Apparatus and method for preparing microparticles using in-line solvent extraction
Abstract
A process for preparing microparticles, comprising: preparing a first phase, the first phase comprising an active agent and a polymer; prepare a second phase; combining the first phase and the second phase in a first static mixer to form an emulsion; combining the emulsion and a first extraction liquid in a second static mixer; and combine a flow rate of the second static mixer with a second extraction liquid.

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49 claims: 4 independent, 45 dependent
- 1ES 2 236 035 T3 REIVINDICACIONES 1. Un procedimiento para preparar micropartículas, que comprende:preparar una primera fase, comprendiendo la primera fase un agente activo y un polímero;preparar una segunda fase;combinar la primera fase y la segunda fase en un primer mezclador estático para formar una emulsión;combinar la emulsión y un primer líquido de extracción en un segundo mezclador estático;y combinar un caudal del segundo mezclador estático con un segundo líquido de extracción.
- 2El procedimiento de la reivindicación 1, en el que la etapa de combinar el caudal del segundo mezclador estático con el segundo líquido de extracción comprende:dejar que el caudal del segundo mezclador estático fluya dentro de un recipiente que contiene el segundo líquido de extracción.
- 3El procedimiento de la reivindicación 1, en el que la etapa de combinar el caudal del segundo mezclador estático con el segundo líquido de extracción comprende:combinar el caudal del segundo mezclador estático y el segundo líquido de extracción en un tercer mezclador estático.
- 4El procedimiento de la reivindicación 3, que comprende además:dejar que un caudal del tercer mezclador estático fluya dentro de un recipiente.
- 5El procedimiento de la reivindicación 4, en el que el recipiente está vacío antes de dejar que el caudal del tercer mezclador estático fluya en él.
- 6El procedimiento de la reivindicación 4, que comprende además:continuar la etapa de combinar el caudal del segundo mezclador estático y el segundo líquido de extracción en el tercer mezclador estático hasta que la primera fase se agota;y transferir un resto del segundo líquido de extracción al recipiente.
- 7El procedimiento de la reivindicación 1, en el que la etapa de combinar el caudal del segundo mezclador estático con el segundo líquido de extracción comprende:dejar que el caudal del segundo mezclador estático fluya dentro de un recipiente;y añadir el segundo líquido de extracción al recipiente.
- 8El procedimiento de la reivindicación 7, en el que la etapa de añadir el segundo líquido de extracción al recipiente se lleva a cabo mientras el caudal del segundo mezclador estático fluye dentro del recipiente.
- 9El procedimiento de la reivindicación 7, en el que la etapa de añadir el segundo líquido de extracción al recipiente se lleva a cabo después de que se completa la etapa de dejar que el caudal del segundo mezclador estático fluya dentro del recipiente.
- 10El procedimiento de la reivindicación 1,2 ó 3 en el que el segundo mezclador estático comprende una pluralidad de mezcladores estáticos individuales configurados para proporcionar una pluralidad de corrientes de flujo paralelas.
- 11El procedimiento de la reivindicación 10, en el que la pluralidad de mezcladores estáticos individuales es dos.
- 12El procedimiento de la reivindicación 1, en el que la etapa de combinar la primera fase y la segunda fase comprende:bombear la primera fase a una primera velocidad de flujo;y bombear la segunda fase a una segunda velocidad de flujo mayor que la primera velocidad de flujo. ES 2 236 035 T3
- 13El procedimiento de la reivindicación 12, en el que una relación de la segunda velocidad de flujo frente a la primera velocidad de flujo es aproximadamente 2:1.
- 14El procedimiento de la reivindicación 1, en el que la etapa de combinar la emulsión y la primera extracción líquida comprende:bombear la primera extracción líquida a una primera velocidad dentro de la emulsión que fluye fuera del primer mezclador estático para formar una primera corriente combinada y;dejar que la primera corriente combinada fluya a través del segundo mezclador estático.
- 15El procedimiento de la reivindicación 14, en el que una relación de volumen de la emulsión frente al primer líquido de extracción es aproximadamente 1:1.
- 16El procedimiento de la reivindicación 1 o reivindicación 14, en el que la etapa de combinar el caudal del segundo mezclador estático con el segundo líquido de extracción comprende:bombear el segundo líquido de extracción a una segunda velocidad dentro del caudal del segundo mezclador estático para formar una segunda corriente combinada y;dejar que la segunda corriente combinada fluya a través de un tercer mezclador estático.
- 17El procedimiento de la reivindicación 16, en el que la segunda velocidad es mayor que la primera velocidad.
- 18El procedimiento de la reivindicación 1 o reivindicación 16 en el que el primer líquido de extracción y el segundo líquido de extracción son el mismo.
- 19El procedimiento de la reivindicación 1 o reivindicación 16 en el que el primer líquido de extracción y el segundo líquido de extracción son diferentes.
- 20El procedimiento de la reivindicación 1, en el que una relación de volumen de la segunda fase frente a la primera fase es aproximadamente 5:1.
- 21El procedimiento de la reivindicación 1, en el que una relación de volumen de la segunda fase frente a la primera fase es aproximadamente 3:1.
- 22El procedimiento de la reivindicación 1, en el que el primer líquido de extracción es el mismo que la segunda fase.
- 23El procedimiento de la reivindicación 22, en el que el segundo líquido de extracción es el mismo que la segunda fase.
- 24El procedimiento de la reivindicación 1, en el que la etapa de preparar la primera fase comprende:disolver el agente activo en un primer disolvente para formar una solución de agente activo;disolver el polímero en un segundo disolvente para formar una solución de polímero;y mezclar la solución de agente activo y la solución de polímero.
- 25El procedimiento de la reivindicación 24, en el que el agente activo se selecciona del grupo formado por risperidona, 9-hidroxirrisperidona, y sales farmacéuticamente aceptables de éstos.
- 26El procedimiento de la reivindicación 24, en el que el primer disolvente es alcohol bencílico.
- 27El procedimiento de la reivindicación 26, en el que el segundo disolvente es acetato de etilo.
- 28El procedimiento de la reivindicación 1, en el que la etapa de preparar la primera fase comprende:disolver el agente activo y el polímero en un disolvente para formar una solución.
- 29El procedimiento de la reivindicación 28, en el que el agente activo es bupivacaína y el disolvente es acetato de etilo.
- 30El procedimiento de la reivindicación 24 o reivindicación 29, en el que el polímero es poli(d,1-láctido-coglicólido) que tiene una relación molar de láctido frente a glicólido en el intervalo entre aproximadamente 85:15 y aproximadamente 50:50. ES 2 236 035 T3
- 31Un procedimiento para preparar micropartículas, que comprende:preparar una primera fase, comprendiendo la primera fase un agente activo y un polímero;preparar una segunda fase;combinar la primera fase y la segunda fase en un primer mezclador estático para formar una emulsión, formando la emulsión un caudal del primer mezclador estático;combinar el caudal del primer mezclador estático y una primera parte de un volumen de partida de un líquido de extracción en un segundo mezclador estático para formar un caudal del segundo mezclador estático;dividir el caudal del segundo mezclador estático para formar al menos dos corrientes de flujo;fluir cada una de las al menos dos corrientes de flujo a través de un tercer mezclador estático distinto;y combinar las al menos dos corrientes de flujo con una segunda parte del líquido de extracción.
- 32El procedimiento de la reivindicación 31, en el que la etapa de combinar las al menos dos corrientes de flujo con la segunda parte del líquido de extracción comprende:dejar que las al menos dos corrientes de flujo fluyan dentro de un recipiente que contiene la segunda parte del líquido de extracción.
- 33El procedimiento de la reivindicación 31, en el que la etapa de combinar las al menos dos corrientes de flujo con la segunda parte del líquido de extracción comprende:combinar las al menos dos corrientes de flujo y la segunda parte del líquido de extracción en un cuarto mezclador estático.
- 34Los procedimientos de la reivindicación 33, que comprenden además:dejar que un caudal del cuarto mezclador estático fluya dentro de un recipiente.
- 35El procedimiento de la reivindicación 34, que comprende además:continuar la etapa de combinar las la menos dos corrientes de flujo y la segunda parte del líquido de extracción en el cuarto mezclador estático hasta que la primera fase se agota;y transferir un resto del volumen de partida del líquido de extracción al recipiente.
- 36El procedimiento de la reivindicación 31, en el que la etapa de combinar las al menos dos corrientes de flujo con la segunda parte del líquido de extracción comprende:combinar las al menos dos corrientes de flujo y la segunda parte del líquido de extracción en un cuarto mezclador estático y repetir esta etapa de combinación hasta que el volumen de partida del líquido de extracción se agota.
- 37Un procedimiento para preparar micropartículas, que comprende:preparar una primera fase, comprendiendo la primera fase un agente activo y un polímero;preparar una segunda fase;combinar la primera fase y la segunda fase en un primer mezclador estático para formar una emulsión, formando la emulsión un caudal del primer mezclador estático;combinar un caudal del primer mezclador estático y un primer un líquido de extracción en un segundo mezclador estático para formar un caudal del segundo mezclador estático;dividir el caudal del segundo mezclador estático para formar al menos dos corrientes de flujo;fluir cada una de las al menos dos corrientes de flujo a través de un tercer mezclador estático distinto;y combinar las al menos dos corrientes de flujo con un segundo líquido de extracción.
- 38El procedimiento de la reivindicación 37, en el que el segundo líquido de extracción es diferente del primer líquido de extracción. ES 2 236 035 T3
- 39El procedimiento de la reivindicación 37, en el que la etapa de combinar las al menos dos corrientes de flujo con el segundo líquido de extracción comprende:dejar que las al menos dos corrientes de flujo fluyan dentro de un recipiente que contiene el segundo líquido de extracción.
- 40El procedimiento de la reivindicación 37, en el que la etapa de combinar las al menos dos corrientes de flujo con el segundo líquido de extracción comprende:combinar las al menos dos corrientes de flujo y el segundo líquido de extracción en un cuarto mezclador estático.
- 41El procedimiento de la reivindicación 40, en el que el segundo líquido de extracción es diferente del primer líquido de extracción.
- 42El procedimiento de la reivindicación 40, que comprende además:dejar que un caudal del cuarto mezclador estático fluya dentro de un recipiente.
- 43El procedimiento de la reivindicación 37, en el que la etapa de combinar las al menos dos corrientes de flujo con el segundo líquido de extracción comprende:combinar las al menos dos corrientes de flujo y el segundo líquido de extracción en un cuarto mezclador estático y repetir esta etapa de combinación hasta que el segundo líquido de extracción se agota.
- 44El procedimiento de la reivindicación 42, que comprende además:continuar la etapa de combinar las la menos dos corrientes de flujo y el segundo líquido de extracción en el cuarto mezclador estático hasta que la primera fase se agota;y transferir un resto del volumen de partida del líquido de extracción al recipiente.
- 45Un sistema para preparar micropartículas, que comprende:una primera bomba;una segunda bomba;un primer mezclador estático en comunicación fluida con dicha primera bomba y con dicha segunda bomba, en el que dicha primera bomba se configura para bombear una fase orgánica en dicho primer mezclador estático y dicha segunda bomba se configura para bombear una fase continua dentro de dicho primer mezclador estático;un distribuidor en comunicación fluida con dicho primer mezclador estático, comprendiendo dicho distribuidor una pluralidad de mezcladores estáticos;una tercera bomba en comunicación fluida con dicho distribuidor, en el que dicha tercera bomba se configura para bombear un líquido de extracción;y un segundo mezclador estático en comunicación fluida con dicho distribuidor, en el que el segundo mezclador estático y dicho distribuidor se configuran de modo que un caudal de dicho primer mezclador estático y el líquido de extracción fluyan a través de dicho distribuidor y luego a través de dicho segundo mezclador estático.
- 46El sistema de la reivindicación 45, que comprende además:un recipiente en comunicación fluida con dicho segundo mezclador estático, en el que un caudal de dicho segundo mezclador estático fluye dentro de dicho recipiente.
- 47El sistema de la reivindicación 45, que comprende además:una cuarta bomba en comunicación fluida con dicho segundo mezclador estático, en el que dicha cuarta bomba se configura para bombear el líquido de extracción dentro de dicho segundo mezclador estático.
- 48El sistema de la reivindicación 47, en el que dicha cuarta bomba se configura para funcionar a una velocidad de flujo mayor que una velocidad de flujo de dicha tercera bomba. ES 2 236 035 T3
- 49El sistema de la reivindicación 45, que comprende además:un tercer mezclador estático en comunicación fluida con dicho primer mezclador estático y con dicho distribuidor, en el que el caudal de dicho primer mezclador estático y el líquido de extracción fluyen a través de dicho tercer mezclador estático antes de fluir a través de dicho distribuidor.
Independent claims49
137 paragraphs in 7 sections, as filed
ES 2 236 035 T3
DESCRIPTION
Equipment and procedure for preparing microparticles using in-line solvent extraction.
Background of the invention
Field of the invention
The present invention relates to the preparation of microparticles. More particularly, the present invention relates to a process and equipment for preparing microparticles using in-line solvent extraction.
Related art
Various processes are known by which the compounds can be encapsulated into microparticles. It is particularly advantageous to encapsulate a biologically active or pharmaceutically active agent within a biodegradable and biocompatible barrier-forming material (eg, a polymer) to provide sustained or delayed release of drugs or other active agents. In these procedures (eg, as disclosed in US 5,650,173) the material to be encapsulated (drugs or other active agents) is generally dissolved, dispersed, or emulsified, using stirrers, or other dynamic mixing techniques. , in a solvent that contains the material that forms the barrier. The solvent is then removed from the microparticles and thereafter the microparticle product is obtained.
Developing a microencapsulation process suitable for commercial scale production typically requires scaling up, by multiple factors, a laboratory scale procedure and / or a pilot scale procedure. The scaled-up process will almost always require larger pipes and higher flow rates, particularly when the scale factor is very large or if it is desired or necessary to keep the process transfer times similar to those of smaller scale processes. Scaling up on new, larger equipment is often unpredictable and is largely accomplished through trial and error. However, the economic costs of large-scale trial and error experiments can be prohibitive.
One approach to aid in the scaling up procedure is to use a static mixer to form an emulsion, as disclosed in US Patent No. 5,654,008. In the process disclosed in US Patent No. 5,654,008, a first phase, comprising the active agent and polymer, and a second phase are pumped through a static mixer into an inactivation liquid to form microparticles. containing the active agent. The use of a static mixer to form the emulsion tends to make scaling up more predictable and reliable than scaling up other dynamic mixing processes for making microparticles. However, many trials and experiments are still required to fully and accurately scale up, such as to commercial scale or by a factor of 20 or more, a procedure such as that disclosed in US Patent No. 5,654,008. The use of static mixers in microencapsulation is also disclosed by YF Maa and C. Hsu (J. Microencapsulation, 1996, vol 13, no 4, 419-433).
Thus, there is a need in the art for an improved method and equipment for preparing microparticles. There is a particular need in the art for an improved process that can be scaled up more quickly, more accurately and more reliably from a laboratory or pilot scale to a commercial scale. The present invention, the description of which is fully published below, solves the need in the art for such a method and equipment.
Summary of the invention
The present invention relates to a kit and a process for preparing microparticles. In one aspect of the invention, a process for preparing microparticles is provided. The procedure includes:
preparing a first phase, the first phase comprising an active agent and a polymer; prepare a second phase;
combining the first phase and the second phase in a first static mixer to form an emulsion;
combining the emulsion and a first extraction liquid in a second static mixer; and combining a flow rate from the second static mixer with a second extraction liquid. In one aspect of such a process, the flow rate from the second static mixer flows into a vessel containing the second extraction liquid. In another aspect, the flow rate from the second static mixer flows into a container, and the second extraction liquid is added to the container. The second extraction liquid can be added to the vessel while the flow rate from the second static mixer is flowing into the vessel, or after the flow rate from the second static mixer has fully flowed into the vessel. In another aspect, the flow rate from the second static mixer and the second extraction liquid can be combined in another static mixer.
ES 2 236 035 T3
In a further aspect of the present invention, another method of preparing microparticles is provided. The procedure includes:
preparing a first phase, the first phase comprising an active agent and a polymer; prepare a second phase;
combining the first phase and the second phase in a first static mixer to form an emulsion, the emulsion forming a flow from the first static mixer;
combining the flow rate of the first static mixer and a first part of a starting volume of an extraction liquid in a second static mixer to form a flow rate of the second static mixer;
dividing the flow rate of the second static mixer to form at least two flow streams;
flowing each of the at least two flow streams through a separate third static mixer; and combining the at least two flow streams with a second part of the extraction liquid.
In one aspect of said process, the at least two flow streams flow into a container containing the second part of the extraction liquid. In another aspect, the at least two flow streams and the second part of the extraction liquid are combined in a fourth static mixer. In yet another aspect, the at least two flow streams and the second part of the extraction liquid are combined in a fourth static mixer, and the combining step is repeated until the starting volume of the extraction liquid is exhausted. The combining step can be repeated by continuing to combine the at least two flow streams and the extraction liquid in the fourth static mixer until the starting volume of the extraction liquid is exhausted. Alternatively, the combining step can be repeated by combining the at least two flow streams and the extraction liquid in additional static mixers until the starting volume of the extraction liquid is exhausted.
In a further aspect of the present invention, another method of preparing microparticles is provided. The procedure includes:
preparing a first phase, the first phase comprising an active agent and a polymer; prepare a second phase;
combining the first phase and the second phase in a first static mixer to form an emulsion, the emulsion forming a flow from the first static mixer;
combining the flow rate of the first static mixer and a first an extraction liquid in a second static mixer to form a flow rate of the second static mixer;
dividing the flow rate of the second static mixer to form at least two flow streams;
flowing each of the at least two flow streams through a separate third static mixer; and combining the at least two flow streams with a second extraction liquid.
In yet another aspect of the present invention, there is provided a microencapsulated active agent prepared by a process for preparing microparticles. This procedure includes:
preparing a first phase, the first phase comprising an active agent and a polymer; prepare a second phase;
combining the first and second phases in a first static mixer to form an emulsion;
combining the emulsion and a first extraction liquid in a second static mixer; and combining a flow rate from the second static mixer with a second extraction liquid.
In yet another aspect of the present invention, there is provided a microencapsulated active agent prepared by another method for preparing microparticles. This procedure includes:
preparing a first phase, the first phase comprising an active agent and a polymer; prepare a second phase;
ES 2 236 035 T3 combining the first phase and the second phase in a first static mixer to form an emulsion, the emulsion forming a flow from the first static mixer;
combining the flow rate of the first static mixer and a first part of a starting volume of an extraction liquid in a second static mixer to form a flow rate of the second static mixer;
dividing the flow rate of the second static mixer to form at least two flow streams;
flowing each of the at least two flow streams through a separate third static mixer; and combining the at least two flow streams with a second part of the extraction liquid.
In yet another aspect of the present invention, a system for preparing microparticles is provided. The system includes a first and a second pump, and a first static mixer in fluid communication with each of the pumps. One of the pumps is configured to pump an organic phase into the first static mixer. One of the pumps is configured to pump a continuous phase into the first static mixer. A distributor, comprising a plurality of static mixers, is in fluid communication with the first static mixer. A third pump is configured, in fluid communication with the distributor, to pump an extraction liquid. A second static mixer is in fluid communication with the distributor. A flow rate from the first static mixer and the extraction liquid flow through the distributor and then through the second static mixer.
In another aspect, the system may include a third static mixer in fluid communication with the first static mixer and with the dispenser. The flow rate from the first static mixer and the extraction liquid are combined in the third static mixer, before flowing through the distributor. The system may also include a container in fluid communication with the second static mixer so that the flow rate from the second static mixer flows into the container. A fourth pump can also be provided to pump the extraction liquid into the second static mixer.
Other features of the invention are set forth in the dependent claims herein.
Features and Benefits
It is a feature of the present invention that it can be used to prepare microparticles, including microparticles containing an active agent.
It is another feature of the present invention that it contemplates parallel flow streams for in-line solvent extraction.
Yet another feature of the present invention is the ability to easily use different extraction liquids during the process. The system can be configured to introduce these different extraction liquids at the appropriate time and point of processing.
An advantage of the present invention is that it substantially reduces or eliminates the need for a separate quenching or extraction tank containing a large volume of quenching liquid to remove the solvent and to form hardened microparticles.
The present invention advantageously allows controlled extraction of the polymer solvent from a polymer / active agent droplet to form microparticles containing the active agent. The process advantageously provides a level of solvent removal sufficient for commercial products. The process also advantageously provides high loading efficiency, making it particularly useful for commercial products.
The process of the present invention advantageously provides a more consistent processing environment than conventional processes for forming microparticles. The inline solvent extraction process of the present invention allows all emulsion droplets to be exposed to the same processing conditions. In contrast, in conventional processes using an extraction tank or vessel, the processing conditions change over time as the solvent is withdrawn from the emulsion droplets in the tank.
The more consistent processing environment and conditions of the present invention advantageously result in a process that is less time or scale dependent than alternative processes.
The present invention provides a method and equipment that are particularly advantageous for scaling up. The parallel line distributor of the present invention takes into account capacity increases from an established system (single line) without full scale trial and error experiments on new and different equipment. The total flow rate can be increased from the single line system based on the number of flow streams in the manifold.
ES 2 236 035 T3
Brief description of the figures
The present invention is described with reference to the accompanying drawings. In the drawings, like reference numerals indicate identical or similar elements of functionality.
Fig. 1 shows an embodiment of an equipment configuration for preparing microparticles in accordance with the present invention;
Fig. 2 shows another embodiment of an equipment configuration for preparing microparticles in accordance with the present invention;
Fig. 3 illustrates flow through a static mixer; Y
Fig. 4 shows a static mixer suitable for use with the present invention.
Detailed Description of the Preferred Embodiments Summary
The present invention provides an improved process and equipment for preparing microparticles. The equipment and processes of the present invention use in-line solvent extraction to provide a process that is more scalable, with less overall processing time than conventional processes.
The processes of the present invention use a static mixer to combine a first phase, comprising an active agent and a polymer, with a second phase to form an emulsion. A process for forming an emulsion using a static mixer is described, for example, in US Patent No. 5,654,008. The phase comprising the active agent and the polymer may be referred to herein as the "organic phase". The other phase may be referred to herein as the "continuous phase."
The flow rate from the static mixer in which the emulsion is formed is combined with an extraction liquid in another static mixer which may be referred to herein as a "static mixing mixer". In one embodiment, the flow rate from the static mixing mixer flows into a vessel where it is combined with an additional extraction liquid which may be the same or different from the extraction liquid added to the static mixing mixer. In another embodiment, the flow rate of the static mixing mixer is divided into a plurality of flow streams that flow through a manifold containing a plurality of static mixers. The plurality of flow streams are subsequently recombined, and combined with additional extraction liquid. In a particularly preferred embodiment, the recombined flow streams and additional extraction liquid are combined in another static mixer, and this combining step is repeated until the starting volume of extraction liquid is exhausted. Such an embodiment eliminates the need for an extraction tank to extract solvent.
In the present invention, a static mixing mixer is used to combine the emulsion and the extraction liquid to form a combined flow stream. In one embodiment, the combined flow stream is divided into a plurality of flow streams to flow through the manifold. The use of the static mixing mixer prior to the dispenser is particularly advantageous because the emulsion and extraction liquid may not be immediately miscible or homogeneous, making splitting of the combined flow stream problematic. For multiphase streams such as emulsion and extraction liquid combined, using the manifold without the static mixing mixer could result in different compositions in each static mixer in the manifold. Since the combined emulsion and the extraction liquid are not homogeneous, they would not split evenly in a conventional pipe.
The configuration of the dispenser of the present invention is particularly advantageous for scaling up. The parallel line distributor of smaller diameter static mixers allows capacity increases from an established system (single line) without full scale trial and error experiments on new and different equipment. The total flow rate can be increased from the single line system based on the number of flow streams in the manifold.
To ensure clarity of the description that follows, the following definitions are provided. By "microparticles" or "microspheres" is meant solid particles that contain an active agent or other substance dispersed or dissolved within a polymer that serves as a matrix or binder for the particle. The polymer is preferably biodegradable and biocompatible. By "biodegradable" is meant a material that must be degraded by physical processes to products that are easily disposable by the body and must not accumulate in the body. The products of biodegradation must also be biocompatible with the body. By "biocompatible" is meant non-toxic to the body, it is pharmaceutically acceptable, it is not carcinogenic, and it does not significantly induce inflammation in body tissues. As used herein, "body" preferably refers to the human body, but it should be understood that body can also refer to a non-human animal body. By "% by weight" is meant parts by weight per total weight of microparticle. For example, 10% by weight of active agent would mean 10 parts of active agent by weight and 90 parts of polymer by weight. Unless otherwise indicated, the percentages (%) presented herein are by weight. By "controlled release microparticle"
ES 2 236 035 T3 or "sustained release microparticle" means a microparticle from which an active agent or other type of substance is released as a function of time. By "mass median diameter" is meant the diameter in which half of the distribution (percent by volume) has a larger diameter and half has a smaller diameter.
Procedure and examples
The following examples are provided to explain the invention, and to describe the materials and procedures used in carrying out the invention. The examples are not intended to limit the invention in any way. Example 1
Risperidone Microparticle Preparation
Microparticles comprising risperidone were prepared on a kilogram scale. The 1 kg procedure (400 grams of active agent and 600 grams of polymer) provides a theoretical drug loading of the microparticles of 40% (400 grams / 1000 grams x 100%).
A 16.7% polymer solution was prepared by dissolving 600 grams of MEDISORB® 7525 DL polymer (Alkermes, Inc., Blue Ash, Ohio) in ethyl acetate. A 24% drug solution was prepared by dissolving 400 grams of risperidone base (Janssen Pharmaceutica, Beerse, Belgium) in benzyl alcohol. The original phase was prepared by mixing the drug solution into the polymer solution. The continuous or aqueous phase was 30 kg of a 1% polyvinyl alcohol (PVA) solution containing 6.5% ethyl acetate.
The emulsification step used two positive displacement pumps that fed the individual phases (one pump for the organic phase and one pump for the aqueous phase) to a connecting junction where they were combined. A 5: 1 ratio of aqueous phase to organic phase was maintained throughout the emulsification step, at an average total flow rate of 3.2 kg / min. Immediately after the connecting joint in the process stream was a 1.27 centimeter diameter, 1.2 meter long in-line mixer. The outlet emulsion (static mixer flow rate) was then mixed with an amount of a first extraction solution which was pumped by a peristaltic pump at an average flow rate of 9 kg / min. The total volume of the first extraction solution that was transferred was 100 kg.
The combined stream (dilute mixture of emulsion and first extraction solution) was then passed through an in-line 1 inch diameter static mixer (16 inch long static mixer). The mixture was then passed through approximately 1.42 meters of a transfer line to reach 144 kg of a second extraction solution contained in a stirred holding vessel. The mixture was stirred for 4-6 hours in the holding vessel. Samples were taken periodically to determine levels of residual solvent (s), and to determine loading efficiency. Loading efficacy is the ratio, expressed as a percentage, of actual drug loading versus theoretical drug loading.
Two experiments were performed using the one kilogram risperidone partial inline extraction procedure described above. In Experiment One, the first and second extraction solutions both contained 2.5% ethyl acetate. In Experiment Two, the first extraction solution contained 2.5% ethyl acetate, and the second extraction solution was pure water.
Residual solvent levels and loading efficiencies obtained from the two experiments were compared to a control. The control was the average of four one-kilogram batches of risperidone microparticles prepared in the following manner. For each of the four control batches, the same steps were used to prepare the organic and aqueous phases as in the partial line extraction procedure described above, and the same emulsification step was also used. However, for each of the four control batches, the emulsion exiting the first static mixer was then transferred to a holding vessel containing an aqueous extraction solution containing 2.5% ethyl acetate.
A comparison of the results obtained in Experiments One and Two with the risperidone control is shown below in Table 1. Table 1 shows the residual solvent level for both ethyl acetate (Ac / Et) and benzyl alcohol ( AB) for Experiments One and Two and the control. As shown in Table 1, the residual solvent levels for experiment one (3.6 / 5.1%) were comparable to the residual solvent levels for the risperidone control (3.0 / 5.0%). . In Experiment Two, the solvent level of the residual BA (9.5%) was significantly higher than the solvent level of the BA from the riperidone control (5.0%). The extraction rate of each solvent is affected by the concentration of ethyl acetate in the extraction solution, for example as described in US Patent No. 5,650,173. The results obtained in Experiment Two for the residual benzyl alcohol level of 9.5% were comparable, however, with another processed risperidone control without initial ethyl acetate component in the extraction solution, resulting in a level of Benzyl alcohol in 9.3% microparticles. The lower level of residual solvent for ethyl acetate in Experiment Two (0.9%) is also probably the result of the lack of ethyl acetate in the second extraction solution.
ES 2 236 035 T3
TABLE 1
<td></td><td colspan="2">Risperidone procedure Partial online extraction</td><td>Risperidone control</td>
<td>Experiment</td><td>One</td><td>Two</td><td>Average 1 kg</td>
<td>Residual solvents (AcEt / AB)</td><td> 3,6/5,1%</td><td> 0,9/9,5%</td><td> 3,0/5,0%</td>
<td>Charging efficiency</td><td> 92,2%</td><td> 88,0%</td><td> 93,2%</td>
As shown in Table 1, the loading efficiency of Experiment One (92.2%) was comparable to that of the risperidone control (93.2%). The 93.2% loading efficiency for the risperidone control is the loading efficiency of the final microparticle product after the levels of the residual ethyl acetate and benzyl alcohol solvent are reduced to 1-2%. The loading efficiency for the same product containing 5-9% residual solvent levels of ethyl acetate and benzyl alcohol is expected to be lower due to mass balance. This is consistent with the results obtained in Experiment Two, with a lower loading efficiency of 88.0%.
Example 2
Preparation of bupivacaine microparticles
Microparticles comprising bupivacaine were prepared on a twenty gram scale. The 20 gram procedure (4 grams of active agent and 16 grams of polymer) provides a theoretical drug loading of the microparticles of 20% (4 grams / 20 grams x 100%).
Sixteen grams of MEDISORB® 7525 DL polymer (Alkermes, Inc., Blue Ash, Ohio) and four grams of bupivacaine base were dissolved in 230 grams of ethyl acetate to make the organic phase. The aqueous phase consisted of a 1% PVA solution containing a saturating amount of polymer solvent (ethyl acetate), with a pH of 8.5 and a trizma buffer concentration of 0.05 molar. The extraction solution was an aqueous solution buffered with 0.05 molar trizma at a pH of 8.5.
The emulsification step used two positive displacement pumps that fed the individual phases (one pump for the organic phase and one pump for the aqueous phase) to a connecting junction where they were combined. The organic phase pump ran at 75 ml / min, and the aqueous phase pump ran at 150 ml / min. A 3: 1 ratio of aqueous phase to organic phase was maintained throughout the emulsification step. Immediately after the connecting joint was a 0.64 centimeter diameter, 44.5 centimeter long in-line mixer. The outlet emulsion (static mixer flow rate) was then mixed with an amount of the extraction solution which was pumped by a positive displacement pump at a ratio of extraction solution to emulsion of 1: 1. This extraction solution pump ran at 225 ml / min.
The combined stream (dilute mixture of emulsion and first extraction solution) was then passed through a 0.95 centimeter diameter in-line static mixer (static mixing mixer) 12.06 centimeters long. Even though solvent extraction is being performed in the static mixing mixer, at this point in the process stream, the microdroplets of the emulsion have not fully hardened, and additional processing is needed to ensure the desired particle size. The static mixing mixer flow rate was divided into two flow streams, each then passing through a separate in-line static mixer 0.64 centimeters in diameter and 15.24 centimeters in length. The two flow streams create less shear stress in each flow stream, tending to create larger microparticles. With just a large flow stream, there can be enough shear stress that results in smaller microparticles. The two flow streams were then recombined, and added to a flow stream of the extraction solution which was pumped by a positive displacement pump operating at 450 ml / min. The resulting flow stream was passed through a 1.27 centimeter diameter in-line static mixer that was 12 inches long, and was then collected in an initially empty holding vessel. The two extraction solution pumps started at the same time as the aqueous phase pump, and ran continuously.
After the organic phase was exhausted, the contents in the holding vessel were carefully mixed using an overhead stirrer and the remainder of the extraction solution was transferred to the holding vessel. The mixture was stirred for one hour. The microparticles were recovered on a 25 micron screen, dried in a laboratory hood overnight, and analyzed for residual solvent level and loading efficiency.
The residual solvent level and loading efficiency obtained from the bupivacaine procedure of 20
ES 2 236 035 T3 grams were compared to a 20 gram bupivacaine control. The 20 gram bupivacaine control was made using the same aqueous, organic, extraction solution, and concentrations thereof, as in the bupivacaine on-line extraction procedure described above. The emulsification step was the same as described above, except for the use of a 0.64 centimeter diameter, 40.64 centimeter long in-line static mixer to create the emulsion. The emulsion exiting this static mixer was then transferred to the total volume of the extraction solution that was contained in the stirred holding vessel.
A comparison of the results obtained using the bupivacaine online extraction procedure ("bupivacaine procedure") with the bupivacaine control is shown below in Table 2. As shown in Table 2, the residual solvent level for the bupivacaine procedure is identical to the residual solvent level for the bupivacaine control (4.2%). The loading efficiency for the bupivacaine procedure (75%) is comparable to the loading efficiency for the bupivacaine control (88.5%).
<td></td><td>Bupivacaine procedure Online extraction</td><td>Bupivacaine control</td>
<td>Lot Size</td><td>20 grams</td><td>20 grams</td>
<td>Residual solvent (AcEt)</td><td> 4,2%</td><td> 4(2%</td>
<td>Charging efficiency</td><td> 75%</td><td> 88,5%</td>
Examples 1 and 2 demonstrate that the process of the present invention allows the controlled extraction of polymer solvent from a polymer / active agent droplet to form microparticles containing the active agent. Each of the emulsion droplets is exposed to substantially the same processing conditions throughout the process. The initial setting of the emulsion droplets is not time or scale dependent, as in conventional encapsulation procedures. The process of the present invention provides a sufficient level of solvent removal for conventional products. The process also provides great loading efficiency, making it particularly useful for commercial products. Example 3
Procedures for preparing microparticles
As exemplified by the examples discussed above, the processes for preparing microparticles according to the present invention will now be described in more detail. Exemplary equipment for carrying out such procedures will be described below. In one embodiment of the present invention, a first phase is prepared, comprising an active agent and a polymer. In one embodiment of the present invention, the first phase is prepared by dissolving the active agent in a first solvent to form an active agent solution. The polymer dissolves in a second solvent to form a polymer solution. The active agent solution and the polymer solution are mixed to form the first phase. In a particularly preferred embodiment, the active agent is selected from the group consisting of risperidone, 9-hydroxyrisperidone, and pharmaceutically acceptable salts thereof. In one such embodiment, a first preferred solvent is benzyl alcohol, and a second preferred solvent is ethyl acetate.
In another embodiment of the present invention, the first phase is prepared by dissolving the active agent and the polymer in a solvent to form a solution. In a particularly preferred embodiment, the active agent is bupivacaine, and the solvent is ethyl acetate. It should be understood that the present invention is not limited to any particular procedure by which the first phase is prepared, and other suitable procedures would be clearly apparent to one of ordinary skill in the art.
A second phase is prepared, and combined with the first phase in a first static mixer to form an emulsion. In a preferred embodiment, the two phases are pumped into the static mixer, the second phase being pumped at a flow rate greater than the flow rate of the first phase. In a preferred embodiment, the ratio of the second phase flow rate to the first phase flow rate is approximately 2: 1. Exemplary second phase volume to first phase volume ratios are approximately 5: 1 and approximately 3: 1. However, one skilled in the art should understand that the present invention is not limited to such flow rate or volume ratios, and other appropriate flow ratios and volume ratios would be clearly apparent to one of ordinary skill in the art.
The emulsion is combined with a first extraction liquid in a second static mixer. In a preferred embodiment, the first extraction liquid is pumped at a first rate into the emulsion that flows out of the first static mixer to form a first combined stream. The first combined stream is then allowed to flow through the second static mixer. The volume ratio of the emulsion to the first extraction liquid can be about 1: 1, although it should be clearly apparent to one of ordinary skill in the art that other volume ratios can be used. In one embodiment, the second static mixer comprises
ES 2 236 035 T3 a plurality of individual static mixers configured to provide a plurality of parallel flow streams. In a particularly preferred embodiment, the plurality of individual static mixers is two. However, one skilled in the art should understand that the present invention is not limited to the use of two individual static mixers in such a configuration, and appropriate numbers of individual static mixers would be clearly apparent to one skilled in the art.
The flow rate from the second static mixer is combined with a second extraction liquid. The second extraction liquid can be the same as or different from the first extraction liquid. The second extraction liquid can be the same as, or different from, the second phase. Similarly, the first extraction liquid can be the same as, or different from, the second phase.
In one embodiment of the present invention, the flow rate from the second static mixer flows into a vessel containing the second extraction liquid. In an alternative embodiment, the flow rate from the second static mixer flows into the container, and the second extraction liquid is added to the container. The second extraction liquid can be added to the vessel while the flow rate from the second static mixer is flowing into the vessel, or after the flow rate from the second static mixer has fully flowed into the vessel.
In a further embodiment of the present invention, the flow rate from the second static mixer is combined with the second extraction liquid in a third static mixer. Preferably, the second extraction liquid is pumped at a second rate into the flow rate of the second static mixer to form a second combined stream, and the second combined stream is allowed to flow through the third static mixer. In one embodiment, the second pumping speed of the second extraction liquid is greater than the first pumping speed of the first extraction liquid. However, the present invention is not limited to such pumping speeds, and suitable pumping speeds would be clearly apparent to one of ordinary skill in the art.
The third static mixer may be a single static mixer, a plurality of individual static mixers arranged in series, or a plurality of static mixers configured to provide a plurality of parallel flow streams. The flow from the third static mixer flows into a vessel. The container may be empty before allowing the flow from the third static mixer to flow into it. Alternatively, the vessel may contain an extraction liquid or other type of quenching solution before allowing the flow from the third static mixer to flow into it.
An alternative process for preparing microparticles in accordance with the present invention will now be described. A first phase is prepared, comprising an active agent and a polymer. A second phase is prepared, and combined with the first phase in a first static mixer to form an emulsion, the emulsion forming a flow from the first static mixer. Proper procedures for preparing the first and second stages, and for combining in the first static mixer, have been described above and will not be repeated here for brevity.
The flow from the first static mixer is combined with a first part of a starting volume of an extraction liquid in a second static mixer to form a flow from the second static mixer. The extraction liquid can be the same or a different one from the second phase. The second static mixer may be a single static mixer, a plurality of individual static mixers arranged in series, or a plurality of individual static mixers configured to provide a plurality of parallel flow streams.
The flow rate from the second static mixer is divided to form at least two flow streams. Each of the at least two flow streams flows through a separate static mixer. The third distinct static mixer may be a single static mixer, one of a plurality of individual static mixers arranged in series, or one of a plurality of individual static mixers configured to provide a plurality of parallel flow streams.
The at least two flow streams are combined with a second part of the extraction liquid. In an alternative embodiment of the present invention, the at least two flow streams are combined with another extraction liquid different from the first part of the extraction liquid. This other extraction liquid can be the same or a different one from the second phase.
In one embodiment of the present invention, the at least two flow streams are combined with the second part of the extraction liquid by allowing the at least two flow streams to flow into a container containing the second part of the extraction liquid. In an alternative embodiment, the at least two flow streams are combined with the second part of the extraction liquid in a fourth static mixer. The flow from the fourth static mixer can then flow into a vessel. In a particularly preferred embodiment, the at least two flow streams are combined with the second part of the extraction liquid in a fourth static mixer, and this combining step is continued until the starting volume of the extraction liquid is exhausted.
Microparticles of the present invention
Microparticles prepared by the process of the present invention preferably comprise a polymeric binder, but one skilled in the art should understand that the present invention is not limited to the preparation of microparticles comprising a polymeric binder. Polymeric Binder Materials
Suitable ES 2 236 035 T3 include poly (glycolic acid), poly-d, 1-lactic acid, poly-1-lactic acid, copolymers of the above, poly (aliphatic carboxylic acids), copolyoxalates, polycaprolactone, polydioxanone, poly (ortho carbonates), poly (acetals), poly (lactic acid-caprolactone), polyorthoesters, poly (glycolic acid-caprolactone), polyanhydrides, polyphosphazines, albumin, casein, and waxes. Poly (d, 1-lactic-co-glycolic acid) is commercially available from Alkermes, Inc. (Blue Ash, OH). A suitable product commercially available from Alkermes, Inc. is a 50:50 poly (d, 1-lactic-coglycolic acid) known as MEDISORB® 5050 DL. This product has a molar percentage composition of 50% lactide and 50% glycolide. Other suitable commercially available products are MEDISORB<sup>®</sup> 6535 DL, 725 DL, 8515 DL and poly (d, 1-lactide acid) (100 DL). Poly (lactide-co-glycolides) are also commercially available from Boehringer Ingelheim (Germany) under their brand name Resomer®, for example PLGA 50:50 (Resomer® RG 502), PLGA 75:25 (Resomer® RG 752) and d , 1-PLA (Resomer® RG 206), and from Birmingham Polymers (Birmingham, Alabama). These copolymers are available in a wide range of molecular weights and lactic acid versus glycolic acid ratios.
One type of microparticle suitable for preparation by the present invention is a sustained release microparticle that is biodegradable. However, one skilled in the art should understand that the present invention is not limited to biodegradable or other sustained release microparticles. As would be apparent to one skilled in the art, the molecular weight of the polymeric binder material for biodegradable microparticles is of some importance. The molecular weight must be large enough to allow the formation of satisfactory polymer coatings, that is, the polymer must be a good film former. Typically, a satisfactory molecular weight is in the range of 5,000 to 500,000 daltons, preferably about 150,000 daltons. However, since the properties of the film are also partially dependent on the particular polymeric binder material being used, it is very difficult to specify an appropriate molecular weight range for all polymers. The molecular weight of the polymer is also important from the point of view of its influence on the rate of biodegradation of the polymer. For a dysfusional drug release mechanism, the polymer must remain intact until all of the drug is released from the microparticles and then degraded. The drug can also be released from the microparticles as the polymeric binder bioeroses. By appropriate selection of polymeric materials, a microparticle formulation can be made in which the resulting microparticles display both diffusional release and biodegradation release properties. This is useful according to multiphase release models.
The microparticles prepared in accordance with the present invention may include an active agent or other type of substance that is released from the microparticles into the host. Such active agents can include 1,2-benzazoles, more particularly, 1,2-benzisoxazoles and 3-piperidinyl substituted 1,2-benzisothiazoles. The most preferred active agents of this type are 3- [2- [4- (6-fluoro-1,2-benzisoxazol-3-yl) -1-piperidinyl] ethyl] -6,7,8,9-tetrahydro2- methyl-4H-pyrido [1,2-a] pyrimidin-4-one ("risperidone") and 3- [2- [4- (6-fluoro-1,2-benzisoxazol-3-yl) -1-piperidinyl ] ethyl] 6,7,8,9-tetrahydro-9-hydroxy-2-methyl-4H-pyrido [1,2-a] pyrimidin-4-one ("9-hydrorrisperidone") and the pharmaceutically acceptable salts thereof . Risperidone (which term, as used herein, is intended to include its pharmaceutically acceptable salts) is most preferred. Risperidone can be prepared in accordance with the teachings of US Patent No. 4,804,663, the entirety of which is incorporated herein by reference. 9-Hydrorrisperidone can be prepared in accordance with the teachings of US Patent No. 5,158,952, the entirety of which is incorporated herein by reference.
Other biologically active agents include non-steroidal antifertility agents; parasympathomimetic agents; psychotherapeutic agents; major tranquilizers such as chlorpromazine HCl, clozapine, mesoridazine, metiapine, reserpine, thioridazine, and the like; minor tranquilizers such as chlordiazepoxide, diazepam meprobamate, temazepam, and the like; rhinological decongestants; sedative-hypnotics such as codeine, phenobarbital, sodium pentobarbital, sodium secobarbital, and the like; steroids such as testosterone and testosterone propionate; sulfonamides; sympathomimetic agents; vaccines; vitamins and nutrients such as essential amino acids; essential fats and the like; antimalarials such as 4-aminoquinolines, 8-aminoquinolines, pyrimethamine, and the like; anti-migraine agents such as mazindol, phentermine, and the like; anti-Parkinson agents such as L-dopa; anti-spasmodics such as atropine, methscopolamine bromide, and the like; antispasmodic and anticholinergic agents such as biliary, digestive, enzyme therapy, and the like; antitussives such as dextromethorphan, noscapine, and the like; bronchodilators; cardiovascular agents such as anti-hypertensive compounds, Rauwolfia alkaloids, coronary vasodilators, nitroglycerin, organic nitrates, pentaerythrotetranitrate, and the like; electrolyte substitutes such as potassium chloride; ergot alkaloids such as ergotamine with and without caffeine, hydrogenated ergot alkaloids; dihydroergocristine methanesulfate, dihydroergocornine methanesulfonate, dihydroergocriptine methanesulfate, and combinations thereof; alkaloids such as atropine sulfate, Belladonna, hyoscine hydrobromide, and the like; analgesics, narcotics such as codeine, dihydrocodienone, meperidine, morphine, and the like; non-narcotics such as salicylates, aspirin, acetaminophen, d-propoxyphene, and the like; antibiotics such as salicylates, aspirin, acetaminophen, d-propoxyphene, and the like; antibiotics such as cephalosporins, chloroamphenical, gentamicin, kanamycin A, kanamycin B, penicillins, ampicillin, streptomycin A, antimycin A, chloropamteniol, metromidazole, penicillin G, oxytetracyclinics, tetracyclines, and the like; anticancer agents anti-convulsants such as mephenytoin, phenobarbital, trimethadione; anti-emetics such as thiethylperazine; antihistamines such as chlorofinazine, dimenhydrinate, diphenhydramine, perphenazine, tripelenamine, and the like; anti-inflammatory agents, such as hormonal agents, hydrocortisone, prednisolone, prednisone, non-hormonal agents, allopurinol, aspirin, indomethacin, phenylbutazone, and the like; prostaglandins; cytotoxic drugs such as thiotepa; chlorambucil, cyclophosphamide, melphalan, nitrogen mustard, methotrexate, and the like; antigens of microorganisms such as Neisseria gonorrhea, Mycobacterium tuberculosis, Herpes virus (homonis, types 1 and 2), Candida albicans, Tropical Candida, Trichomonas vaginalis, Haemophilus vaginalis, Streptococcus ecoli Group B, Mycoplasma hominis,
ES 2 236 035 T3
Haemophilus ducreyi, Granuloma inguinale, Lymphopathia venereum, Treponema pallidum, Brucella abortus, Brucella melitensis, Brucela suis, Brucela canis, Campylobacterfetus, Campylobacterfetus intestinalis, Leptospira pomona, Listeria monocytogenes virus, Herpes viruses equinocytogenes 1, Herpes arteritis virus equinovirus 1, Herpes viruses equinovisitis virus IBR-IBP, BVDMB virus, Chlamydia psittaci, Trichomonas fetus, Toxoplasma gondii, Escherichia coli, Actinobacillus equuli, Salmonella abortus ovis, Salmonella abortus equi, Pseudomonas aeruginosa, Corynebacterium equi, Corynebacterium pyogenes, Actinobacillus seminis, Mycoplasma bovigenitalium, Aspergillus fumigatus, Absidia ramosa, Trypanosoma equiperdum, Babesia caballi, Clostridium tetani, and the like; antibodies that counteract the above microorganisms; and enzymes such as ribonuclease, neuramidinase, trypsin, glycogen phosphorylase, sperm lactic dehydrogenase, sperm hyaluronidase, adenosine triphosphatase, alkaline phosphatase, alkaline phosphatase esterase, amino peptidase, trypsin, chymotrypsin, amylautic acid protease, protease, muraminehydroenase, amylase, protease, muramidathylase, protease, muramidahydrogens , succinic acid dehydrogenase, beta-glyphosphatase, lipase, gamma-glutamylotranspeptidase alpha-peptate ATP-ase, sterol3-beta-ol-dehydrogenase, and DNP-di-aprorase.
Other suitable active agents include estrogens such as diethyl stilbestrol, 17-beta-estradiol, estrone, ethinyl estradiol, mestranol, and the like; progestins such as norethindrone, norgestril, ethinodiol diacetate, linestrenol, medroxyprogesterone acetate, dimestisterone, megestrol acetate, chlormadinone acetate, norgestimate, norethisterone, ethisterone, melengestrol, norethindrel and the like; and spermicidal compounds such as nonylphenoxypolyoxyethylene glycol, benzethonium chloride, chlorindanol, and the like.
Other suitable active agents include antifungals, antivirals, anticoagulants, anticonvulsants, antidepressants, antihistamines, hormones, vitamins and minerals, cardiovascular agents, peptides and proteins, nucleic acids, immunological agents, antigens of such bacterial organisms such as Streptococcus pneumoniae, Haemophilus influenzae, Staphylococcus a. , Streptococcus pyogenes, Corynebacterium diphtheriae, Bacillus anthracis, Clostridium tetani, Clostridium botulinum, Clostridium perfringens, Streptococcus mutans, Salmonella typhi, Haemophilusparainfluenzae, Bordetella pertussis, Francisella tularensis, Yersinia pestis, Vibrio cholerae, Legionella pneumophila, Mycobacterium leprae, Leptospira interrogans, Borrelia, burgbacteria viruses, such as smallpox virus, Aubergine virus, and Campyri virus respiratory syncytial, parainfluenza, measles, HIV, varicella-zoster, herpes simplex 1 and 2, cytomegalovirus, Epstein-Barr, rotavirus, rhinovirus, adenovirus, papillomavirus, poliovirus, mumps, rabies, rubella, coxsakievirus, equine encephalitis, Japanese encephalitis, yellow fever, Rift Valley fever, lymphocytic choriomeningitis, hepatitis B, antigens of such fungal protozoa, and parasitic organisms such as Cryptococcus neoformans, Histoplasma capsulatum, Candida capsulatum , Candida tropicalis, Nocardia asteroides, Rickettsia ricketsii, Rickettsia typhi, Mycoplasma pneumoniae, Chlamydia psittaci, Chlamydia trachomatis, Plasmodium falciparum, Trypanosoma brucei, Entamoeba histolytica, Toxoplasma gondii, Trichomonas vaginalis, Schistosoma mansoni. These antigens can be in the form of completely killed organisms, peptides, proteins, glycoproteins, carbohydrates, or combinations of these.
Other macromolecular bioactive agents that can be selected for incorporation include, but are not limited to, blood clotting factors, hematopoietic factors, cytokines, interleukins, colony stimulating factors, growth factors, and analogs and fragments thereof.
Microparticles can be mixed by size or by type. However, it should be understood that the present invention is not limited to the use of biodegradable or other microparticles containing an active agent. In one embodiment, the microparticles are mixed in a way that provides active agent delivery to the patient in a multiphasic fashion and / or in a way that provides different active agents to the patient at different times, or a mixture of active agents at the same time. . For example, secondary antibiotics, vaccines, or any desired active agent, in microparticulate or conventional non-encapsulated form can be mixed with a primary active agent and delivered to the patient.
Team
Turning now to Figure 1, one embodiment of the equipment of the present invention is shown (system 100). A first stage (110) and a second stage (120) are pumped by a pump (112) and a pump (122), respectively, into a first static mixer (130) to form an emulsion. The first phase preferably comprises an active agent and a polymer, and is preferably in the form of a solution. The second phase is preferably an aqueous solution that functions as the continuous phase of the emulsion.
A static mixer is made up of a conduit or tube in which several static mixing elements are received. Static mixers provide uniform mixing in a relatively short length of the conduit, and in a relatively short period of time. With static mixers, the fluid moves through the mixer, rather than some part of the mixer, such as a blade, moving through the fluid. Flow through one type of static mixer is illustrated in Figure 3. A pump (not shown) introduces a stream of one or more fluids into a static mixer (10), as generally shown in (1). The stream splits and is forced to the opposing outer walls, as generally shown in (2). An axial vortex is created to the center line of the static mixer (10), as generally shown in (3). The eddy is cut off and the process is repeated, but with the opposite rotation, as generally shown in (4). The clockwise / counter-clockwise movement ensures a homogeneous product.
An example of a static mixer is shown in Figure 4. The static mixer (10) includes several elements
ES 2 236 035 T3 stationary or static mixers (14) arranged in a series within a conduit or pipe (12). The number of static mixing elements can vary between 4 and 32 or more. Conduit 12 is circular in cross section and open at opposite ends (18) and (20) to introduce and extract fluids. Mixing element 14 comprises segments (42). Each segment (42) is formed by several generally flat plates or paddles (44). The two substantially identical segments 42 are generally zigzagged axially relative to each other. A static mixer as shown in Figure 4 is more fully described in US Patent No. 4,511,258, the entirety of which is incorporated herein by reference.
The emulsion is combined with a first extraction liquid (150), pumped by means of a pump (152), in a second static mixer (140). The static mixer (140) functions as a static mixing mixer to mix the emulsion and the first extraction liquid. The flow from the second static mixer (140) flows into a vessel (160). In one embodiment of the present invention, the container (160) contains a second extraction liquid. The second extraction liquid can be the same or a different one from the first extraction liquid. In further embodiments of the invention, the second phase 120 can be used as the first extraction liquid and / or the second extraction liquid.
In another embodiment of the present invention, the flow rate from the second static mixer (140) flows into the container (160), and the second extraction liquid is added to the container (160). The second extraction liquid can be added to the container (160) while the flow rate from the second static mixer (140) is flowing into the container (160), or after the second static mixer (140) has completely flowed into the container ( 160).
Static mixer (140) is shown in Figure 1 as a single static mixer. Alternatively, the static mixer (140) could be configured as a manifold that includes a plurality of individual static mixers arranged in parallel to provide a plurality of parallel flow streams, as shown, for example, by the manifold (240) illustrated at Figure 2. Alternatively, the static mixer (140) could be configured as a plurality of individual static mixers arranged in series. Similarly, the static mixer (130) could also be configured as a manifold that includes a plurality of individual static mixers arranged in parallel, or as a series of individual static mixers. One skilled in the art should understand that the present invention is not limited to the use of a single static mixer for any of the elements depicted as individual static mixers in the Figures. As would be clearly apparent to one skilled in the art, a plurality of individual static mixers arranged in series could be used, or a manifold containing a plurality of individual static mixers arranged in parallel could also be used to provide a plurality of parallel flow streams. .
Another embodiment of the invention is shown in Figure 2 (system 200). A first stage (210) and a second stage (220) are pumped by a pump (212) and a pump (222), respectively, into a first static mixer (230) to form an emulsion. The first phase preferably comprises an active agent and a polymer, and is preferably in the form of a solution. The second phase is preferably an aqueous solution that functions as the continuous phase of the emulsion.
The emulsion is combined with a first part of an extraction liquid (250), it is pumped by means of a pump (252), in a static mixer (235). The static mixer (235) functions as a static mixing mixer to mix the emulsion and the first extraction liquid. The flow rate from the static mixer (235) is divided into a plurality of flow streams that flow within a manifold (240). Distributor (240) includes a plurality of individual static mixers (242) configured in a parallel arrangement providing a plurality of parallel flow streams. Although Figure 2 shows three separate and individual static mixers (242) in the manifold (240), it should be clearly apparent to one of ordinary skill in the art that the manifold (240) can be configured with more or fewer static mixers (242). ) individual. In a preferred embodiment, the manifold (240) includes two individual static mixers (242), and the flow rate from the static mixer (235) is divided into two flow streams, with each of the two flow streams flowing through one of the two flow streams. the two individual static mixers.
The flow rates from the individual static mixers (242) combine to form the flow rate from the distributor (240). The flow from the distributor (240) is combined with a second part of extraction liquid (250), pumped by means of a pump (254), in another static mixer (270). In an alternative embodiment of the present invention, the manifold (240) is replaced by a single static mixer located between the static mixer (235) and the static mixer (270). In another alternate embodiment, the manifold (240) is replaced by a plurality of individual static mixers arranged in series. As would be clearly apparent to one skilled in the art, the static mixers (230), (235), and (270) depicted in Figure 2 as individual static mixers could be replaced by a plurality of individual static mixers arranged in series, or by a dispenser containing a plurality of individual static mixers arranged in parallel.
In one embodiment, the pump (254) is configured to operate at a flow rate greater than a flow rate of the pump (252). It should be understood that the present invention is not limited to such a flow rate setting, and other suitable flow rates would be clearly apparent to one skilled in the art.
The flow from the distributor (240) is combined with the extraction liquid (250) in a static mixer (270),
ES 2 236 035 T3 and this combination is repeated until the starting volume of the extraction liquid (250) is exhausted. Once the starting volume of the extraction liquid (250) is exhausted, the flow rate from the static mixer (270) flows into a container (260) which is preferably initially empty, that is, does not contain any extraction liquid. In this way, all the extraction liquid (250) is introduced into the processing stream, and is combined with the emulsion in one of the static mixers.
In system 200 as shown in Figure 2, extraction liquid (250) is introduced into the process stream at two different points by pumps (252) and (254). In an alternative embodiment of the system (200), an extraction liquid could be introduced by the pump (252), and a different type of extraction liquid could be introduced by the pump (254). In a further embodiment, the second stage (220) could be used as one or both of the extraction liquids introduced via the pumps (252) and (254).
Alternatively, the system (200) could be modified to eliminate the static mixer (270) so that the flow rate from the distributor (240) would flow into the container (260) containing the second part of the extraction liquid (250). The system (200) could also be modified to add additional static mixers (270) in which additional portions of extraction liquid (250), or a different type of extraction liquid, are combined with the flow stream.
Conclution
Although various embodiments of the present invention have been described above, it should be understood that they have been presented by way of example only, and not by way of limitation. The present invention is not limited to the preparation of controlled release microparticles, nor is it limited to a particular active agent, polymer or solvent, nor is the present invention limited to a particular scale or batch size. Thus, the breadth and scope of the present invention should not be limited by any of the exemplary embodiments described above, but should be defined solely in accordance with the following claims and their equivalents.
Contents7
4 sheets
Sheet 1 Sheet 2 Sheet 3 Sheet 4
56 members in 12 offices
Priority claims2
| Document | Office | Kind | Date |
|---|---|---|---|
| 19990438656 | United States of America | – | |
| 43865699 | United States of America | A |
Members56
| Document | Office | Kind | |
|---|---|---|---|
| CA2390284A1 | Canada | A1 | |
| CA2390563A1 | Canada | A1 | |
| WO0134113A2 | World Intellectual Property Organization (WIPO) | A2 | |
| WO0134120A1 | World Intellectual Property Organization (WIPO) | A1 | |
| AU2750801A | Australia | A | |
| AU3437901A | Australia | A | |
| US2001031801A1 | United States of America | A1 | |
| US6331317B1 | United States of America | B1 | |
| WO0134120B1 | World Intellectual Property Organization (WIPO) | B1 | |
| WO0134113A3 | World Intellectual Property Organization (WIPO) | A3 | |
| US6395304B2 | United States of America | B2 | |
| EP1231898A2 | European Patent Office (EPO) | A2 | |
| EP1242053A1 | European Patent Office (EPO) | A1 | |
| US2002146461A1 | United States of America | A1 | |
| US6495166B1 | United States of America | B1 | |
| US6537586B2 | United States of America | B2 | |
| US6540393B1 | United States of America | B1 | |
| JP2003513710A | Japan | A | |
| JP2003513905A | Japan | A | |
| US2003133357A1 | United States of America | A1 | |
| US2003147967A1 | United States of America | A1 | |
| US6705757B2 | United States of America | B2 | |
| AU771497B2 | Australia | B2 | |
| US6713090B2 | United States of America | B2 | |
| AU773734B2 | Australia | B2 | |
| US2004197469A1 | United States of America | A1 | |
| US2004247688A1 | United States of America | A1 | |
| EP1242053B1 | European Patent Office (EPO) | B1 | |
| AT286722T | Austria | T | |
| ATE286722T1 | Austria | T1 | |
| DE60017461D1 | Germany | D1 | |
| US6861016B2 | United States of America | B2 | |
| PT1242053E | Portugal | E | |
| DK1242053T3 | Denmark | T3 | |
| ES2236035T3This record | Spain | T3 | |
| US6939033B2 | United States of America | B2 | |
| US2005196457A1 | United States of America | A1 | |
| US2005266091A1 | United States of America | A1 | |
| DE60017461T2 | Germany | T2 | |
| EP1231898B1 | European Patent Office (EPO) | B1 | |
| AT349201T | Austria | T | |
| ATE349201T1 | Austria | T1 | |
| DE60032631D1 | Germany | D1 | |
| PT1231898E | Portugal | E | |
| DK1231898T3 | Denmark | T3 | |
| ES2277867T3 | Spain | T3 | |
| DE60032631T2 | Germany | T2 | |
| US7300671B2 | United States of America | B2 | |
| US2008053904A1 | United States of America | A1 | |
| US2008054220A1 | United States of America | A1 | |
| JP4146639B2 | Japan | B2 | |
| CA2390284C | Canada | C | |
| CA2390563C | Canada | C | |
| US7510730B2 | United States of America | B2 | |
| CY1106372T1 | Cyprus | T1 | |
| JP4838471B2 | Japan | B2 |
Numbers
- Publication
- 2236035
- Application
- 990484
Titles2
- Spanish
- EQUIPO Y PROCEDIMIENTO PARA PREPARAR MICROPARTICULAS USANDO EXTRACCION POR DISOLVENTE EN LINEA.
- English
- EQUIPMENT AND PROCEDURE TO PREPARE MICROPARTICLES USING EXTRACTION BY SOLVENT ONLINE.
Classification
- CPC, 7
- A61K9/1694
- A61K9/1647
- Y10T428/2989
- A61P23/02
- A61P25/18
- A61P25/22
- A61P25/24
- IPC, 7
- A61K9 16
- A61K9 50
- A61K31 519
- A61P25 18
- B01F1 00
- B01F3 08
- B01F5 00