><td>7.0 g / L</td><td>7.0 g / L</td>
<td>L-glutamine</td><td>0.876 g / L</td><td>0.584 g / L</td><td>0.584 g / L</td>
<td>Sodium bicarbonate</td><td>1.6 g / L</td><td>1.6 g / L</td><td>1.6 g / L</td>
<td>HEPES</td><td>1.8 g / L</td><td>1.8 g / L</td><td>1.8 g / L</td>
<td>NaCI</td><td>2.67 g / L</td><td>2.45 g / L</td><td>0 g / L</td>
<td>Pluronic F-68 (Poloxamer 188 NF)</td><td>1.0 g / L</td><td>1.0 g / L</td><td>1.0 g / L</td>
<td>NaH<sub>2</sub>PO<sub>4</sub>H<sub>2</sub>OR</td><td>0.031 g / L</td><td>0 031 g / L</td><td>0.031 g / L</td>
<td>Na<sub>2</sub>HPO<sub>4</sub>-7H<sub>2</sub>OR</td><td>0.436 g / L</td><td>0.436-g / L</td><td>0.436 g / L</td>
<td>Bacto TC Yeastolate</td><td>4.0 g / L</td><td>10.7 g / L</td><td>14.27 g / L</td>
<img file="MX353340B_D0155.tif" />
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<img file="MX353340B_D0156.tif" />
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INWSTWAL
<td rowspan="2">Component</td><td rowspan="2">Source of Increase SR-274</td><td rowspan="2">Source of Production SR-286</td><td>Source of</td>
<td>Production SR-382</td>
<td>Peptona Phytone</td><td>2,579 g / L</td><td>6.92 g / L</td><td>9.23 g / L</td>
<td>2mM Methotrexate</td><td>0.05 mL / L</td><td>0.05 mL / L</td><td>0.05 mL / L</td>
<td>2N NaOH</td><td>3.5 mL / L</td><td>5.67 mL / L</td><td>8.95 mL / L</td>
<td>HCI 2N</td><td>2.91 g / L</td><td>2.5 mL / L</td><td>4.1 mL / Kg</td>
<td>final pH</td><td> 7.1 - 7.2</td><td> 7.1 - 7.2</td><td> 7.1 - 7.2</td>
<td>Final osmolarity (mOsm / kg)</td><td> 373 - 403</td><td> 373 - 403</td><td> 373 - 403</td>
1Q Nutrients were enriched in the following medium to provide additional energy sources and building components for CHO cell growth and antibody production. In process B, although cells were still cultured in SR-371 medium during the training stage, SR-372 medium was used in seeding the single-stage bioreactor prior to the production stage. The cells were then cultured in SR-382 medium in the production stage, with a temperature change of 35 to 32 ° C, to prolong the longevity of the cell culture and therefore extend the effects of the SR-382 medium on the 2q cells.
Process A: Performance of Anti-IL-18 Cells and AntiEPO / R Cells in SR-372 Medium and SR-286 Medium
Cells expressing anti-IL18 antibody were cultured in SR-371 medium, with 100 nM MTX, to accumulate cell mass 25 for the production step. SR-371 medium was used to
147 shows a growth profile of
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INDUSTRIAL - support moderate cellular productivity. The Table representative production of CHO cells producing anti-IL-18, in the production bioreactor of 3000 L. Using this process (Process A) with SR-372 medium, a final titer of up to 1 g / L was obtained.
Table 8: Production of Anti-IL-18 Antibody in Medium 372 (Process A)
<td>Measurable Outcomes</td><td>Scale Process Pilot (n = 5) Temp = 35 ° C</td><td>Process at 3000 L (n = 6) Temp = 35 ° C</td>
<td>Maximum Cell Density [10<sup>6</sup> viable cells / mL]</td><td> 8.68</td><td> 9.2</td>
<td>Duration up to 50% of viability [Days]</td><td> 11</td><td> 11</td>
<td>Cell Specific Productivity [pg / cell-day]</td><td> 20.5</td><td> 17.6</td>
<td>Volumetric Productivity Until Harvest @ 50% viability [mg / L-day]</td><td> 98.8</td><td> 81.8</td>
<td>Title @ 50% viability [mg / L]</td><td> 1004</td><td> 900</td>
<img file="MX353340B_D0157.tif" />
148
Medium 286, which shares the same formulation as medium 372, except for the concentration of MTX, was used for the production of anti-EPO / R. Although normally a lower cell density is obtained in the production stage, a higher productivity was achieved, to enable the cells to produce up to 1.8 g / L of antibody at 3000 L scale, using SR-286 medium as production. Reasonable cell growth was observed, as summarized in Table 9. Pilot scale results, as well as 3000 L scale results, demonstrated that this medium increased cell specific productivity and a final titer of up to 1.9 g / L was observed. These results demonstrate that media with similar formulation (SR-372 and SR-286 in Tables 1 and 2), support good cell growth and high antibody production, in large-scale CHO cell cultures.
Table 9: Production of anti-EPO / R antibody in medium 286
<td>Measurable Outcomes</td><td>Pilot Scale Process (n = 5) Temp = 35 ° C</td><td>Process at 3000 L (n = 6) Temp = 35 ° C</td>
<td>Maximum Cell Density [10<sup>6</sup> viable cells / mL]</td><td> 8.68</td><td> 9.2</td>
<td>Duration up to 50% of viability [Days]</td><td> 11</td><td> 11</td>
<td>Specific Productivity of Cells</td><td> 20.5</td><td> 17.6</td>
<img file="MX353340B_D0158.tif" />
<img file="MX353340B_D0159.tif" />
149
<td rowspan="2">Measurable Outcomes</td><td rowspan="2">Process a Pilot (n = 5) Temp = 35 ° C</td><td rowspan="2">Scale</td><td></td>
<td>(n = 6) Temp = 35 ° C</td>
<td>[pg / cell-day]</td><td colspan="2"></td><td></td>
<td>Volumetric Productivity Until Harvest @ 50% viability [mg / L-day]</td><td colspan="2"> 98.8</td><td> 81.8</td>
<td>Title @ 50% viability [mg / L]</td><td colspan="2"> 1004</td><td> 900</td>
Process B: Performance of Anti-IL 18 Cells in Process B with SR-382 Medium
The SR-382 medium was the most enriched that was used in the extended batch process for the production of the anti-IL-18 antibody. Process B includes the use of SR-371 medium in the training stage and SR-372 in the seeding bioreactor before the production stage, or the low-fill stage. Cell growth was moderate compared to cell growth in SR-372 medium, in the production stage. However, with the change in temperature, a final titer of up to 2.5 g / L was obtained, using SR-382 medium.
SR-382 medium was developed based on the study that showed that the specific activity of cells expressing anti-IL18 increased proportionally with the increase of 25 nutrients in the production medium. SR-382 medium was the medium
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<img file="MX353340B_D0160.tif" />
optimal that provided the balance between cell growth and increase in the final titer. Although the maximum cell density only reached 5.9χ10<sup>6</sup> cells / mL, cell specific productivity was increased by a factor of two. Combination with temperature change to prolong the duration of cell culture, caused a titer of up to 2.2 g / L to be achieved, as shown in
Table 10.
Table 10: Production of anti-IL18 antibody in SR-382 medium (Process B)
<td>Measurable Outcomes</td><td>Scale Process Pilot (n = 1) Temp = 35-33 ° C</td><td>Process at 3000 L (n = 1) Temp = 35-33 ° C</td>
<td>Maximum Cell Density [10<sup>6</sup> viable cells / mL]</td><td> 7.85</td><td> 5.90</td>
<td>Duration up to 50% of viability [Days]</td><td> 12</td><td> 13</td>
<td>Cell Specific Productivity [pg / cell-day]</td><td> 32.0</td><td> 42.1</td>
<td>Volumetric Productivity Until Harvest @ 50% viability [mg / L-day]</td><td> 181.1</td><td> 191.8</td>
<td>Title @ 50% viability</td><td> 2173</td><td> 2110</td>
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<td>Medial Results</td><td>Scale Process Pilot (n = 1) Temp = 35-33 ° C</td><td>Process 3UUÜ L (n = 1) Temp = 35-33 ° C</td>
<td>[mg / L]</td><td></td><td></td>
EXAMPLE 2: Improved Feeding Batch Process and Feeding Solutions for Antibody Expression
Analysis of the spent medium from the bioreactors operating in the batch mode, showed the depletion of certain amino acids. This result also suggested the depletion 10 of other components of the medium, even if not measured, which could cause additional deficiencies in nutrition. In order to compensate for these potential deficiencies, nutrient solutions were added. In the engineering field, this approach is generally referred to as feed-batch.
From an operational point of view, it is convenient to use concentrated feeding solutions. The following examples describe the addition of highly concentrated solutions of the chemically defined basal medium (PFCHO, Catalog # 67411-50L) and complex hydrolyzates, for example yeastolate and phytone. This pair of hydrolyzates was determined to exhibit a synergistic effect on increased productivity, related to its concentration ratio.
Example 2.1: Adalimumab Batch Feeding Process
The initial adalimumab (Humira / D2E7) process consisted of a 3-day process in which the medium was removed and filled
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<img file="MX353340B_D0161.tif" />
152 eight consecutive times. An improved pnr int ^ Q feeding process was developed by replacing the hydrolyzate in the medium
Primatone by the hydrolyzed Yeastolate and using new parameters in the reactor. The improved batch feeding process lasted approximately 12 days.
The productivity of the initial batch process was further improved by reformulating the basal medium, PFCHO, and adding a new hydrolyzate, eg Phytone. This hydrolyzate containing medium formulation was used in the process referred to above as SR-286 (see Table 2). The reactor operating parameters were also investigated, which resulted in the identification of an optimal temperature to run the entire adalimumab production process.
Analysis of samples taken daily from the reactor experiments highlighted some potential nutritional deficiencies. In the case of the adalimumab batch process, the potential nutritional deficiency was corrected by feeding a 25x concentrated PFCHO solution and a 33x solution of the yeastolate and phytone hydrolyzates. Hydrolyzates are complex components that exhibit a synergistic effect related to their concentration ratio. This ratio was maintained in a highly concentrated 33x version.
Experimental Plan
The goal of the experiment was to compare the new batch feeding process to the two control batch process (change of
<img file="MX353340B_D0162.tif" />
<img file="MX353340B_D0163.tif" />
153 temperature of 37-> 33 ° C vs. constant temperature at 35 ° C).
<img file="MX353340B_D0164.tif" />
The batch feed modifications were:
one. 25x basal medium enrichment (PFCHO solution), fed based on amino acid deficiencies.
2. 33x hydrolyzate enrichment solution fed at intervals such that the osmolarity of the medium never exceeds 440 mOsm (condition that results in a reduction in cell growth and viability).
3. The reactor temperature set at 35 ° C throughout the process.
Controls for this experiment were.
a) An identical reactor operating with the current means (SR-286) and under the parameters of the control batch process (the control conditions included reactors operating with the medium
SR-286, with a change in temperature and a linear increase in pH), designated as control # 1; and
b) an identical reactor operating with the current medium (SR286) and under all the parameters of the current batch processes, except for the operating temperature of 35 ° C throughout the process, designated as control # 2.
materials
Braun ED reactors with a working volume of 13 L Pilot Plant Inoculum AFI915A using the
WCB970513-6 Work Cells
3XP11Y7P Basal Medium Solution (SR-286)
<img file="MX353340B_D0165.tif" />
MaHío Basal Enrichment Solution (25x) (PF CHO solution)
Hydrolyzate Enrichment Solution (33x)
Glucose feeding (200 g / L) (glucose solution)
0.5N sodium hydroxide solution, for pH control
Solution Preparation
one. Production Medium (see SR-286 Solution Record described above in Table 2)
2. 2 kg of PFCHO Enrichment Solution (25x) (basal enrichment solution):
Prepared in the following order, under constant agitation and allowing to mix for 10 minutes before each addition:
<td>Component</td><td>Mass [g]</td><td>Notes</td>
<td>H<sub>2</sub>Or MilliQ</td><td> 1500</td><td></td>
<td>PFCHO</td><td> 131.5</td><td></td>
<td>NaOH 10N</td><td>49 mL</td><td>Up to pH 10</td>
<td>Asparagine</td><td> 15</td><td>the pH would drop to -9.73</td>
<td>Glucose</td><td> 100</td><td>pH would drop to -9.71</td>
<td>H<sub>2</sub>Or MilliQ</td><td>As required</td><td>Bring the weight up to 2000 g, pH -9.70 and osmolarity -1480 mOsm</td>
<td colspan="3">Filter through a 0.2 pm PES membrane filter Store at 4 ° C</td>
<td colspan="3">In each addition of 1% of the initial volume of the previous solution, the following will be increased:</td>
155
<img file="MX353340B_D0166.tif" />
<img file="MX353340B_D0167.tif" />
a) PFCHO concentration at 0.25x compared to original 3x concentration
b) asparagine at 75 mg / L
c) glucose concentration in 0.5 g / L
d) osmolarity at 10 mOsm
e) pH in -0.10 pH units
3. 1 kg of Hydrolyzate Enrichment Solution (33x):
Prepared in the following order, under constant agitation and allowing to mix for 10 minutes after each addition:
<td>Component</td><td>Mass [g]</td><td>Notes</td>
<td>H<sub>2</sub>Or MilliQ</td><td> 500</td><td></td>
<td>Yeastolate TC</td><td> 265</td><td></td>
<td>Peptona Phytone</td><td> 165</td><td></td>
<td>H<sub>2</sub>Or MilliQ</td><td>As required</td><td>Bring the weight up 1000 g</td>
<td colspan="3">Filter through a 0.2 pm PES membrane filter Store at 4 ° C</td>
<td colspan="3">Note: Each addition of 1% of the initial volume of the previous solution will increase the following: a) Yeastolate TC concentration at 2.65 g / L (0.33x), compared to the original batch concentration. b) the Phytone peptone concentration at 1.65 g / L (0.33x), compared to the original batch concentration.</td>
Methods
Reactor operation:
To inoculate the reactor, a flask was thawed and
<img file="MX353340B_D0168.tif" />
<img file="MX353340B_D0169.tif" />
156 expanded following process description 4® - sio <nbra Httmira. · After growth in the reactor, it was drained to 3.62 L, to simulate the low-fill stage. Thereafter, the reactor was increased to the 13 L level with production medium (SR-286).
The reactors were operated with the following parameters:
a) Agitation, 70 rpm
b) Temperature, 35 ° C
c) Linear decrease in pH starting at pH 7.16 until pH
6.90, in a 72 hour period
d) Dissolved oxygen, 30%
e) The reactors were fed with 195 g of a glucose solution at 200 g / L, when the glucose level decreased to less than 2.0 g / L
Feeding Program
The feeding schedule for adding additional nutrients, for example supplemental basal medium and hydrolyzates to the adalimumab batch, is depicted below.
Table 11: Feeding schedule for the adalimumab batch feeding process
<td rowspan="2">Day</td><td colspan="2">Amounts Fed [g]</td>
<td>PFCHO 25x</td><td>Hydrolyzed 33x</td>
<td> 0-3</td><td></td><td></td>
<td> 4</td><td> 130</td><td> 130</td>
<td> 5</td><td></td><td></td>
<td> 6</td><td> 260</td><td></td>
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<img file="MX353340B_D0170.tif" />
<img file="MX353340B_D0171.tif" />
<td rowspan="2">Day</td><td colspan="2">Amounts Fed [g]</td>
<td>PFCHO 25x</td><td>Hydrolyzed 33x</td>
<td> 7</td><td></td><td>130, glucose</td>
<td> 8</td><td></td><td></td>
<td> 9</td><td>260, glucose</td><td></td>
<td> 10</td><td> 260</td><td></td>
<td> 11</td><td> 130</td><td></td>
<td> 12-13</td><td></td><td></td>
Results:
Results (as well as projected improvements) compared control processes # 1 and # 2 with the improved batch feeding process, described in Tables 12 and 13. As shown in Table 12, the productivity of adalimumab it was increased with the addition of improved fortified basal medium and hydrolyzate fortification solution, using the improved batch feeding process, at constant temperature.
Table 12: Comparison of batch feeding processes for adalimumab
<td>Results Measurable</td><td>Control # 1 (Process 3000L) Temp. = 37 ° C 1 33 ° C</td><td>Control # 2 (Process 3000L) Temp. = 35 ° C</td><td>Batch Feeding Experiment Temp. = 35 ° C</td>
<td>Maximum Cell Density [10<sup>6</sup> viable cells / mL]</td><td> 3.63</td><td> 4.45</td><td> 4.41</td>
<img file="MX353340B_D0172.tif" />
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<td>Results Measurable</td><td>Control # 1 (Process 3000L) Temp. = 37 ° C 1 33 ° C</td><td>Control # 2 (Process 3000L) Temp. = 35 ° C</td><td>Batch Feeding Experiment Temp. = 35 ° C</td><td></td>
<td>Duration up to 50% of viability [Days]</td><td> 13</td><td> 10</td><td> 12</td><td></td>
<td>Cell Specific Productivity [pg / cell-day]</td><td> 42.5</td><td> 46.7</td><td> 61.4</td><td></td>
<td>Volumetric Productivity Until Harvest @ 50% viability [mg / L-day]</td><td> 98</td><td> 114</td><td> 163</td><td></td>
<td>Title @ 50% viability [mg / L]</td><td> 1322</td><td> 1178</td><td> 1979</td><td></td>
Table 13: Comparison of Projected Results Using Adalimumab Batch Feeding Processes
<td>Projected Result</td><td>Control # 1 (Process 3000L) Temp. = 37 ° C | 33 ° C</td><td>Control # 2 (Process 3000L) Temp. = 35 ° C</td><td>Batch Feeding Experiment Temp. = 35 ° C</td>
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<td>Harvests Annuals [Allowing 3 days of recovery]</td><td> 22</td><td> 28 _</td><td>—Open · »». * ·· »</td>
<td>Annual Product Yield [Based on harvests of 2600 L)</td><td> 75.6</td><td> 85.7</td><td> 123.4</td>
<td>Annual Yield Increase (control = 100%)</td><td> 100%</td><td> 114%</td><td> 163%</td>
Example 2.2: ABT-874 Batch Feeding Process
As in the case of the aforementioned improved batch feeding process for adalimumab, analysis of the samples taken daily from the ABT-874 reactor operating in the batch mode highlighted amino acid depletion. Once again, this deficiency was corrected using a 25x PFCHO solution and a 33x concentrated hydrolyzate solution.
The AVT-874 batch process was originally developed for D2E7 (adalimumab), replacing the hydrolyzate in the media and introducing new parameters into the reactor. In addition, as in the case of D2E7 (adalimumab), the media
<img file="MX353340B_D0173.tif" />
<sub>160</sub> IMPI
ΠΤΠΊΤυΤΟ MEXICAN
OF THE PROPERTY
INDUSTRIAL basal areas were reformulated and a new hydrolyzate was added. This media formulation was used in the current D2E7 process as SR-286 (see Table 2 above).
Experimental Plan
The goal of the experiment was to compare a control batch process with the following batch feeding conditions, both starting at the time the previously identified amino acids were depleted:
<td>to)</td><td>They fed</td><td>alternatively</td><td>solution</td><td>of</td>
<td>enrichment</td><td>basal medium</td><td>PFCHO 25x and</td><td>solution</td><td>of</td>
<td colspan="2">hydrolyzate enrichment 33x</td><td></td><td></td><td></td>
<td>b)</td><td>They fed</td><td>daily the</td><td>solution</td><td>of</td>
<td>enrichment</td><td>basal medium</td><td>PFCHO 25x and the</td><td>solution</td><td>of</td>
<td colspan="2">hydrolyzate enrichment 33x</td><td></td><td></td><td></td>
The control for this experiment included an identical reactor operating with current media (SR-286) and under the parameters of the control batch process (SR-286 medium, with a change in temperature and a linear decrease in pH).
materials
Braun ED reactors with a working volume of 13 L
Work Cell Bank W990107-J695
3XP11Y7P Basal Medium Solution (SR-286-111899-1)
Growth Medium PFCHO-0-500-HG2Y
Basal Medium Enrichment Solution (25x)
Hydrolyzate Enrichment Solution (33x)
161
0.5N Sodium Hydroxide Solution
<img file="MX353340B_D0174.tif" />
Solution Preparation
one. Production medium (see Solution Log
SR-286)
2.
PFCHO 25x solution (basal enrichment solution: described in the previous example; with the exception that 462 g of glucose solution was used instead of powdered glucose, then being the final weight of 2170 g).
Note: With each addition of 1% of the initial volume of the previous solution, the following will be increased:
a) PFCHO concentration at 0.25x compared to original 3x concentration
b) Asparagine at 75 mg / L
c) Glucose concentration in 2.1 g / L • pH in ~ 0.10 pH units
3. Hydrolyzate Solution 33x (described in the previous example with the addition of 2.40 g / L glucose)
Note: in adding 1% of the initial volume of the previous solution, the following will be increased:
a) The Yeastolate TC concentration at 2.65 g / L (0.33x), compared to the original batch concentration.
b) The concentration of Phytone peptone at 1.65 g / L (0.33x), compared to the original concentration of the batch.
Method:
To inoculate the reactor, a flask was thawed and
<img file="MX353340B_D0175.tif" />
162 expanded following the description of the t1t process. ~ “3Ililibra ΛΒΤ · β74
After growing in the reactor, it was drained to 4.06 liters (run designation B9013-ED2 and B9014-ED3, as described in Table 13), to simulate the underfilling process. The reactor was then filled to 13 L with regular production medium (SR-286).
The reactors were operated in accordance with the following parameters:
a) Agitation, 70 rpm
b) Temperature, 33 ° C
c) pH 6.90
d) Dissolved oxygen, 40%
Table 13: Feeding Program for ABT-874
<td></td><td colspan="4">Amounts Fed [g]</td>
<td></td><td>Program of</td><td>Feeding</td><td colspan="2">Feeding Program</td>
<td></td><td>Alternative</td><td></td><td>Daily</td><td></td>
<td></td><td>Designation</td><td>of process</td><td>Designation</td><td>of process</td>
<td></td><td>B9013-ED2</td><td></td><td>B9014-ED3</td><td></td>
<td></td><td>PFCHO 25x</td><td>Hydrolyzed</td><td>PFCHO 25x</td><td>Hydrolyzed</td>
<td></td><td></td><td>33x</td><td></td><td>33x</td>
<td> 0-4</td><td></td><td></td><td></td><td></td>
<td> 5</td><td> 130</td><td></td><td> 65</td><td> 65</td>
<td> 6</td><td></td><td> 130</td><td> 65</td><td> 65</td>
<td> 7</td><td> 130</td><td></td><td> 65</td><td> 65</td>
<td> 8</td><td></td><td> 130</td><td> 65</td><td> 65</td>
<td> 9</td><td> 130</td><td></td><td> 65</td><td> 65</td>
<td> 10</td><td></td><td> 130</td><td> 65</td><td> 65</td>
<td> 11</td><td> 130</td><td></td><td> 65</td><td> 65</td>
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<td> 12</td><td></td><td> 130</td><td> 65</td><td> ---</td>
<td> 13</td><td> 130</td><td></td><td> 65</td><td> 65</td>
<td> 14-15</td><td></td><td></td><td></td><td></td>
Results
The results comparing the improved batch feeding processes are described below in Tables 14 and
15.
Table 14: Results of the batch feeding process
<td>Parameter</td><td>Control (Process 1000L) Temp. = 33 ° C</td><td>Alternative Batch Feeding Experiment Temp. = 33 ° C</td><td>Daily Batch Feeding Experiment Temp. = 33 ° C</td>
<td>Maximum Cell Density [10<sup>6</sup> viable cells / mL]</td><td> 3.79</td><td> 5.39</td><td> 4.15</td>
<td>Duration up to 50% of viability [Days]</td><td>14 to 76%</td><td> 15</td><td> 15</td>
<td>Cell Specific Productivity [pg / cell-day]</td><td> 71</td><td> 83</td><td> 82</td>
<td>Volumetric Productivity Until Harvest @ 50% of</td><td> 188</td><td> 281</td><td> 212</td>
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<td rowspan="2">viability [mg / L-day]</td><td rowspan="2"></td><td></td><td></td>
<td></td><td></td>
<td>Title @ 50% viable (mg / L]</td><td> 2505 @ 76%</td><td> 3995</td><td> 3033</td>
Table 15: Results of the batch feeding process
<td>Outcome Projected</td><td>Control (Process 1000L) Temp. = 33 ° C</td><td>Batch Feeding Experiment Alternative Temp. = 33 ° C</td><td>Daily Batch Feeding Experiment Temp. = 33 ° C</td>
<td>Harvests Annuals [Allowing 3 days of recovery]</td><td> 21</td><td> 20</td><td> 20</td>
<td>Annual Product Yield [Based on harvests of 2600 L) [kg / year]</td><td> 137</td><td> 208</td><td> 158</td>
<td>Annual Yield Increase (control = 100%)</td><td> 100%</td><td> 152%</td><td> 115%</td>
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EXAMPLE 3: Stable Combined Feeding Solutions to Increase the Volumetric Productivity of Batch-Fed Crop
The following examples describe a new approach to formulating stable highly concentrated feed solutions, including two hydrolyzates, at least one amino acid other than glutamine, one sugar, and one chemically defined base medium. The resulting feeding solutions are comparable in increasing the volumetric production of recombinant protein-producing mammalian cell lines. Finally, an accelerated method for the development of batch feeding processes was proposed, based on the control of the glucose concentration feedback.
Materials and methods
The combined feeds contained the Bacto TC yeastolate hydrolyzates, (RM-216) (BD Difeo 255771) and peptone phytone, (BD Difeo 2922450) plus glucose, L-asparagine monohydrate (Sigma-Aldrich), a reduced version of DMEM / F12 ( NaCI, phosphate salts, pH indicators, and other nonessential components were removed; Invitrogen 12500) or Ex-Cell PFCHO (A) -S1 (poorly modified) without glutamine, without NaHCO (JRH Biosciences 67411-500L35470) .
For the preparation of solutions, water was filtered using a Millipore Milli-Q PF filter, with a PMQ004D2 filter cartridge. The materials were dissolved in the specified mass of water,
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166 using a laboratory magnetic stirrer. After each component was added, complete dissolution was visually verified before the next component was incorporated.
When applicable, turbidity was quantified using a HACH 2100P portable turbidity meter (Hach Co. Loveland, CO). The human eye threshold for detecting turbidity is approximately 15 UTN (Nephelometric Turbidity Units).
The bioreactor experiments were carried out in 3 L Applikon bioreactors, at an operating volume of 1.5 L, with control of pH, temperature, agitation and oxygen, by the application of cascade air and an oxygen flow. The cell count was performed with a Cedex apparatus (Innovatis AG, Bielefeld, Germany). Glucose and lactate were determined using a YSI 2700 apparatus (YSI Inc., Yellow Springs, OH), and in some cases additional metabolites were also determined with a Nova Bioprofile 400 apparatus (Nova Biomedical Corp., Waltham, MA). The partial pressure of oxygen (pO<sub>2</sub>) at equilibrium, carbon dioxide (pCO<sub>2</sub>) and pH were verified with an ABL 5 Blood Gas Analyzer (Radiometer A / S, Copenhagen, Bronshoj, Denmark).
Example 3.1. Preparation of Combined Feeds
Stable Using PFCHO as Basal Medium
A single high-concentration feed facilitates the manufacture of cell cultures by batch feed, as it reduces the volume and number of additions required. However, this is complicated by the fact that the dust
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PFCHO must be dissolved at pH values above 9.00. Furthermore, hydrolyzates are soluble under neutral pH conditions. Thus, simply trying to mix both components at neutral or high pH values will produce suspensions of (undissolved) powders. As reported in the scientific literature, fully optimized feeds often exist in the form of two or more separate solutions that support more than one introduction rate and feed pH (eg for reasons of solubility) [1],
Combined Feed Stability Experiment
The addition of the hydrolyzates was determined to allow PFCHO concentrations to remain stable for longer periods, as described in the following table. Component amounts of 20 g / kg PFCHO, 7.5 g / kg asparagine, 21 g / kg glucose, 22 g / kg yeastolate, and 14 g / kg phytone were added in order to approximately 700 g of water and at the end water was added until reaching the final weight of 1 kg. The solutions were mixed and then brought to the target pH with 2.0N HCI. In the following table, turbidity was determined by visual observation with the naked eye.
Table 16. Effect of the final pH on different formulations of combined feeding
<td rowspan="2"></td><td>Formulation</td><td colspan="5">Final pH of the solution</td>
<td></td><td> 6.75</td><td> 7.00</td><td> 7.25</td><td> 7.50</td><td> 7.75</td>
<td> 1</td><td>PFCHO,</td><td>N / A</td><td>N / A</td><td>N / A</td><td colspan="2">They rushed by</td>
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<td rowspan="2"></td><td rowspan="2">asparagine and glucose dissolved at pH 10.0</td><td rowspan="2"></td><td rowspan="2"></td><td rowspan="2"></td><td colspan="2">full before 4</td>
<td colspan="2">hours</td>
<td> 2</td><td>The same as in (1) at PH 7.75, then add Phytone and yeastolate</td><td>N / A</td><td>N / A</td><td>Final PH of 7.3</td><td>N / A</td><td>N / A</td>
<td> 3</td><td>Same as in (2), then pH at 6.75, 7.00, 7.25 7.50, 7.75</td><td colspan="4">Slight turbidity over a period of 30-60 still, the solution remains stable</td><td>min .; and</td>
As observed in Table 16, the least turbid were 2) and 3), pH 6.75 and 7.25. Note that both formulations 2) and 3) did not become cloudy even after almost 24 hours. Based on these results, it was clear that the hydrolyzates stabilize the PFCHO in solution, since a low turbidity was achieved.
Since the hydrolyzates stabilize the resulting mixture, phytone and yeastolate could be added to the PFCHO solution, at pH 10.0; the entire mixture was then brought to the target pH. This order of addition eliminates the unstable step of maintaining the PFCHO solution at pH values less than 8.0, particularly vulnerable when mixing larger volumes.
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To test the above hypothesis, this n was tested<sup>| IAwn</sup>· Order of addition with a formulation containing 20 and 7.5 g / kg of PFCHO and asparagine, respectively. The resulting solution, X-1, was divided and brought to pH 7.0, 6.75, 6.5, and 6.25. These solutions proved to be stable, as can be seen in the following graph:
Table 17. Turbidity Profiles (UTN) of formulation X-1, at different pH values
<td></td><td colspan="4">pH</td>
<td>Time [h]</td><td> 6.25</td><td> 6.50</td><td> 6.75</td><td> 7.00</td>
<td> 2.25</td><td>n / a</td><td> 8.44</td><td> 9.86</td><td> 11.32</td>
<td> 4.00</td><td> 8.77</td><td> 7.8</td><td> 9.25</td><td> 10.70</td>
<td> 6.00</td><td> 7.02</td><td> 5.71</td><td> 6.28</td><td> 4.25</td>
After three hours, the least cloudy solution was at pH 6.50. The apparent decrease in turbidity, particularly for pH 7.0, was due to the sedimentation of some tiny particles. Glucose as a stabilizer
A formulation (see Table 18) was tested with 200 g / kg of added glucose as a stabilizer.
Table 18. Diluted D2E7 Feeding Solution
<td>H 2 Omí i li Q</td><td> 750.0</td>
<td>Glucose</td><td> 200.0</td>
<td>PFCHO</td><td> 20.0</td>
g / kg
-There was excess water
-As a potential stabilizer
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<td>NaOH 10N</td><td></td>
<td>Asparagine</td><td> 2.29</td>
<td>Yeastolate</td><td> 15.7</td>
<td>Phytone</td><td> 10.0</td>
<td>HCI 5N</td><td></td>
-> ρΗ 10.00
- »ρΗ 6.75-7.50
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This solution proved to be stable for several hours, for a range of pH values, as can be seen in the following table:
Table 19. Turbidity readings (UTN) of the combined feed as a function of time and pH
<td></td><td colspan="4">pH</td>
<td>Time [h]</td><td> 6.72</td><td> 7.00</td><td> 7.22</td><td> 7.50</td>
<td> 0.25</td><td> 3.48</td><td> 3.75</td><td> 3.95</td><td> 5.83</td>
<td> 2.50</td><td> 3.07</td><td> 3.13</td><td> 3.42</td><td> 3.74</td>
<td> 8.50</td><td> 2.98</td><td> 2.95</td><td> 2.99</td><td> 3.15</td>
The modified combined feeding solutions comprising glucose were used to express two different antibodies, that is, adalimumab (D2E7) and the anti-IL-18 antibody ABT-325.
Combination of powered solutions for stable D2E7 production
If the volume of the formulation added to the bioreactor is based on the least concentrated component (for example PFCHO),
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They would need very large amounts of feed to be added to match what has been individually assessed. Therefore, higher concentrations were the next step in the development of an effective feed formulation. This solution is called as the combined feeding solution
D2E7 and is described in the following table.
Table 20. D2E7 Combined Power Solution
<td>H2Om, IIÍQ</td><td> 750.0</td>
<td>Glucose</td><td> 150.0</td>
<td>PFCHO</td><td> 27.0</td>
<td>NaOH 10h</td><td></td>
<td>Asparagine</td><td> 3.1</td>
<td>Yeastolate</td><td> 21.2</td>
<td>Phytone</td><td> 13.5</td>
<td>HCI 5N</td><td></td>
g / kg
-> pH 10.00 ~> pH 6.75
Formulations with 200, 150 and 100 g / kg of glucose were tested. As can be seen in the following table, these solutions also had a stable turbidity for several hours.
Table 21 shows that the addition of glucose reduced the turbidity of the solution.
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Table 21. Time profiles of the tnrhiariad for «> ^ · ιι-ιi □ n dr combined feed D2E7, as a function of glucose concentration
<td></td><td colspan="3">Glucose [combined feed g / kg)</td>
<td>Time [h]</td><td> 100</td><td> 150</td><td> 200</td>
<td> 0</td><td>n / a</td><td> 9.23</td><td> 7.31</td>
<td> 1</td><td> 13.80</td><td> 8.77</td><td>n / a</td>
<td> 2</td><td> 13.20</td><td> 9.33</td><td>n / a</td>
<td> 3</td><td> 12.80</td><td> 10.30</td><td>n / a</td>
<td> 4</td><td> 12.80</td><td> 10.70</td><td> 5.98</td>
<td> 7</td><td>n / a</td><td>n / a</td><td> 6.80</td>
As shown in Table 21, increasing the glucose level decreased the turbidity of the solution. These different formulations, based on their turbidity levels, were considered as acceptable for filtration experiments.
Combined feeding solution for stable production of ABT-325
To obtain a stable ABT-325 combination feed, 50 L of the current formulation was prepared in accordance with the method used for the D2E7 combination feed, as shown in Table 22.
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Table 22. ABT-325 Combined Feeding Solution
<td>H 2O M il | ¡Q</td><td> 750.0</td>
<td>Glucose</td><td> 150.0</td>
<td>PFCHO</td><td> 21.0</td>
<td>NaOH 10N</td><td></td>
<td>Asparagine</td><td> 5.0</td>
<td>Yeastolate</td><td> 65.0</td>
<td>Phytone</td><td> 40.0</td>
<td>HCI 5N</td><td></td>
g / kg
-> pH 10.00
-> pH 6.75
After preparation, the solution maintained a turbidity level of approximately 20-30 UTN, as can be seen in the following table:
Table 23. Turbidity of the combined feed ABT-325
<td>Time [h]</td><td>Turbidity [UTNs]</td>
<td> 0.00</td><td> 41.8</td>
<td> 1.00</td><td> 28.7</td>
<td> 1.50</td><td> 19.8</td>
<td> 2.00</td><td> 20.0</td>
<td> 3.50</td><td> 14.5</td>
50 L of an ABT-325 formulation combination feed solution was prepared, in accordance with the D2E7 method, to test the scalability and applicability of the preparation method. As shown above, the solution remained
<img file="MX353340B_D0189.tif" />
174 stable for four hours.
It should be noted that the PF CHO medium referred to in the previous example corresponds to the modified PF CHO (Modified Part A), referred to in the cell culture medium of Example 1.
EXAMPLE 3.2: Preparation of Stable Combined Feeds Using DMEM-F12 as Basal Medium
As described in the previous example, it was possible to prepare a stable combined feed solution with PFCHO and two hydrolyzates, as well as glucose. The following example demonstrates that this methodology can be applied to any basal feeding formulation and produces a stable combined feeding solution.
DMEM-F12, which is a publicly available formulation medium, was modified to make it compatible with the combined feeding preparation, referred to herein as DMEMF12m. The following components were removed: NaCI, NaHCO<sub>3</sub>, NaH<sub>2</sub>PO<sub>4</sub>H<sub>2</sub>O, Na<sub>2</sub>HPO<sub>4</sub>, D-Glucose, HEPES, Na Hypoxanthine, phenol red, L-glutamine and thymidine. Combined feed solutions were prepared that matched the feed formulations D2E7 and ABT-325, in accordance with the methodology described in Examples 3.0 and 3.1. The final components and the sequence of the formulation are shown in the following table:
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Table 24. DMEM-F12 Combined Feeds
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<td></td><td>Food I</td><td>Food II</td>
<td>Μ2θΜίΙΙίΟ</td><td> 600.0</td><td></td>
<td>Glucose</td><td> 150.0</td><td> 150.0</td>
<td>DMEM-F12m</td><td> 27.0</td><td> 21.0</td>
<td>NaOH 10N</td><td></td><td></td>
<td>Asparagine</td><td> 3.1</td><td> 5.0</td>
<td>Yeastolate</td><td> 21.2</td><td> 65.0</td>
<td>Phytone</td><td> 13.5</td><td> 40.0</td>
<td>HCI 5N</td><td></td><td></td>
<td>H2Omíiiíq</td><td>Up to 1000 g</td><td></td>
g / kg
-> pH
10.00
-> pH 6.75
Once prepared, both feed solutions I and II maintained a turbidity of 12 UTN or less, for more than 4 hours.
EXAMPLE 3.3: Cell Growth and Productivity Improvement Caused by the Addition of Combined Feeding Solutions
To assess the growth and titer promoting characteristics of the above combined feeding solutions, ABT-874 cells (expressing a fully human anti-IL-12 IgG1 antibody) were used. This CHO cell line is normally grown in SR-383 cell culture medium (2X with 500 nM mtx).
For these experiments, the cells were passed as
DMEM / F12 for at least 5 generations, until adaptation was observed by a constant growth rate. The
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176 Cultures were shaken on a Thermolyne shaker plate, at 70 rpm in an incubator at 35 ° C and 5% CO<sub>2</sub>. Immediately prior to inoculation, the required amount of cell suspension was taken from the maintenance culture. The cells were centrifuged, the supernatant was discarded and the pellets were resuspended in freshly prepared and previously heated medium, to obtain a seed density of 4x10<sup>5</sup>/ mL.
The cell culture was expanded in shake flasks until a sufficient volume was generated for inoculation of the bioreactor, until reaching a division ratio of 1: 5 in Applikon 1.5 L bioreactors. The reactor conditions were pH 6.9, 35 ° C , 150 rpm and dissolved oxygen level at 40% saturation. All the bioreactor experiments were carried out in duplicate. Cells were given three boluses of 1% of the initial volume of the combined feed reactor every third day, during the course of a run.
The use of both combination feeding solutions greatly increases the growth of cell culture. In the case of CF I, twice the peak of cell density was reached, although the culture lasted only 10 days, compared to 13 for the control. In the case of CF II, the peak cell density almost tripled compared to the control and the culture lasted a similar time. In terms of the final title, a more drastic effect was obtained. The titers for DMEM / F12 medium were approximately 41 mg / L, vs. 188 for CF I and 434 for CF II. The mee
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177 effect of different feeding solutions ^ ocher maximum cell density, culture duration, titer and specific productivity, are summarized in the following table:
Table 25. Performance of DMEM-F12m Combined Feeding Solutions
<td></td><td colspan="5">Parameter</td>
<td>Description</td><td>Peak Cell Density [1 0® viable cells / mL]</td><td>Final IVC [x10<sup>6 </sup>cells / d / mL]</td><td>Duration of cultivation [d]</td><td>Final Title [mg / L]</td><td>QP [pg / d-cell]</td>
<td>Control (n = 2)</td><td> 1.07 + 0.018</td><td> 9.53 + 0.005</td><td> 13</td><td> 41 ± 1.9</td><td> 4.7 ± 0.29</td>
<td>CFI (n = 2)</td><td> 1.92 ± 0.031</td><td> 11.27+ 0.004</td><td> 10</td><td> 188 ± 0.1</td><td> 16.4 ± 12.03</td>
<td>CFII (n = 2)</td><td> 2.72 ± 0.009</td><td> 20.74 ± 0.177</td><td> 13</td><td> 434 ± 16.5</td><td> 25.1 ± 1.17</td>
EXAMPLE 3.4: High Titer Cell Culture Process Through the Addition of Combined Feeding Solution
Obtaining higher titles results in fewer manufacturing runs being required to satisfy a given total return. The following example describes a large-scale batch feed process for ABT-874, which yielded an average titer of approximately 4 g / L during a batch feed process. Additionally, a further improvement of the media and of the combined feeding solution, allowed to reach titers higher than 6 g / L.
Materials and methods
As a model system, the ABT-874 antibody production line was used.
Preparation of the feeding solution
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The feeding solution was prepared according to the previously described procedures. Two concentrations of asparagine were used, that is, 5.0 or 7.5 g / kg. The preparation method is shown in the following table:
Table 26. ABT-874 Combined Feed Preparation
<td> 1</td><td>HsOmíiiíq</td><td> 600.0</td><td>g / kg</td>
<td> 2</td><td>Glucose</td><td> 150.0</td><td></td>
<td> 3</td><td>PFCHO</td><td> 21.0</td><td></td>
<td> 4</td><td>NaOH 10N</td><td></td><td>-> pH 10.00</td>
<td> 5</td><td>Asparagine</td><td>5.0 or 7.5</td><td></td>
<td> 6</td><td>Yeastolate</td><td> 65.0</td><td></td>
<td> 7</td><td>Phytone</td><td> 40.0</td><td></td>
<td> 8</td><td>HCI 5N</td><td></td><td>^ pH 6.75</td>
The components were weighed and added in order to achieve a final mass of 1 kg.
The materials were dissolved in the specified mass of water, using a laboratory magnetic stirrer under intense stirring. Until step 5, after adding each component, complete dissolution was visually verified before incorporating the next component. However, this was not possible in steps 6 and 7. For these two steps, incorporation of the powder into the solution was considered sufficient to proceed with the final addition of HCI.
Process medium selection
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In order to obtain performance data WH®4í * # - 4 «-Uftea-BASAL _, an experiment with 3X batch feed (FB) 3000 L was carried out as a control, the prototype process 4X FB and conditions unpowered (extended batch: EB) 3X and 4X. In particular, it has been suggested that higher media concentrations create an initial lag phase in the growth profile of the culture; however, no significant lag phase was observed for 3X or 4X extended batch (EB) processes.
As expected, fed supplementation produced higher titers for both 3X and 4X processes. However, significant growth suppression was observed for the 4X process if fed (ie, batch feeding). Amino acid analysis from small-scale experiments showed that, even after being fed, there was still a complete depletion of the amino acids asparagine and glutamine. For this reason, the total feeding time and the amount of asparagine in the combined feeding were increased. In conclusion, it was determined that the 4X FB process had the potential to achieve higher final titers than the EB processes or that the 3X FB control. Therefore, it was chosen as a starting point for further development.
The differences between the 3X (control) and 4X batch feed processes are described in Table 27 and described in more detail below.
Viable cell density at feeding start
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It was observed that upon initiating feeding at very low cell densities, there was a tendency to suppress cell growth and eventually the final titer. Thus, excessively delayed feeding was expected to cause loss of volumetric productivity due to cell starvation.
In order to investigate the above hypothesis, several experiments were carried out to determine the meaning of feeding at different viable cell densities. The combined results of these experiments are presented in the graph described in Figure 1. As can be seen in Figure 1, the title on day 15 shows a strong dependence on the density of viable cells on the day that the feeding. A third degree polynomial fit of the data shows that the maximum titer on day 15 can be expected at a feed rate of 3.5x10<sup>6</sup> cells / mL.
Reproducibility
The process conditions for the 67 g / L process are described in Table 27 and defined as inoculum to a 1: 4 partition of the run with little fill in SR-383, pH 7.0, OD = 30%, 37 ° C to a cell density of 5.0x10® viable cells / mL. The reactor operating conditions were pH 7.9, T = 35 ° C, DO = 40%. The feeding was started when the cells reached a viable density of 3.5x10® cells / mL, lasting 10 days, through bolus additions of the combined feeding solution consisting of 1% of the initial weight of the reactor, every day.
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The process conditions for the 4 g / L process are described below in Table 27.
Table 27. Most outstanding results of the ABT-874 4 and 6 g / L cell culture process
<td></td><td>Process</td><td></td>
<td>Parameter</td><td>3X FB</td><td>4X FB</td>
<td>Means, medium</td><td>SR-286 (3XPFCHO)</td><td>SR-382 (4XPFCHO)</td>
<td>Partition ratio</td><td> 1:5</td><td> 1:4</td>
<td>Density of sowing [10<sup>6</sup> cells viable / mL]</td><td> 0.5-1.0</td><td> 1.0-1.25</td>
<td>Feed Start Criterion</td><td>Day 3</td><td>3.5x10<sup>and</sup> cells / mL</td>
<td>Amount fed [% 1</td><td> 1</td><td> 1</td>
<td>Duration of feeding [days]</td><td> 7</td><td> 10</td>
<td>Asparagine in the feeding [g / L]</td><td> 5.0</td><td> 7.5</td>
<td>Change of temperature</td><td>33 ° C @ 3.5 / 10<sup>6</sup> cells / mL</td><td>none</td>
<td>Final title</td><td>4 g / L</td><td>6 g / L ± 0.24 (n = 9)</td>
d glucose
Example 3.5: Batch Feeding Using Combined Feeding Solution Using Feedback Control
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Feedback control ιχτπντο MU1CA £ Q I heard LA FHOFIIPAO tNWjmiAL
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established for a given parameter with a very limited understanding of the intrinsic behavior of the system. In this way, a given point can be maintained regardless of any alteration that the system may have suffered. Due to the complexity of the metabolism of mammalian cell culture, it is an intensive task to obtain complete models that could allow the prediction of the trajectory of a given culture. However, it is desirable to develop a sampling method, for example using an automatic sampler, to be able to deliver glucose in order to maintain a target glucose level. This enables the effect of a given concentration of glucose (or other metabolites) to be decoupled and also provides a mechanism for studying the effect that different glucose ratios in the combined feeding solution have on different cultures. Decoupling of effects refers to the effect of maintaining a given glucose concentration, versus the effect of using a different amount of glucose in a combined feeding solution.
Materials and methods
As a model system, the product lines of two different anti-IL-12 antibodies were used, which were ABT-784 and
1D4.7.
Automated sampling was chosen; that is, the Analyzer
Bioprocess YSI 2700, as a means of monitoring concentration
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OF THE INDUSTRIAL MONEDAD
<img file="MX353340B_D0199.tif" />
glucose in the cell culture medium. The apparatus gives nruiasírerL- ^. » Automated online was established by attaching a YSI 2730 monitor and Control Accessory to a YSI 2700 Bioprocess Analyzer (see YSI Life Sciences; Yellow Spring, OH). This sampling apparatus consisted of a pump holding two tubes. The first tube had two branches, one that collected the sample from the bioreactor, and the other that pumped antiseptic to maintain sterility. Once the sample was taken, it was pumped into an external chamber, from which the sample was taken for actual analysis. The second tube through the pump was used to collect the discharge in a waste container. Various parameters of the online sampling fixture were controlled, such as the sampling interval and the TPU (Time Per Unit Error, which corresponds to the time the free pump runs based on the measured displacement from a set point).
The pump was connected to the YSI using a 15 needle connector. The needle corresponding to the glucose probe (White-7, Black-11) on the YSI, was connected to the TTL on / off needle (8) on the pump, and one of the YSI ground needles (1 -5) Connected to the chassis, from the 15-pin connector for the pump. The connection was tested by turning the pump on and off from the YSI setup menu. The pump tubing used was CFLEX 082 from Masterflex.
Table 28: Preparation of the initial feedback experiment
<img file="MX353340B_D0200.tif" />
184
IMPI
WSTITUTO MBXICAN ·
OtlAHCHIMD iNDUmiAL
<td>Cells</td><td>ABT-874 i »</td>
<td>Media</td><td>3xPFCHO (SR-286)</td>
<td>Glucose fed</td><td>400 g / L</td>
<td>YSI TPU</td><td> 16</td>
<td>Reactor volume tested</td><td>1.5 L</td>
<td>YSI Purge Time</td><td>60 sec.</td>
<td>Pump speed</td><td>50 (half, ~ 16 rpm)</td>
<td>YSI Sampling Interval</td><td>4 h / 2 h (explained later)</td>
<td>YSI Output Signal</td><td>X2 (for YSI1-A25)</td>
<td>Antiseptic</td><td>NaOH 0.1N</td>
The YSI1-A25 reactor was controlled at 4.9 g / L glucose. Glucose control at 4.9 g / L was started approximately on day 2, using a sampling interval of 4 hours until day 8. On day 8, the sampling interval was reduced to 2 hours, and the point established in YSI Automated Device was re-adjusted to clear PID memory. Fluctuations caused by exceeding the set point were significantly reduced after day 8. Hence, a 2-hour sampling interval was established to be optimal for these conditions. The average overrun from day 2 to day 8 was 0.43 g / L, and the average gap was 0.31 g / L, with a fluctuation error of approximately 8% of the set point. On the other hand, the average overrun from 8 to 13 was 0.08 g / L, and the »
<img file="MX353340B_D0201.tif" />
185 Average missing was 0.09 g / L, with a fluctuation error of approximately 2%.
Control of glucose concentration using combined feeding
The feeding schedule of the combined feeding solutions to a culture in a bioreactor was defined using an empirical approach. Different feeding amounts, as well as different feeding times, were tested until a viable batch feeding scheme was found. Ideally, the feeding schedule for a combination feeding solution should meet the specific requirements for a given crop.
In view of the above considerations, it was advantageous to provide the combined feed based on the needs of the cell culture, for example, using glucose as an indicator of nutritional requirements. In this way, a feedback control system can be used to 1) test different feed solutions with varying glucose concentrations, and 2) use the generated feed profile to manually feed in large-scale culture.
The following table summarizes two different modes of reactor operation, employing a cell line that produces the 1D4.7 monoclonal antibody. The reference experiment (referred to as baseline in Table 29), illustrates the typical titer performance of an extended batch process on SR-372 medium,
<img file="MX353340B_D0202.tif" />
186 running at pH 6.9, T = 35 ° C, DO - 40-5, in 1.5L Applikon bioreactors. The YSI experiments were conducted under the same conditions, plus feedback control, to supply the combined feed solutions containing
100, 150 or 200 g / L of glucose.
Tala 29. Performance of combined feeding using feedback control
<td>Experiment</td><td>Final title [mg / L]</td>
<td>Baseline</td><td> 1312 ± 33</td>
<td>(n = 2)</td><td></td>
<td>YSI100</td><td> 1974</td>
<td>(n = 1)</td><td></td>
<td>YSI150</td><td> 2044 ±164</td>
<td>(n = 2)</td><td></td>
<td>YSI200</td><td> 1837 ± 163</td>
<td>(n = 2)</td><td></td>
As can be seen in Table 29, the feedback system using a variety of combined feeding solutions, greatly improved the final antibody titer.
The feeding profiles of the experiments as above were obtained by weighing the amount of combined feeding solution supplied per day. A profile of
IMPI
<img file="MX353340B_D0203.tif" />
187 typical feeding is presented in the following latria?
Table 30: Typical feeding profile generated through the feedback control (profile for antibody 1D4.7)
<td>Day</td><td>Food [%]</td>
<td> 1</td><td> 0.00</td>
<td> 2</td><td> 0.00</td>
<td> 3</td><td> 0.00</td>
<td> 4</td><td> 0.00</td>
<td> 5</td><td> 1.12</td>
<td> 6</td><td> 1.58</td>
<td> 7</td><td> 1.79</td>
<td> 8</td><td> 1.23</td>
<td> 9</td><td> 0.89</td>
<td> 10</td><td> 0.75</td>
<td> 11</td><td> 0.46</td>
<td> 12</td><td> 0.32</td>
The above scheme can also be performed to manually power a reactor even without a feedback control system. In this way, the feeding program can be scaled.
Summary of Results
Batch feeding processes using a mixture of hydrolyzates and a chemically defined basal medium are
<img file="MX353340B_D0204.tif" />
188 it was shown that they increase the final titer of secreted m'ó'noclonal anti-antibodies in mammalian cell cultures.
In addition, a method capable of generating the following stable combined feeds was demonstrated:
Table 31: Stable Combined Feeds
<td></td><td>X-1</td><td>D2E7 diluted</td><td>D2E7</td><td>ABT-325, ABT-874</td><td>Power 1</td><td>Food II</td><td></td>
<td>Glucose</td><td> 21</td><td> 200</td><td> 100, 150, 250</td><td> 150</td><td> 150</td><td> 150</td><td>g / kg</td>
<td>PFCHO (p), DMEM, F12m (d)</td><td>20 (P)</td><td>20 (P)</td><td>27 (p)</td><td>21 (d)</td><td>27 (d)</td><td>21 (d)</td><td></td>
<td>NaOH 10N</td><td></td><td></td><td></td><td></td><td></td><td></td><td>- »pH 10.00</td>
<td>Asparagine</td><td> 7.5</td><td> 2.29</td><td> 3.1</td><td> 5, 7.5</td><td> 3.1</td><td> 5</td><td></td>
<td>Yeastolate</td><td> 22</td><td> 15.7</td><td> 21.2</td><td> 65.0</td><td> 21.2</td><td> 65.0</td><td></td>
<td>Phytone</td><td> 14</td><td> 10.0</td><td> 13.5</td><td> 40.0</td><td> 13.5</td><td> 40.0</td><td></td>
<td>HCI 5N</td><td></td><td></td><td></td><td></td><td></td><td></td><td>pH 6.75</td>
<td>H 2Omíii¡o</td><td colspan="7">Up to 1000 g</td>
The combined feed described in Table 31 was prepared starting with H<sub>2</sub>Omíii¡q (up to 750 g). As indicated above, the ingredients were added to the water up to a final weight (overall weight of the combined feed) of 1000 g. Additionally, the combined feed solutions were shown to increase cell culture longevity, peak viable cell density, and specific productivity. I know
<img file="MX353340B_D0205.tif" />
189 demonstrated batch feeding processes of euitwoa aelulares, using combined feeding solutions capable of reaching titres up to 6 g / L of the secreted monoclonal antibody. The above combined feeding solutions were also shown to increase the cell density of the cultures.
Finally, it was also shown that a method that uses a feedback control system and different combined feeding solutions, is capable of increasing the titers. This approach could be used to accelerate the development of the cell culture process, by rapidly generating feeding programs.
References
one. Whitford, WG, Feb-Batch Mammalian Cell Culture in Bioproduction. BioProcess International, 2006. 30-40.
2. YSI Incorporated. (1998) YSI 2700 Select Biochemistry Analyzer User's Manual.
3. YSI Incorporated. (1998) YSI 2730 Monitor and Control Accessory User's Manual.
Four. Watson Marlow Pumps. 101F, 101U User's Manual.
Example 4: Application of Sodium Butyrate and N-acetylcysteine to Increase Productivity of an Anti-IL-18 Producing CHO Cell Line
The present invention encompasses a new approach to increase the productivity of an antibody, for example an anti-IL-18 producing CHO cell line. More specifically, the
190
<img file="MX353340B_D0206.tif" />
MEXICAN INSTTTVTO
Pt L * FRORIIDA »INDUSTRIAL The following example refers to an increase in. Final antibody titer, eg anti-IL-18, by adding chemicals to the cell culture medium. The improvements in cell viability and in antibody titer are described below using an example antibody; that is, the IL-18 antibody.
Cell Line and Culture Media
The anti-IL-18 antibody used in the following example is a fully human IgG1 (Ab) antibody against IL-18. The CHO cell line expressing anti-IL-18 was grown in growth medium 10, previously described in Table 4 of Example 1, SR-371. Production media for the cell line are also as previously described in Example 1, SR-372 (used for shake flask culture) and SR-372 (used for bioreactor culture).
<15 Cultivation Conditions for Experiments Conducted in Shaking Flasks
All shake flask experiments were performed in duplicate. The flask cultures were shaken on a Thermolyne shaking plate at 80 rpm, in an incubator at 35 ° C 20 with 5% CO<sub>2</sub>. Immediately prior to inoculation, the required amount of cell suspension was taken from the maintenance culture. The cells were centrifuged, the supernatant was discarded and the pellets were resuspended in freshly prepared and previously heated culture medium, to obtain a seed density of 4 x 10<sup>5</sup> cells / mL.
<img file="MX353340B_D0207.tif" />
191
Example 4.1: Effect of sodium butyrate on the growth and productivity of an anti-IL-producing CHO cell line
18, grown in growth medium
To determine the concentration range of sodium butyrate, the first experiment was carried out in SR-371 medium containing various concentrations of sodium butyrate. The experiment was carried out in 100 mL shake flasks, with a working volume of 70 mL. Sodium butyrate was added from a 1M concentrated solution, which was prepared by dissolving 1,101 g of sodium butyrate in 10 mL of MilliQ water and filter sterilized through a 0.2 pm filter. The solution was stored at -20 ° C.
Sodium butyrate was added at the beginning of the culture (day 0), in concentrations of 0 mM, 0.125 mM, 0.5 mM and 1 mM. Cell density and viability were determined with an automatic cell counter (Cedex, Innovatis, Germany) in this example and in all the following examples. Table 32 shows the density of viable cells with respect to time, and Table 33 describes the viability with respect to time. The experiment was carried out for 12 days.
Table 32: Viable Cell Density with respect to Time d
Culture
<td colspan="2">Viable Cell Density</td><td> [10<sup>5</sup>/ mL]</td><td></td><td></td><td></td><td></td><td></td>
<td>Flask Day 1:</td><td>Flask 2:</td><td>Flask 3:</td><td>Flask 4:</td><td>Flask 5:</td><td>Flask 6:</td><td>Flask 7:</td><td>Flask 8:</td>
<td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate 1</td>
<img file="MX353340B_D0208.tif" />
192
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MUAPKONITMD
MPUmiM
<td></td><td>0 mM</td><td rowspan="2">0 mM</td><td> 0 125</td><td> 0 125</td><td rowspan="2">0.5 mM</td><td rowspan="2">0.5 mM</td><td></td><td></td>
<td></td><td></td><td>mM</td><td>mM</td><td></td><td></td>
<td> 0</td><td> 3.2</td><td> 3.85</td><td> 4.46</td><td> 3.01</td><td> 3.66</td><td> 3.98</td><td> 3.83</td><td></td>
<td> 3</td><td> 36.38</td><td> 33.18</td><td> 27.12</td><td> 29.96</td><td> 16.97</td><td> 11.71</td><td> 7.68</td><td></td>
<td> 5</td><td> 84.48</td><td> 70.37</td><td> 62.56</td><td> 66.1</td><td> 21.79</td><td> 9.77</td><td> 3.25</td><td></td>
<td> 7</td><td> 65.98</td><td> 64.19</td><td> 59.15</td><td> 68.65</td><td> 17.72</td><td> 5.41</td><td> 1.04</td><td></td>
<td> 10</td><td> 7.83</td><td> 11.17</td><td> 8.63</td><td> 11.85</td><td> 4.53</td><td> 6.93</td><td> 0.8</td><td></td>
<td> 12</td><td> 1.36</td><td> 2.28</td><td> 3.68</td><td> 3.81</td><td> 2.08</td><td> 1.89</td><td> 0.22</td><td></td>
Table 33: Viability with respect to the cultivation time
Viability [%]
<td>Day</td><td>Flask 1:</td><td>Flask 2:</td><td>Flask 3:</td><td>Flask 4:</td><td>Flask 5:</td><td>Flask 6:</td><td>Flask 7:</td><td>Flask 8:</td>
<td></td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate 1</td>
<td></td><td>0 mM</td><td>0 mM</td><td> 0.125</td><td> 0.125</td><td>0.5 mM</td><td>0.5 mM</td><td>1 mM</td><td>mM</td>
<td></td><td></td><td></td><td>mM</td><td>mM</td><td></td><td></td><td></td><td></td>
<td> 0</td><td> 98.5</td><td> 97.5</td><td> 98.9</td><td> 100</td><td> 97.4</td><td> 98.2</td><td> 98.8</td><td> 98.8</td>
<td> 3</td><td> 98.3</td><td> 98.1</td><td> 97.3</td><td> 97.9</td><td> 95.4</td><td> 92.2</td><td> 88.3</td><td> 73.8</td>
<td> 5</td><td> 96.7</td><td> 96.7</td><td> 96</td><td> 96.7</td><td> 88.8</td><td> 72.9</td><td> 54</td><td> 40.1</td>
<td> 7</td><td> 73.4</td><td> 75.5</td><td> 78.1</td><td> 83.3</td><td> 69</td><td> 43.1</td><td> 24.2</td><td> 16.4</td>
<td> 10</td><td> 7.9</td><td> 13.1</td><td> 13.1</td><td> 14.3</td><td> 21</td><td> 25.9</td><td> 11.3</td><td> 14.5</td>
<td> 12</td><td> 1.4</td><td> 2.8</td><td> 5.9</td><td> 4.9</td><td> 7.6</td><td> 14.9</td><td> 3.2</td><td> 8.9</td>
It can be clearly seen that sodium butyrate affected the growth and viability of the cell. While there was no obvious effect on cell growth and viability at a butyrate concentration of 0.125mM, there was a clear impact on cell growth at 0.5mM butyrate, causing a lower maximum cell density. With 0.5 mM sodium butyrate, viability was affected after 5 days of cultivation time. Sodium butyrate completely inhibited cell growth at a concentration
<img file="MX353340B_D0209.tif" />
193 of 1 mM, and the viability decreased MMinuamantA ri ^ t hl-. n<sub>or</sub>.
ahead.
Table 34 shows the anti-IL-18 titer with respect to culture time. The anti-IL-18 concentration was determined by a Poros A HPLC assay, in this example and in the following examples.
Table 34: Anti-IL-18 titer with respect to culture time
Title (mg / L]
<td>Day</td><td>Flask 1:</td><td>Flask 2:</td><td>Flask 3:</td><td>Flask 4:</td><td>Flask 5:</td><td>Flask 6:</td><td>Flask 7:</td><td>Flask 8</td>
<td></td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td>
<td></td><td>0 mM</td><td>0 mM</td><td> 0.125</td><td> 0.125</td><td>0.5 mM</td><td>0.5 mM</td><td>1 mM</td><td>mM</td>
<td></td><td></td><td></td><td>mM</td><td>mM</td><td></td><td></td><td></td><td></td>
<td> 0</td><td> 5.4</td><td> 2.4</td><td> 1.8</td><td> 1.6</td><td> 1.3</td><td> 1.3</td><td> 1.1</td><td> 1.3</td>
<td> 3</td><td> 68.9</td><td> 58.1</td><td> 67.7</td><td> 65.7</td><td> 52.1</td><td> 41.9</td><td> 36.3</td><td> 26.2</td>
<td> 5</td><td> 173.2</td><td> 150.4</td><td> 169.4</td><td> 174.3</td><td> 132.6</td><td> 84.2</td><td> 68.6</td><td> 46.4</td>
<td> 7</td><td> 235.5</td><td> 211.9</td><td> 253.6</td><td> 278.5</td><td> 217.7</td><td> 110.7</td><td> 85</td><td> 60.9</td>
<td> 10</td><td> 265.5</td><td> 241.8</td><td> 304.3</td><td> 365.9</td><td> 278.2</td><td> 163.3</td><td> 91.8</td><td> 70.3</td>
<td> 12</td><td> 269.7</td><td> 244.4</td><td> 318.7</td><td> 385.8</td><td> 282.7</td><td> 175.9</td><td> 94</td><td> 75.4</td>
The average final titer of the 0.125 mM butyrate cultures was 352 mg / L, the average final titer of the untreated control was 257 mg / L. At this butyrate concentration, the treatment produced a 40% increase in the final titer.
Example 4.2: Effect of sodium butyrate on the growth and productivity of an antiIL-18 producing CHO cell line grown in SR-372
The CHO cell line expressing anti-IL-18 was adapted to grow in SR-372 medium, in order to exclude any
<img file="MX353340B_D0210.tif" />
194 Possible effect of culture partitioning of SR-371 to GR 9 '? · 2. — fed-os. Experiments with cells adapted to grow in SR372 medium were carried out in 250 mL shake flasks, with a working volume of 180 mL. Cultures were carried out applying the conditions previously indicated in the section titled Culture Conditions for Experiments Conducted in Flasks for Shaking.
An experiment was designed to add butyrate when the cells were in the middle and late exponential growth phase. The latest addition of butyrate will probably cause less stress to the cells, and will result in improved cell growth and a higher ICV compared to the addition on day 0, because the concentration of butyrate per cell is higher. low (the viable cell integral (ICV), is defined as the integral of the density of viable cells versus the culture time). Butyrate was added on day 4 and day 5 in concentrations of 0.5mM and 2mM. The experiment was carried out for 12 days. Table 4 shows the density of viable cells with respect to the culture time, Table 5 shows the viability with respect to the culture time. Only 2 mM sodium butyrate added on day 4 resulted in reduced viability compared to control, the other conditions did not affect viability.
Table 35: Density of viable cells with respect to the time of culture
IMPI Mexican iMrWrvrc
M PROPERTY
INDUmAL
<img file="MX353340B_D0211.tif" />
195
Viable Cell Density [10<sup>AND</sup>/ mL]
<td>Day</td><td>Flask 1:</td><td>Flask 2:</td><td>Flask 3:</td><td>Flask 4:</td><td>Flask 5:</td><td>Flask 6:</td><td>Flask 7:</td><td>Flask 8:</td>
<td></td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate 1</td>
<td></td><td>0 mM</td><td>0 mM</td><td> 0.125</td><td> 0.125</td><td>0.5 mM</td><td>0.5 mL</td><td>1 mM</td><td>mM</td>
<td></td><td></td><td></td><td>mM</td><td>mM</td><td></td><td></td><td></td><td></td>
<td> 0</td><td> 2.35</td><td> 3.37</td><td> 3.08</td><td> 2.61</td><td> 2.27</td><td> 2.41</td><td> 3.2</td><td> 2.27</td>
<td> 3</td><td> 14.51</td><td> 15.79</td><td> 12.79</td><td> 13.69</td><td> 14.04</td><td> 9.42</td><td> 11.41</td><td> 11.36</td>
<td> 4</td><td> 28.88</td><td> 20.91</td><td> 18.88</td><td> 26.11</td><td> 25.48</td><td> 16.09</td><td> 18.78</td><td> 23.15</td>
<td> 5</td><td> 28.58</td><td> 32.17</td><td> 36.01</td><td> 33.03</td><td> 27.82</td><td> 21.98</td><td> 30.76</td><td> 35.8</td>
<td> 6</td><td> 61.91</td><td> 54.31</td><td> 45.2</td><td> 43.08</td><td> 37.02</td><td> 34.28</td><td> 47.82</td><td> 55.66</td>
<td> 7</td><td> 56.23</td><td> 51.59</td><td> 40.09</td><td> 36.19</td><td> 33.34</td><td> 27.21</td><td> 42.97</td><td> 52.03</td>
<td> 10</td><td> 43.06</td><td> 51.89</td><td> 29.2</td><td> 23.33</td><td> 14.07</td><td> 13.05</td><td> 29.58</td><td> 28.61</td>
<td> 12</td><td> 24.8</td><td> 33.38</td><td> 19.38</td><td> 14.32</td><td> 9.66</td><td> 8.22</td><td> 18.25</td><td> 16.18</td>
<td colspan="2">Table Viability [%]</td><td colspan="2">36: Feasibility</td><td colspan="2">with respect to</td><td>I time</td><td colspan="2">cultivation</td>
<td>Day</td><td>Flask 1:</td><td>Flask 2:</td><td>Flask 3:</td><td>Flask</td><td>Flask 5:</td><td>Flask 6:</td><td>Flask 7:</td><td>Flask 8:</td>
<td></td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td> 4:</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate 1</td>
<td></td><td>0 mM</td><td>0 mM</td><td>0.125 mM</td><td>Butirat or 0.125 mM</td><td>0.5 mM</td><td>0.5 mM</td><td>1 mM</td><td>mM</td>
<td> 0</td><td> 98.4</td><td> 94.6</td><td> 92.7</td><td> 99</td><td> 95.2</td><td> 94.9</td><td> 98.8</td><td> 97.7</td>
<td> 3</td><td> 96.6</td><td> 97.2</td><td> 98.8</td><td> 99</td><td> 97.2</td><td> 98</td><td> 97.8</td><td> 97.8</td>
<td> 4</td><td> 97</td><td> 98.5</td><td> 99</td><td> 98.6</td><td> 98.5</td><td> 98</td><td> 98.9</td><td> 97.8</td>
<td> 5</td><td> 96.6</td><td> 97.7</td><td> 97.5</td><td> 97.3</td><td> 98.6</td><td> 97.9</td><td> 98</td><td> 97.2</td>
<td> 6</td><td> 96.5</td><td> 96.4</td><td> 98.2</td><td> 98</td><td> 93.6</td><td> 92.4</td><td> 95.3</td><td> 96</td>
<td> 7</td><td> 95.6</td><td> 95.7</td><td> 93.8</td><td> 92.9</td><td> 87.8</td><td> 87.5</td><td> 94.2</td><td> 94</td>
<td> 10</td><td> 62.6</td><td> 69.4</td><td> '61.9</td><td> 53.9</td><td> 40.8</td><td> 39.2</td><td> 63.7</td><td> 56.9</td>
<td> 12</td><td> 38.3</td><td> 46.2</td><td> 40.4</td><td> 33.6</td><td> 24.5</td><td> 25.2</td><td> 36.7</td><td> 32.7</td>
Table 37 shows the anti-IL-18 titer with respect to culture time. 2 mM sodium butyrate added on day 5,
<img file="MX353340B_D0212.tif" />
196 resulted in a 29% increase compared to control (317 mg / L versus 245 mg / L, respectively). Cell growth was not significantly inhibited under these conditions (see Table 35).
Table 37: Titer of anti-IL-18 with respect to culture time
Title (mg / Ll
<td>Day</td><td>Flask</td><td>Flask</td><td>Flask 3:</td><td>Flask 4:</td><td>Flask 5:</td><td>Flask 6:</td><td>Flask 7:</td><td>Flask 8:</td><td>Flask</td><td>Flask</td>
<td></td><td>Γ.</td><td> 2.</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate</td><td>Butyrate 1</td><td>Butyrate</td><td> 9:</td><td> 10:</td>
<td></td><td>Butyrate</td><td>Butyrate</td><td>0.125 mM</td><td>0.125 mM</td><td>0.5 mM</td><td>0.5 mM</td><td>mM</td><td>0.5 mM</td><td>Butyrate</td><td>Butyrate</td>
<td></td><td>0 mM</td><td>0 mM</td><td></td><td></td><td></td><td></td><td></td><td></td><td>0.5 mM</td><td>1 mM</td>
<td> 7</td><td> 138.5</td><td> 141.1</td><td> 147.7</td><td> 139.2</td><td> 183.4</td><td> 182</td><td> 129.5</td><td> 137.5</td><td> 152.8</td><td> 149.5</td>
<td> 10</td><td> 192.2</td><td> 208.7</td><td> 226.9</td><td> 203.3</td><td> 269.6</td><td> 259.5</td><td> 202.5</td><td> 205.4</td><td> 266.1</td><td> 260.6</td>
<td> 12</td><td> 232.2</td><td> 258.7</td><td> 269.4</td><td> 235.3</td><td> 307,8</td><td> 286.2</td><td> 237.4</td><td> 236.9</td><td> 319.3</td><td> 315</td>
Example 4.3: Effect of sodium butyrate on the growth and productivity of an anti-IL-18 producer CHO cell line grown in SR-382 medium, in a 3 L Bioreactor
The following example demonstrates the increase in the final titer of anti-IL-18 antibodies, by applying sodium butyrate to anti-IL-18 process B (see Section 1.5), in large-scale bioreactors; that is, 3 L. This process was developed in 3L Applikon bioreactors. The cultivation for sowing was carried out in SR-371 medium until the low filling stage (SR-372). The underfilling stage was simulated in a 20 L Biowave bag, with a working volume of 10 L. The experiment to investigate the effect of sodium butyrate on the growth and productivity of anti-IL-18 process B, was carried out in 3 L Applikon bioreactors, with a working volume of 1.5 L. Each bioreactor was filled with 1125 mL of SR-382 medium and inoculated by adding 375 mL of suspension
<img file="MX353340B_D0213.tif" />
197 cell from the Biowave bag containing cells that produced anti-IL-18 in SR-372 medium.
In Example 4.2, the titer increase was achieved by adding butyrate when the cells were in the mid to late logarithmic phase, which was on day 5 in shake flasks. Historically, the mid to late log phase of the anti-IL-18 production process in a 3L bioreactor is on day 7 of culture time. In this example, on day 7 it was selected to add sodium butyrate to the culture, to ensure that the butyrate was added in the middle to late log phase.
A concentrated solution of sodium butyrate at a concentration of 200 mM was prepared on day 7 immediately prior to addition to the culture by dissolving 4,404 g of sodium butyrate in 200 mL of MilliQ water. This solution was sterilized by filtration through a 0.22 pm filter.
The experiment was carried out with 5 bioreactors. The process of each bioreactor was finished when the respective viability was lower than 50%. Bioreactors served as control (anti-IL-18 process B). Sodium butyrate was added on day 7 of culture time to the other 3 bioreactors, in concentrations of 0.3 mM, 1 mM and 3 mM, respectively. Table 38 shows the concentration of viable cells with respect to the culture time, and Table 39 shows the viability with respect to the culture time.
Table 38: Dnsity of viable cells during the time of
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<img file="MX353340B_D0214.tif" />
culture
<td colspan="4">Viable Cell Density [10<sup>5</sup>/ mL]</td><td></td><td></td>
<td>Day</td><td>Reactor 1: Butyrate 1 mM</td><td>Reactor 2: Without Butyrate</td><td>Reactor 3: Butyrate 0.3 mM</td><td>Reactor 4: 3mM Butyrate</td><td>Reactor 5: Without butyrate</td>
<td> 0</td><td> 5.53</td><td> 5.22</td><td> 4.89</td><td> 5.28</td><td> 5.41</td>
<td> 1</td><td> 8.21</td><td> 7.68</td><td> '7.66</td><td> 9.66</td><td> 6.81</td>
<td> 2</td><td> 11.35</td><td> 13.53</td><td> 10.39</td><td> 11.12</td><td> 10.07</td>
<td> 3</td><td> 15.62</td><td> 17.37</td><td> 12.58</td><td> 14.3</td><td> 13.07</td>
<td> 4</td><td> 20.69</td><td> 22.4</td><td> 18.39</td><td> 22.46</td><td> 16.49</td>
<td> 5</td><td> 29.58</td><td> 31.55</td><td> 31.15</td><td> 34.03</td><td> 23.43</td>
<td> 6</td><td> 41.27</td><td> 44.42</td><td> 43.321</td><td> 46.81</td><td> 32.3</td>
<td> 7</td><td> 59.07</td><td> 62.09</td><td> 56.91</td><td> 60.46</td><td> 33.95</td>
<td> 8</td><td> 67.07</td><td> 76.26</td><td> 51.82</td><td> 76.4</td><td> 45.43</td>
<td> 9</td><td> 68.68</td><td> 73.23</td><td> 63.11</td><td> 61.52</td><td> 5-7.6</td>
<td> 10</td><td> 65.55</td><td> 70.17</td><td> 64.53</td><td> 55.52</td><td> 62.45</td>
<td> 11</td><td> 66.55</td><td> 72.98</td><td> 66.23</td><td> 47.27</td><td> 63.42</td>
<td> 12</td><td> 60.98</td><td> 56.33</td><td> 45.87</td><td> 30.99</td><td> 44.65</td>
<td> 13</td><td> 49.67</td><td> 52.03</td><td> 40.39</td><td> 21.34</td><td> 39.1</td>
<td> 14</td><td> 38.46</td><td> 30.51</td><td> 21.93</td><td></td><td> 18.38</td>
<td> 15</td><td> 33.23</td><td> 38.37 ·</td><td> 41.34</td><td></td><td> 35.97</td>
<td> 16</td><td> 27.97</td><td> 29.31</td><td> 33.89</td><td></td><td> 24.58</td>
<td> 17</td><td></td><td></td><td> 30.13</td><td></td><td> 17.51</td>
<td> 18</td><td></td><td></td><td> 20.98</td><td></td><td></td>
Table 39: Viability with respect to cultivation time
<td colspan="4">Viable Cell Density [10<sup>5</sup>/ mL]</td><td colspan="2"></td>
<td>Day</td><td>Reactor 1: Butyrate 1 mM</td><td>Reactor 2: Without Butyrate</td><td>Reactor 3: Butyrate 0.3 mM</td><td>Reactor 4: 3mM Butyrate</td><td>Reactor 5: Without butyrate</td>
<td> 0</td><td> 95.3</td><td> 96</td><td> 92.9</td><td> 94.3</td><td> 96.4</td>
<td> 1</td><td> 96.4</td><td> 95.4</td><td> 96.4</td><td> 96.3</td><td> 95.9</td>
<td> 2</td><td> 96.3</td><td> 95.9</td><td> 95.9</td><td> 96.1</td><td> 96.7</td>
<td> 3</td><td> 96.6</td><td> 95.6</td><td> 97.7</td><td> 96.6</td><td> 95.3</td>
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<img file="MX353340B_D0215.tif" />
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<td> 4</td><td> 97.3</td><td> 97.2</td><td> 96.4</td><td> 95.8</td><td> 95.2</td>
<td> 5</td><td> 97.1</td><td> 96.4</td><td> 96.2</td><td> 96.4</td><td> 95.3</td>
<td> 6</td><td> 96.4</td><td> 96.5</td><td> 96.2</td><td> 96.8</td><td> 95.9</td>
<td> 7</td><td> 96.3</td><td> 95.2</td><td> 95.8</td><td> 94.3</td><td> 95.1</td>
<td> 8</td><td> 96.2</td><td> 95.2</td><td> 94.2</td><td> 95.1</td><td> 94.8</td>
<td> 9</td><td> 95.6</td><td> 95.2</td><td> 95.4</td><td> 93.6</td><td> 94.2</td>
<td> 10</td><td> 94.3</td><td> 94.5</td><td> 94.6</td><td> 87.4</td><td> 93.4</td>
<td> 11</td><td> 92.2</td><td> 93.9</td><td> 93.8</td><td> 78.9</td><td> 93</td>
<td> 12</td><td> 88.1</td><td> 91.7</td><td> 92.4</td><td> 51.9</td><td> 92</td>
<td> 13</td><td> 80.6</td><td> 86.9</td><td> 90.2</td><td> 33.7</td><td> 89.2</td>
<td> 14</td><td> 66.7</td><td> 76.2</td><td> 88.9</td><td></td><td> 84.1</td>
<td> 15</td><td> 57</td><td> 60.7</td><td> 85.2</td><td></td><td> 73.4</td>
<td> 16</td><td> 45.9</td><td> 42.7</td><td> 69.5</td><td></td><td> 50.7</td>
<td> 17</td><td></td><td></td><td> 58.1</td><td></td><td> 34.2</td>
<td> 18</td><td></td><td></td><td> 41</td><td></td><td></td>
The control culture grew slower in reactor 5 than in replicate (reactor 2), due to the high initial concentrations of CO<sub>2</sub> in reactor 5. Reactor 2 was terminated on day 16 of culture time (historically observed in the anti-IL-18 production process), reactor 5 was terminated on day 17. Sodium butyrate at a concentration of 3 mM (reactor 4), affected the growth and viability of the cells. Two days after the addition of the butyrate, the cells began to die. Butyrate at a concentration of 1 mM, did not affect growth or cell viability (reactor 1), the reactor worked until it was finished in the day
16. Cell growth was very similar in Reactor 2 compared to control. Butyrate at a concentration of 0.3 mM, prolonged
<img file="MX353340B_D0216.tif" />
IMPI
<img file="MX353340B_D0217.tif" />
200 culture time 2 days (reactor 3). The TabraTLI'iYiüéSTrá he LILUler of anti-IL-18 with respect to the time of cultivation.
Table 40: Anti-IL-18 titer with respect to culture time
<td>Title</td><td colspan="4">[mg / L]</td><td></td>
<td>Day</td><td>Reactor 1: Butyrate 1 mM</td><td>Reactor 2: Without Butyrate</td><td>Reactor 3: Butyrate 0.3 mM</td><td>Reactor 4: 3mM Butyrate</td><td>Reactor 5: Without butyrate</td>
<td> 9</td><td> 1033</td><td> 1074.2</td><td> 905.8'</td><td> 966.9</td><td> 747.4</td>
<td> 10</td><td> 1218.4</td><td> 1223.9</td><td> 1096.4</td><td> 1184.9</td><td> 877.5</td>
<td> 11</td><td> 1410.4</td><td> 1460</td><td> 1261.1</td><td> 1242.9</td><td> 1053.5</td>
<td> 12</td><td> 1663.5</td><td> 1538.1</td><td> 1485.1</td><td> 1269.5</td><td> 1216.7</td>
<td> 13</td><td> 1700.2</td><td> 1912.5</td><td> 1750.9</td><td> 1304.6</td><td> 1303</td>
<td> 14</td><td> 1852.7</td><td> 2136.9</td><td> 1923.4</td><td> 96.4</td><td> 1429.3</td>
<td> 15</td><td> 1909.4</td><td> 2223.2</td><td> 2280.4</td><td> 96.8</td><td> 1672.3</td>
<td> 16</td><td> 1933.7</td><td> 2324.7</td><td> 2108.6</td><td> 94.3</td><td> 1540.5</td>
<td> 17</td><td> 96.2</td><td> 95.2</td><td> 2561.3</td><td> 95.1</td><td> 1589.4</td>
<td> 18</td><td></td><td></td><td> 2448.6</td><td></td><td></td>
The final titer (day 16) of the culture in reactor 2 (representing an anti-IL-18 process B) was 2325 g / L. The final titer in reactor 5 was 1589 g / L. This lower titer is possibly due to the worse cell growth caused by the high initial CO concentration.<sub>2</sub> in the culture medium. Butyrate at a concentration of 1 mM and 3 mM, added on day 7, resulted in a lower final titer than control (reactor 2). Butyrate at a concentration of 0.3 mM added on day 7, resulted in a titer of 2561 g / L on day 17, which is a 10% increase compared to the control. This title was
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INDWJTIUAI highest title achieved in the anti-IL-10 process .-—
Example 4.4: Effect of N-acetylcysteine (10mM, 20mM, 40mM, 80mM) on the growth and productivity of a CHO cell line producing anti-IL-18 antibodies, cultured in SR-372 medium
N-acetylcysteine can protect mammalian cells from cell death. As an antioxidant, it can directly reduce reactive oxygen species. Through deacetylation, it can be transformed into cysteine and increase intracellular glutathione levels. Glutathione can pick up reactive oxygen species and serves as a substrate in the reduction of hydrogen peroxide in water.
This example demonstrates the effect of increasing the anti-IL-18 titer of N-acetylcysteine. The experiments were carried out in 250 mL shake flasks, with a working volume of 180 mL. The culture medium was SR-372. Before the experiment, the cells were pre-adapted to grow in SR-372 medium, as described in Example 4.2. The conditions of the culture under agitation were applied in the manner described above, in the Section Conditions of Culture for Experiments Conducted in Flasks for Agitation.
A concentrated solution of 1M N-acetylcysteine was prepared by dissolving 16.32 g of N-acetylcysteine in 100 mL of MilliQ water on a plate with heating and stirring. The concentrated solution was filter sterilized through a 0.22 filter
<img file="MX353340B_D0218.tif" />
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202 mexican institute
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INDUSTRIAL pm. One day before starting the experiment, H-auethylcylotoin was added to SR-372 medium, until obtaining concentrations of 0 mM, 10 mM, 20 mM, 40 mM and 80 mM. The experiment started by centrifuging the cells from a maintenance culture of anti-IL-18 producing CHO cells, as previously described in the Culture Conditions section for Experiments Conducted in Shake Flasks. Each shaking culture was terminated when the respective viability was less than 50%.
Cell growth was not possible at N-acetylcysteine concentrations of 20mM, 40mM and 80mM. Tables 41 and 42 show the comparison of viable cell density and viability, respectively, with respect to culture time, with cells grown in 0mM N-acetylcysteine and 10mM N-acetylcysteine.
Table 41: Density of viable cells with respect to culture time
<td colspan="5">Viable Cell Density [10 ° / mL]</td>
<td>Day</td><td>Flask 1: Without Nacetylcysteine</td><td>Flask 2: Without N- acetylcysteine</td><td>Flask 3: N-acetylcysteine 1 0 mM</td><td>Flask 4: N-acetylcysteine 10 mM</td>
<td> 0</td><td> 3.60</td><td> 3.44</td><td> 2.73</td><td> 2.73</td>
<td> 3</td><td> 18.34</td><td> 17.72</td><td> 3.58</td><td> 3.02</td>
<td> 4</td><td> 29.39</td><td> 29.71</td><td> 4.47</td><td> 4.24</td>
<td> 5</td><td> 33.54</td><td> 31.05</td><td> 6.46</td><td> 6.40</td>
<td> 6</td><td> 37.38</td><td> 32.92</td><td> 9.84</td><td> 7.27</td>
<img file="MX353340B_D0219.tif" />
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<img file="MX353340B_D0220.tif" />
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<td rowspan="2"> 7</td><td rowspan="2"> 34.26</td><td rowspan="2"> 31.00</td><td> 12.36</td><td> 12.00</td>
<td></td><td></td>
<td> 8</td><td> 17.49</td><td> 17.68</td><td> 24.20</td><td> 22.42</td>
<td> 9</td><td> 25.34</td><td> 21.54</td><td> 20.14</td><td> 19.48</td>
<td> 10</td><td> 17.49</td><td> 17.68</td><td> 24.20</td><td> 22.42</td>
<td> 11</td><td> 10.75</td><td> 13.84</td><td> 25.02</td><td> 26.00</td>
<td> 12</td><td></td><td></td><td> 27.44</td><td> 27.56</td>
<td> 13</td><td></td><td></td><td> 25.77</td><td> 27.86</td>
<td> 14</td><td></td><td></td><td> 22.77</td><td> 24.17</td>
<td> 15</td><td></td><td></td><td> 18.40</td><td> 19.22</td>
<td> 16</td><td></td><td></td><td> 14.60</td><td> 16.30</td>
Table 42: Viability with respect to cultivation time
<td colspan="5">Viability [%]</td>
<td>Day</td><td>Flask 1: Without Nacetylcysteine</td><td>Flask 2: Without N- acetylcysteine</td><td>Flask 3: N-acetylcysteine 10 mM</td><td>Flask 4: N-acetylcysteine 1 0 mM</td>
<td> 0</td><td> 97.4</td><td> 96.9</td><td> 96.2</td><td> 95.3</td>
<td> 3</td><td> 98.8</td><td> 98.6</td><td> 57.2</td><td> 52.1</td>
<td> 4</td><td> 99.0</td><td> 98.8</td><td> 61.9</td><td> 62.2</td>
<td> 5</td><td> 98.7</td><td> 98.5</td><td> 69.5</td><td> 72.1</td>
<td> 6</td><td> 95.4</td><td> 92.8</td><td> 76.0</td><td> 73.5</td>
<td> 7</td><td> 87.8</td><td> 84.0</td><td> 81.5</td><td> 80.9</td>
<td> 8</td><td> 73.3</td><td> 69.6</td><td> 85.5</td><td> 82.7</td>
<td> 9</td><td> 64.9</td><td> 60.8</td><td> 82.7</td><td> 86.5</td>
<td> 10</td><td> 52.5</td><td> 49.0</td><td> 82.5</td><td> 86.9</td>
<td> 11</td><td> 38.6</td><td> 38.1</td><td> 81.7</td><td> 87.2</td>
<td> 12</td><td></td><td></td><td> 79.2</td><td> 83.1</td>
<td> 13</td><td></td><td></td><td> 74.8</td><td> 78.9</td>
<td> 14</td><td></td><td></td><td> 67.2</td><td> 68.7</td>
<img file="MX353340B_D0221.tif" />
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<td> 15</td><td></td><td></td><td> 56.7</td><td>ΤΓ5 -------</td>
<td> 16</td><td></td><td></td><td> 49.3</td><td> 47.2</td>
The control culture (without N-acetylcysteine), was terminated on day 11 of the culture time, while the culture with 10 mM Nacetylcysteine, could be prolonged until day 16. Initially, the 10 mM N-acetylcysteine affected cell growth and viability, and caused a decrease in viability until day 3. Thereafter, viability began to increase. The maximum cell density of the cultures grown in 10 mM N-acetylcysteine was lower compared to the control. Table 43 demonstrates the increase in the final anti-IL-18 antibody titer by N-acetylcysteine.
Table 43: Titer of anti-IL-18 with respect to culture time
<td colspan="4">Title [mg / L]</td><td></td>
<td>Day</td><td>Flask 1: Without N- acetylcysteine</td><td>Flask 2: Without N- acetylcysteine</td><td>Flask 3: N-acetylcysteine 10 mM</td><td>Flask 4: N-acetylcysteine 10 mM</td>
<td> 4</td><td> 102.0</td><td> 94.9</td><td> 23.9</td><td> 21.9</td>
<td> 5</td><td> 130.5</td><td> 122.4</td><td> 35.3</td><td> 32.5</td>
<td> 6</td><td> 168.5</td><td> 154.3</td><td> 60.6</td><td> 55.9</td>
<td> 7</td><td> 190.4</td><td> 171.8</td><td> 84.2</td><td> 78.0</td>
<td> 8</td><td> 216.4</td><td> 194.3</td><td> 125.3</td><td> 119.3</td>
<td> 9</td><td> 233.0</td><td> 206.9</td><td> 156.6</td><td> 153.1</td>
<td> 10</td><td> 243.2</td><td> 216.4</td><td> 185.9</td><td> 187.7</td>
<td> 11</td><td> 258.6</td><td> 227.8</td><td> 224.1</td><td> 230.9</td>
<td> 12</td><td></td><td></td><td> 264.1</td><td> 272.6</td>
<td> 13</td><td></td><td></td><td> 300.2</td><td> 31 1.2</td>
<img file="MX353340B_D0222.tif" />
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<td> 14</td><td></td><td></td><td> 334.0 ——’</td><td>SI 4.0 ---</td>
<td> 15</td><td></td><td></td><td> 393.0</td><td> 384.4</td>
<td> 16</td><td></td><td></td><td> 414.6</td><td> 421.4</td>
The average final titer of the control cultures was 243.2 mg / L, the average final titer of the cultures growing in 10 mM N-acetylcysteine was 418 mg / L. This was a 72% increase compared to the control.
Example 4.5: Effect of N-acetylcysteine (1mM, 2mM, 4mM, 8mM) on the growth and productivity of a CHO cell line producing anti-IL-18 antibodies, cultured in SR-372 medium
As described in Example 4.4, N-acetylcysteine at a concentration of 10 mM, added on day 0, was able to prolong the culture time and caused an increase in the final titer. However, at this concentration, cell viability initially decreased. Based on the results of Example 4.4, an experiment was designed using one-tenth of the Nacetylcysteine concentrations tested in Example 4.4. The conditions for this experiment in shake flasks were the same as in Example 4.4. N-acetylcysteine was added in concentrations of 0mM (control), 1mM, 2mM, 4mM and 8mM.
Table 44 shows the density of viable cells with respect to the culture time, and Table 45 shows the viability with respect to the culture time.
<img file="MX353340B_D0223.tif" />
206
Table 44: Density of viable cells with resp «« te> -aLjUaj3xpauÍ £. culture
<td>Day</td><td>Flask 1:</td><td>Flask 2:</td><td>Flask 3:</td><td>Flask 4:</td><td>Flask 5:</td>
<td></td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td>
<td></td><td>0 mM</td><td>0 mM</td><td>1 mM</td><td>1 mM</td><td>2 mM</td>
<td> 0</td><td> 2.75</td><td> 3,45</td><td> 3.64</td><td> 3.22</td><td> 4.10</td>
<td> 3</td><td> 25.05</td><td> 22.42</td><td> 19.25</td><td> 19.32</td><td> 17.42</td>
<td> 4</td><td> 35.98</td><td> 31.42</td><td> 25.45</td><td> 24.56</td><td> 24.96</td>
<td> 5</td><td> 45.43</td><td> 37.56</td><td> 31.16</td><td> 29.23</td><td> 27.28</td>
<td> 6</td><td> 40.04</td><td> 39.41</td><td> 29.67</td><td> 28.35</td><td> 28.45</td>
<td> 7</td><td> 35.55</td><td> 33.25</td><td> 27.71</td><td> 27.03</td><td> 26.65</td>
<td> 8</td><td> 31.56</td><td> 26.22</td><td> 24.63</td><td> 22.33</td><td> 22.49</td>
<td> 9</td><td> 27.15</td><td> 23.04</td><td> 22.23</td><td> 20.23</td><td> 19.11</td>
<td> 10</td><td> 23.26</td><td> 19.88</td><td> 21.06</td><td> 17.74</td><td> 18.07</td>
<td> 1 1</td><td></td><td></td><td></td><td></td><td> 15.48</td>
<td> 12</td><td></td><td></td><td></td><td></td><td></td>
<td> 13</td><td></td><td></td><td></td><td></td><td></td>
<td> 14</td><td></td><td></td><td></td><td></td><td></td>
<td>Day</td><td>Flask 6:</td><td>Flask 7:</td><td>Flask 8:</td><td>Flask 9:</td><td>Flask 1 0:</td>
<td></td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td>
<td></td><td>2 mM</td><td>4 mM</td><td>4 mM</td><td>8 mM</td><td>8 mM</td>
<td> 0</td><td> 2.96</td><td> 3.1 3</td><td> 2.80</td><td> 2.97</td><td> 3.54</td>
<td> 3</td><td> 19.03</td><td> 17.39</td><td> 16.39</td><td> 11.24</td><td> 10.17</td>
<td> 4</td><td> 28.40</td><td> 24.80</td><td> 23.71</td><td> 14.47</td><td> 1 3.88</td>
<td> 5</td><td> 34.21</td><td> 28.06</td><td> 26.92</td><td> 20.68</td><td> 18 64</td>
<td> 6</td><td> 37.05</td><td> 30.62</td><td> 29.54</td><td> 25.59</td><td> 23.13</td>
<td> 7</td><td> 32.55</td><td> 30.66</td><td> 26.94</td><td> 28.22</td><td> 26.12</td>
<td> 8</td><td> 28.99</td><td> 24.75</td><td> 23 84</td><td> 30.00</td><td> 30.77</td>
<td> 9</td><td> 27.75</td><td> 22.25</td><td> 21.71</td><td> 27.45</td><td> 28.63</td>
<td> 10</td><td> 23.05</td><td> 20.06</td><td> 19.67</td><td> 27.14</td><td> 27.90</td>
<td> 1</td><td> 20.75</td><td> 16.79</td><td> 16.70</td><td> 26.42</td><td> 29.60</td>
<td> 12</td><td></td><td></td><td></td><td> 26.39</td><td> 25.62</td>
<td> 13</td><td></td><td></td><td></td><td> 21.46</td><td> 22.29</td>
<td> 14</td><td></td><td></td><td></td><td> 30.47</td><td> 32.41</td>
<img file="MX353340B_D0224.tif" />
207
Table 45: Viability with respect to cultivation time
<img file="MX353340B_D0225.tif" />
IMP aftmuro MtXICANO DI LA nOHEDAO tHCUrnUAL
<td>Day</td><td>Flask 1:</td><td>Flask 2:</td><td>Flask 3:</td><td>Flask 4:</td><td>Flask 5:</td>
<td></td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine 2</td>
<td></td><td>0 mM</td><td>0 mM</td><td>1 mM</td><td>1 mM</td><td>mM</td>
<td>Day</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td>
<td></td><td>0 mM</td><td>0 mM</td><td>1 mM</td><td>1 mM</td><td>2 mM</td>
<td> 0</td><td> 94.6</td><td> 97.6</td><td> 96.2</td><td> 93.3</td><td> 94.9</td>
<td> 3</td><td> 98.3</td><td> 97.6</td><td> 99.1</td><td> 98.1</td><td> 98.6</td>
<td> 4</td><td> 98.0</td><td> 96.8</td><td> 98.2</td><td> 97.6</td><td> 97.2</td>
<td> 5</td><td> 97.1</td><td> 96.0</td><td> 96.3</td><td> 95.0</td><td> 96.1</td>
<td> 6</td><td> 90.2</td><td> 89.6</td><td> 89.3</td><td> 89.3</td><td> 89.9</td>
<td> 7</td><td> 79.0</td><td> 80.1</td><td> 79.8</td><td> 77.3</td><td> 79.6</td>
<td> 8</td><td> 60.6</td><td> 62.2</td><td> 64.8</td><td> 62.2</td><td> 62.2</td>
<td> 9</td><td> 52.7</td><td> 53.4</td><td> 56.9</td><td> 52.6</td><td> 54.8</td>
<td> 10</td><td> 46.2</td><td> 45.5</td><td> 51.3</td><td> 45.9</td><td> 50.2</td>
<td> 11</td><td></td><td></td><td></td><td></td><td> 40.3</td>
<td> 12</td><td></td><td></td><td></td><td></td><td></td>
<td> 13</td><td></td><td></td><td></td><td></td><td></td>
<td> 14</td><td></td><td></td><td></td><td></td><td></td>
<td>Day</td><td>Flask 6:</td><td>Flask 7:</td><td>Flask 8:</td><td>Flask 9:</td><td>Flask 10:</td>
<td></td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td>
<td></td><td>2 mM</td><td>4 mM</td><td>4 mM</td><td>8 mM</td><td>8 mM</td>
<td> 0</td><td> 93.8</td><td> 94.9</td><td> 91.7</td><td> 92.1</td><td> 93.6</td>
<td> 3</td><td> 97.5</td><td> 97.1</td><td> 98.4</td><td> 96.4</td><td> 94.3</td>
<td> 4</td><td> 98.2</td><td> 97.4</td><td> 97.6</td><td> 96.4</td><td> 94.4</td>
<td> 5</td><td> 97.1</td><td> 97.1</td><td> 96.9</td><td> 96.5</td><td> 94.4</td>
<td> 6</td><td> 93.0</td><td> 92.4</td><td> 93.1</td><td> 95.8</td><td> 92.0</td>
<td> 7</td><td> 86.1</td><td> 84.5</td><td> 85.0</td><td> 93.4</td><td> 89.6</td>
<td> 8</td><td> 71.9</td><td> 68.4</td><td> 70.6</td><td> 85.6</td><td> 84.7</td>
<td> 9</td><td> 65.2</td><td> 58.5</td><td> 60.3</td><td> 79.7</td><td> 79.5</td>
<td> 10</td><td> 54.9</td><td> 52.0</td><td> 55.0</td><td> 76.3</td><td> 75.0</td>
<img file="MX353340B_D0226.tif" />
208
IMPI Mexican INJmvro OF THE INDUSTRIAL WtOHJDAD
<td> 11</td><td> 45.1</td><td> 42.5</td><td> 45.7</td><td> 68.4</td><td> 69.0</td><td></td>
<td> 12</td><td></td><td></td><td></td><td> 61.3</td><td> 61.2</td><td></td>
<td> 13</td><td></td><td></td><td></td><td> 51.1</td><td> 52.2</td><td></td>
<td> 14</td><td></td><td></td><td></td><td> 39.4</td><td> 42.6</td><td></td>
Control cultures (0 mM N-acetylcysteine) were terminated after 10 days of culture time. Nacetylcysteine was able to prolong the longevity of the culture. Cultures grown in 8 mM N-acetylcysteine were terminated after 14 days of culture. Cultures grown on N-acetylcysteine had a lower maximum cell density, compared to the control.
Table 46 shows the effect of N-acetylcysteine on the final anti-IL-18 antibody titer.
Table 46: Anti-IL-18 Antibody Titer Regarding Culture Time
<td>Title</td><td colspan="3">[mg / L]</td><td colspan="2"></td>
<td>Day</td><td>Flask 1: N-acetylcysteine 0 mM</td><td>Flask 2: N-acetylcysteine 0 mM</td><td>Flask 3: N-aceti did you read ina 1 mM</td><td>Flask 4: N-acetylcysteine 1 mM</td><td>Flask 5: N-acetylcysteine 2 mM</td>
<td> 7</td><td> 193.1</td><td> 168.3</td><td> 210.1</td><td> 202.5</td><td> 198.0</td>
<td> 8</td><td> 230.3</td><td> 199.9</td><td> 241.6</td><td> 232.2</td><td> 227.5</td>
<td> 9</td><td> 244.7</td><td> 216.2</td><td> 256.6</td><td> 245.4</td><td> 242.0</td>
<td> 10</td><td> 262.7</td><td> 227.2</td><td> 268.9</td><td> 258.3</td><td> 253.2</td>
<td> 11</td><td></td><td></td><td></td><td></td><td> 268.3</td>
<td> 12</td><td></td><td></td><td></td><td></td><td></td>
<td> 13</td><td></td><td></td><td></td><td></td><td></td>
<td> 14</td><td></td><td></td><td></td><td></td><td></td>
IMPI or not wwwe> o »CA> to züy MunomoAD O — níí'XJ
INOUfniAL * »» '»
<td>Day</td><td>Flask 6:</td><td>Flask 7:</td><td>Flask 8:</td><td>Flask 9:</td><td>Flask 10:</td>
<td></td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td><td>N-acetylcysteine</td>
<td></td><td>2 mM</td><td>4 mM</td><td>4 mM</td><td>8 mM</td><td>8 mM</td>
<td> 7</td><td> 274.0</td><td> 210.9</td><td> 202.0</td><td> 181.9</td><td> 175.1</td>
<td> 8</td><td> 323.9</td><td> 251.6</td><td> 240.2</td><td> 237.6</td><td> 232.2</td>
<td> 9</td><td> 374.7</td><td> 271.7</td><td> 259.3</td><td> 267.7</td><td> 263.9</td>
<td> 10</td><td> 428.8</td><td> 288.9</td><td> 276.3</td><td> 295.3</td><td> 292.2</td>
<td> 11</td><td> 444.1</td><td> 315.5</td><td> 304.3</td><td> 349.1</td><td> 367.9</td>
<td> 12</td><td></td><td></td><td></td><td> 369.5</td><td> 401.4</td>
<td> 13</td><td></td><td></td><td></td><td> 429.5</td><td> 432.0</td>
<td> 14</td><td></td><td></td><td></td><td> 477.6</td><td> 484.4</td>
The final final anti-IL-18 antibody titer of the control cultures was 245 mg / L (very similar to the 243 mg / L of Example 4.4). The final anti-IL-18 antibody titer of the cultures grown in 8 mM N-acetylcysteine was 481 mg / L. This is a 96% increase compared to the control.
Equivalents
Those skilled in the art will recognize, or be able to verify using no more than routine experiments, numerous equivalents of the specific embodiments of the invention described herein. Such equivalents are intended to be covered by the following claims. The contents of all published references, patents and patent applications, which are cited throughout this description, are incorporated herein by reference.
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Priority claims14
| Document | Office | Kind | Date |
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| 60845158 | United States of America | – | |
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| 84515806 | United States of America | P | |
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| 87637406 | United States of America | P | |
| 87637406 | United States of America | P | |
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| 60845158 | – | – | – |
| 60876374 | – | – | – |
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| US20060876374P | – | – | – |
| WO2007US20027 | – | – | – |
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- Application
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- MX20170003647
Titles
- Spanish
- MEJORAS DE CULTIVOS CELULARES.
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- C12N5/0037
- C12N5/00
- C07K16/00
- C07K2317/21
- C12N2500/24
- C12N2500/25
- C12N2500/50
- C12N2500/60
- C12N2500/74
- C12N2500/76
- C12N2510/02
- C12N5/0031
- C07K16/244
- C07K16/241
- C07K16/2869
- C12N5/0603
- C12N2500/30
- C12N2500/32
- C12N2500/90
- C12N2501/33
- C07K2317/14
- C12N2511/00
- C12N2500/38
- C12N2501/10
- C12N2500/34
- IPC, 3
- C07K16 24
- C12N5 10
- C12P21 08