Soft and flexible foams produced from a mixture of alkenyl aromatic polymers and alpha-olefin/vinyl- or vinylidene aromatic and/or sterically protected aliphatic or cycloaliphatic vinyl or vinylidene interpolymers

Soft and flexible foams made from a mixture of alkenylaromatic polymers and alphaolefin / vinyl- or vinylidene-aromatic and / or sterically hindered aliphatic or cycloaliphatic vinyl or vinylidene interpolymers (57)

one monomer selected from the group consisting of ethylene and / or 3 to 20 carbon atoms; and (3) 0 to 20 mole percent polymer units derived from at least one ethylenically unsaturated polymerizable monomer, wherein the polymerizable monomer is not monomers derived from the monomers described in (1) and (2); and (C) optionally at least one nucleating agent; (D) optionally at least one additional additive; and (E) at least one blowing agent, wherein the total amount of the components is (C) + (D) + (E) 0.4 to 5.0 grammols / kilogram based on the total weight of components A and B.

CZ 2001 -1985 A3

The soft foam comprises (A) 30 to 70% by weight, based on the total weight of components A and B, of at least one alkenylaromatic polymer having a weight average molecular weight (M)_w) between 100,000 and 500,000; and (B) 30 to 70% by weight, based on the total weight of components A and B, of at least substantially statistical interpolymers whose melt index I₂ is 0.1 grams / 10 minutes to 50 grams / 10 minutes and has a molecular weight distribution (MJMJ) in the range of 1.5 to 20, wherein the interpolymer comprises (1) 8 to 45 mole percent polymer units derived from: (a) at least one vinyl or vinylidene aromatic monomer, or (b) at least one sterically hindered aliphatic or cycloaliphatic vinyl or vinylidene monomer, or (c) a combination of at least one aromatic vinyl or vinylidene monomer and at least one sterically hindered aliphatic or cycloaliphatic vinyl or vinylidene monomer; and (2) 55 to 92 mole percent of polymer units derived from at least

<img file="CZ20011985A3_D0001.tif" />

<img file="CZ20011985A3_D0002.tif" />

<img file="CZ20011985A3_D0003.tif" />

PV Qjtot-JWr 9 · 9 · · 4 · 9 4 4 9 9 · · · · · · · · · · · ···· In · ·· ·· ··· nsdnwwaž

Soft and flexible foams made from mixtures of alkenylaromatic polymers and α-olefin / vinyl- or vinylidene-aromatic and / or spherically impeded aliphatic or cycloaliphatic vinyl or vinylidene interpolymers

Technical field

The present invention relates to a process for producing soft and flexible foams by foaming polymer blends comprising (A) alkenylaromatic polymers and (B) vinyl or vinylidene aromatic and / or sterically hindered aliphatic or cycloaliphatic vinyl or vinylidene substantially random interpolymers. Suitable alkenylaromatic polymers include alkenylaromatic homopolymers and copolymers of alkenylaromatic compounds and copolymerizable ethylenically unsaturated comonomers. A preferred alkenylaromatic polymer is polystyrene.

Said substantially statistical interpolymers comprise polymer units derived from ethylene and / or one or more α-olefin monomers together with a specific amount of one or more vinyl or vinylidene aromatic monomers and / or sterically hindered aliphatic or cycloaliphatic vinyl or vinylidene monomers. A preferred substantially random interpolymer of the present invention is an ethylene styrene interpolymer. The incorporation of said substantially random interpolymers into a mixture with an alkenylaromatic polymer results in an increase in the softness and flexibility of the foam formed from the mixture.

♦··· ··· «··· • · ····· ·· « • ········· « • · · · · · ··· ······· ·· ·· ·· · · ·

BACKGROUND OF THE INVENTION

Crosslinked olefinic foams are typically made of ethylene polymers such as low density polyethylene, ethylene vinyl acetate copolymer, homogeneous ethylene and / or α-olefin homopolymers or interpolymers containing ethylene and / or α-olefins containing from 3 to 20 carbon atoms, including linear ethylene / a. -olefin interpolymers. These polymers include polyolefin plastomers such as those sold by The Dow Chemical Company under the trade name AFFINITY® and polyethylene elastomers such as those sold by Du Pont Dow Elastomers PLC. under the trade name ENGAGE®.

Crosslinking occurs by conventional means, such as the use of peroxides, silane and / or radiation. One of the advantages of reticulated foams over non-crosslinked foams is the smaller size of the cells making up the foams (usually less than about 1 millimeter), the fine surface of the foams and their thermoformability. However, several disadvantages are also associated with reticulated foams, including: (1) the high cost of blowing agents used (such as azodicarbonamide); (2) Nitrogen-foamed reticulated foams are produced in an energy-intensive equipment at high pressure (typically at a pressure in the range of 68.9 megapascal to 206.8 megapascal, i. E. at a pressure ranging from 10,000 psi to 30,000 psi); (3) The processes used to manufacture said foams are typically batch (or batch) processes that are expensive to operate; and (4) said foams are not recyclable. On the other hand, non-crosslinked olefinic foams are produced by continuous processes at relatively high production rates using cheaper physical blowing agents (such as isobutane) and these foams are recyclable (which is desirable from an environmental point of view), but these foams are difficult to thermoform .

Therefore, it would be desirable to produce soft and flexible non-crosslinked foams containing small cell sizes that have satisfactory aesthetic properties and which could be used as an alternative to crosslinked foams avoiding the above disadvantages. Unexpectedly, it has been found that non-crosslinked foams made from mixtures of alkenylaromatic polymers and certain types and amounts of substantially random interpolymers are soft and flexible and contain small cell sizes. In addition, the foams are thermoformable and can be recycled.

SUMMARY OF THE INVENTION

Accordingly, the present invention provides soft and flexible foams having a Asker C hardness of less than about 65 (and a process for making such foams) comprising (A) from 30 weight percent to 70 weight percent based on the total weight of components A and B, one or more alkenylaromatic polymers, wherein at least one of said alkenylaromatic polymers has a molecular weight (M_w) between 100 000 and 500 000; and (B) from 30 weight percent to 70 weight percent, based on the total weight of components A and B, of one or more substantially random interpolymers whose melt index I₂ is in the range of 0.1 grams / 10 minutes to grams / 10 minutes and whose molecular weight distribution (M_w/ M_n) ranging from 1.5 to 20, wherein the interpolymers comprise (1) from 8 mole percent to 45 mole percent of polymer units derived from (a) at least one vinyl or vinylidene aromatic monomer, or (b) at least one sterically hindered aliphatic or a cycloaliphatic vinyl or vinylidene monomer, or (c) a combination of at least one aromatic vinyl or vinylidene monomer and at least one sterically hindered aliphatic or cycloaliphatic vinyl or vinylidene monomer; and (2) from 55 mole percent to 92 mole percent of polymer units derived from at least one monomer selected from the group consisting of ethylene and / or α-olefin containing from 3 to 20 carbon atoms; and (3) from 0 mole percent to 20 mole percent of polymer units derived from one or more ethylenically unsaturated polymerizable monomers, wherein the polymerizable monomers are not monomers derived from the monomers described in (1) and (2); and (C) optionally one or more nucleating agents;

(D) optionally one or more additional ingredients; and (E) one or more blowing agents having a total amount ranging from 0.4 gram-mol / kg to 5.0 gram-mol / kg based on the total weight of components A and B.

The above-described combination of the individual components allows the production of soft and resilient low density foams when blended from 30 weight percent to 70 weight percent of substantially statistical interpolymers containing from 8 mole percent to 45 mole percent of styrene with alkenylaromatic polymers. When similar foams are made from blends containing less than 30 weight percent of said substantially random interpolymers, the resulting foams are not as soft and flexible as traditional reticulated olefin foams. Also, when foams are made from blends containing more than 70 weight percent of said substantially random interpolymers, the structure of said foams collapses at temperatures to be maintained to prevent solidification of the alkenylaromatic polymer fraction.

All references to elements or metals belonging to a particular group refer to the Periodic Table of the Elements published by CRC Press, Inc. Also, any reference to a group or groups of elements refers to a group or groups as arranged in the Periodic Table of the Elements using the group numbering system according to the IUPAC nomenclature.

• · « « • · · • · · · · « ·

Any numerical values ​​cited in this specification include all values ​​from said lower to said higher value, incremented by one unit each, provided that the difference between the higher and lower values ​​is at least two. For example, when it is stated that the amount of a component or the value of a variable such as temperature, pressure, time is, for example, from 1 to 90, preferably from 20 to 80, more preferably from 30 to 70, it is understood that values ​​such as from 15 to 85, from 22 to 68, from 43 to 51, from 30 to 32, etc. are included. For numbers less than one, one unit is understood to be 0.0001, 0.001, 0.01 or 0.1, as appropriate. The examples given are merely for the purpose of explaining in particular what a range of values ​​is, and when numerical values ​​bounded by a lower and a higher value are given, likewise all values ​​within the interval thus defined are expressly mentioned within the scope of this description.

The term "hydrocarbyl" or "hydrocarbyl" means an aliphatic group, a cycloaliphatic group, an aromatic group, an aryl-substituted aliphatic group, an aryl-substituted cycloaliphatic group, an aliphatic-substituted aromatic group, or an aliphatic-substituted cycloaliphatic group.

ΐ

The term "hydrocarbyloxy" or "hydrocarbyloxy" means a hydrocarbyl or hydrocarbyl bonded to a carbon atom via an oxygen atom.

As used herein, the term "copolymer" refers to a polymer in which at least two different monomers have been used to produce the copolymer.

• · • ·

<img file="CZ20011985A3_D0004.tif" />

As used herein, the term "interpolymer" refers to a polymer in which at least two different monomers were used to produce the interpolymer. The term includes copolymers, terpolymers, etc.

The term &amp; quot; soft foam &amp; quot; as used herein refers to a foam having a Asker C hardness at a foam density of about 95 kilograms / m.³ or less, is less than about 65, preferably less than about 60, more preferably less than about 55.

The term "small cell size" as used herein refers to a foam containing cells less than about 1.8 millimeters in size.

In particular, the present invention relates to foams containing mixtures of one or more alkenylaromatic homopolymers or copolymers of alkenylaromatic monomers and / or copolymers of alkenylaromatic monomers with one or more copolymerizable ethylenically unsaturated comonomers (which are other than ethylene or linear α-olefins containing from 3 to 3). 12 carbon atoms) with at least one substantially random interpolymer. The foams of the present invention are characterized by a softness and elasticity that is comparable to the softness and elasticity of traditional reticulated olefinic foams of similar density.

Said alkenylaromatic polymeric material may further comprise minor proportions of non-alkenylaromatic polymers. Said alkenylaromatic polymeric material may consist of only one or more alkenylaromatic homopolymers, one or more alkenylaromatic copolymers, mixtures of one or more alkenylaromatic homopolymers and copolymers, or mixtures of any of the above materials with a non-alkenylaromatic polymer. Regardless of the particular composition, said alkenylaromatic polymeric material comprises more than 50 weight percent and preferably more than weight percent alkenylaromatic monomer units. Most preferably, said alkenylaromatic polymeric material comprises only alkenylaromatic monomer units.

Suitable alkenylaromatic polymers include homopolymers and copolymers derived from alkenylaromatic compounds such as styrene, α-methylstyrene, ethylstyrene, vinylbenzene, vinyltoluene, chlorstyrene, and bromstyrene. A preferred alkenylaromatic polymer of the present invention is polystyrene. The alkenylaromatic polymeric material of the present invention may also include commercially available high impact strength polystyrene (referred to as HIPS).

alkenylaromatic compounds can be copolymerized with minor amounts of monoethylenically unsaturated compounds, such as alkyl acids containing from 2 to carbon atoms in the alkyl chain, esters thereof and ionomeric derivatives thereof; and dienes containing from 4 to 6 carbon atoms. Particular examples of such copolymerized compounds include acrylic acid, methacrylic acid, ethacrylic acid, maleic acid, itaconic acid, acrylonitrile, maleic anhydride, methyl acrylate, ethyl acrylate, isobutyl acrylate, n-butyl acrylate, methyl methacrylate, butylacetate.

• ·· ·· ♦· ·· • · · * ··· ··· • · ····«'· ······· ·· ·· «· ·«·

The term "substantially statistical, as used herein in connection with" a substantially statistical interpolymer comprising polymer units derived from ethylene and one or more α-olefin monomers together with one or more vinyl or vinylidene aromatic monomers and / or one or more aliphatic or cycloaliphatic vinyl or vinylidene monomers, that the distribution of said monomers in this interpolymer can be described by Bernoulli's statistical model or the first- or second-order Markov statistical model as described in Polymer Sequence Determination, Carbon-13 NMR Method, Academic Press New York, 1977, 71-78 (JC). Randall). Preferably, these substantially random interpolymers contain no more than 15 percent based on the total amount of vinylaromatic monomer, vinylaromatic monomer in blocks of more than 3 units. More preferably, said interpolymer cannot be characterized by a high degree of isotacticity or syndiotacticity. That is, in¹³The C NMR spectra of such a substantially statistical interpolymer should not have a peak area corresponding to the methylene and methine backbone carbon atoms that represent either the mesomeric or racemic pair sequences should not exceed 75 percent of the total peak area corresponding to the methylene and methine backbone carbon atoms.

The group of interpolymers to be used in the production of foams of the present invention comprises essentially statistical interpolymers produced by polymerizing (i) ethylene and / or one or more α-olefin monomers and (ii) one or more vinyl or vinylidene aromatic monomers and / or one or more sterically hindered aliphatic or cycloaliphatic vinyl or vinylidene monomers; and optionally iii) one or more other polymerizable ethylenically unsaturated monomers. Suitable α-olefins include, for example, α-olefins containing from 3 to 20 carbon atoms, preferably from 3 to 12 carbon atoms, and more preferably from 3 to 8 carbon atoms. Particularly preferred α-olefins include ethylene, propylene, 1-butene, 4-methyl-1-pentene, 1-hexene or 1-octene or ethylene in admixture with one or more α-olefins selected from the group consisting of propylene, 1-butene , 4-methyl-1-pentene, 1-hexene or 1-octene. Said α-olefins do not contain aromatic groups.

Other optionally polymerizable ethylenically unsaturated monomers include norbornene and norbornenes substituted with a C 1 -C 10 alkyl group or a norbornene substituted with an C 6 -C 10 aryl group, which can be used, for example, to produce an ethylene / styrene / norbornene interpolymer.

Examples of suitable vinyl or vinylidene aromatic monomers which can be used to produce the interpolymers of the present invention include compounds of the general

Ar (CH₂)_n

R¹ - C = C (R =²)₂ formulas ······························································ ··· ·· · · ·· · where

R¹ is selected from the group consisting of hydrogen and alkyl groups containing from 1 to 4 carbon atoms, preferably hydrogen or methyl;

R² they are both independently selected from the group consisting of hydrogen and alkyl groups having from 1 to 4 carbon atoms, preferably hydrogen or methyl;

Ar is phenyl or phenyl substituted with one to five substituents selected from the group consisting of halogen, alkyl of 1 to 4 carbon atoms and haloalkyl of 1 to 4 carbon atoms;

and n is from 0 to 4, preferably from 0 to 2, more preferably 0.

Examples of the vinylaromatic monomer include styrene, vinyltoluene, α-methylstyrene, target, butylstyrene, chlorstyrene, including all isomers of said compounds. Particularly suitable monomers of this type include styrene and derivatives thereof substituted with a lower alkyl group or a halogen atom. Preferred monomers include styrene, α-methylstyrene, styrene derivatives substituted with a lower alkyl group (i.e. (C1-C4-alkyl) or styrene derivatives substituted on the phenyl ring, such as ortho-, meta- and para-methylstyrene, halogenated styrenes, para-vinyltoluene or mixtures.

<img file="CZ20011985A3_D0005.tif" />

of said compounds. A more preferred aromatic vinyl monomer is styrene.

As used herein, the term "sterically hindered aliphatic or cycloaliphatic vinyl or vinylidene compounds" means addition polymerizable vinyl or vinylidene monomers of the general formula:

AND¹

R¹ - C = C (R =²)₂ where

AND¹ is a sterically bulky aliphatic or cycloaliphatic substituent containing up to 20 carbon atoms;

R¹ j^E selected from the group consisting of hydrogen and alkyl groups containing from 1 to 4 carbon atoms, preferably hydrogen or methyl;

R² they are both independently selected from the group consisting of hydrogen and alkyl groups having from 1 to 4 carbon atoms, preferably hydrogen or methyl; or

R¹ and A¹ together they form a circular system.

Preferred aliphatic or cycloaliphatic vinyl or vinylidene compounds are monomers in which one of the atoms bearing the ethylenically unsaturated bond is tertiary or quaternary substituted. Examples of such substituents include cyclohexyl, cyclohexenyl, cyclooctenyl or derivatives of these compounds in which the ring is substituted. alkyl or aryl, target, butyl and norbornyl. More preferred aliphatic or cycloaliphatic vinyl or vinylidene compounds are various isomeric vinyl derivatives of substituted ring cyclohexene and substituted cyclohexenes and 5-ethylidene-2-norbornene. Particularly suitable compounds are 1-, 3- and 4-vinylcyclohexene. Examples of spherically hindered aliphatic or cycloaliphatic vinyl or vinylidene compounds are not simple linear unbranched α-olefins, the group of which includes, for example, α-olefins containing from 3 to 20 carbon atoms such as propylene, 1-butene, 4-methyl-1-pentene, -hexene or 1-octene.

The group of substantially statistical interpolymers of the present invention includes the pseudo-statistical interpolymers described in European Patent Application Publication No. EP-A-0416815 (James C. Stevens et al.) And US Patent No. 5703187 (Francis J. Timmers) ), the contents of both of which are incorporated herein by reference. Said substantially random interpolymers are prepared by polymerizing a mixture of polymerizable monomers in the presence of one or more metallocene or constrained geometry catalysts together with various cocatalysts. Preferred conditions for such polymerization reactions include a pressure from 101.325 kilopascal to 303.975 megapascal (from atmospheric pressure to 3000 atmospheres) and a temperature from -30 to 200 ° C. Polymerization and removal of unreacted monomer at

<img file="CZ20011985A3_D0006.tif" />

temperatures higher than the autopolymerization temperature of the monomers may result in the formation of certain amounts of radical polymerization homopolymerization products.

Examples of suitable catalysts and methods for producing substantially statistical interpolymers are described in U.S. Patent Application Serial No. 702475, filed on

20 May May 1991 (EP-A-514828); and U.S. Patent Nos. 5,505,438; US 5057475; US 5096867;

US 5064802; US 5,132,380; US 5189192; US 5321106; US 5347024;

US 5350723; US 5374696; US 5399635; US 5470993; US 5703187 and US 5721185.

The substantially statistical α-olefin / vinylaromatic interpolymers of the present invention can also be prepared by the method described in Japanese Patent No. JP 07/278230 using compounds of the formula

<img file="CZ20011985A3_D0007.tif" />

where

Cp¹ and Cp² are independently cyclopentadienyl, indenyl, fluorenyl or substituted derivatives thereof;

R¹ and R² are, independently of one another, hydrogen atoms, halogen atoms, hydrocarbyl groups containing hydrocarbons; From 1 to 12 carbon atoms, an alkoxy group, or an aryloxy group;

M is the metal of IV. groups, preferably zirconium or hafnium, more preferably zirconium; and

R³ is an alkylene group or a silandiyl group joining the Cp substituents¹ and Cp².

The substantially statistical α-olefin / vinylaromatic interpolymers used in the preparation of the compositions of the present invention can also be prepared as described in International Publication Nos. WO 95/32095 (John G. Bradfute - WR Grace &amp; Co.) and WO 94/00500 (RB). Pannell - Exxon Chemicals Patents, Inc.) And in Plastics Technology Magazine on page 25 (published September 1992).

Also suitable are essentially statistical interpolymers comprising at least one α-olefin / vinylaromatic monomer / vinylaromatic monomer / α-olefin tetras described in U.S. patent application Ser. No. 08/708869 filed Sep. 4, 1996 and published internationally. WO 98/09999 (Francis J. Timmers et al.). ¹³The C NMR spectra of these interpolymers contain additional signals whose intensity is more than three times the inter-noise noise. These signals appear in the range of chemical shifts from 43.70 to 44.25 ppm and from 38.0 to 38.5 ppm. In particular, major peaks with a chemical shift of 44.1 ppm, 43.9 ppm and

38.2 ppm. Test measurements of the proton NMR spectrum have shown that chemical shift signals in the range of 43.70 to • ·

44.25 ppm correspond to methine carbon atoms and chemical shift signals in the 38.0 to 38.5 ppm range correspond to methylene carbon atoms.

These new signals are believed to be due to a sequence comprising two insertions of a vinyl aromatic monomer oriented from an initial to an end carbon atom followed by an insertion of at least one α-olefin, such as the ethylene / styrene / styrene / ethylene tetraside in which for insertion of the styrene monomer exclusively by the method 1,2 (i.e. in the direction from the initial to the terminal carbon atom). One skilled in the art will appreciate that in cases where tetrases containing vinyl aromatic monomers other than styrene and α-olefin other than ethylene, these ethylene / vinylaromatic monomer / vinylaromatic monomer / ethylene tetrases will be in the form of a tetraside. ¹³The C NMR spectrum exhibits similar effects, with only minor changes in the chemical shift values ​​of the individual signals.

Said interpolymers may be prepared by polymerization at a temperature of from -30 to 250 ° C in the presence of catalysts of the general formula wherein independently of one another cyclopentadienyl groups are bonded by π-bonds to M;

• ♦· ·· · 4·9 • · · · 4 · · · «· • · ····· « · • · ···· ··· ······· ·· « « « 4«··

Ε is carbon or silicon;

M is the metal atom of IV. groups, preferably zirconium or hafnium, more preferably zirconium;

R are independently selected from hydrogen, hydrocarbyl, silahydrocarbyl or hydrocarbylsilyl containing up to 30, preferably from 1 to 20, more preferably from 1 to 10 carbon or silicon atoms;

R 'are independently selected from the group consisting of hydrogen, halogen, hydrocarbyl, hydrocarbyloxy, silahydrocarbyl, hydrocarbylsilyl containing up to 30, preferably from 1 to 20, more preferably from 1 to 10 carbon or silicon atoms, or two groups R 1 can together form a hydrocarbyl group having 1 to 10 carbon atoms substituted with 1,3-butadiene;

m is 1 or 2;

and optionally, but preferably, in the presence of an activating cocatalyst, in particular in the presence of suitably substituted cyclopentadienyl groups including cyclopentadienyl groups

<img file="CZ20011985A3_D0008.tif" />

Kde · · kde kde kde kde kde kde kde kde kde kde kde kde kde kde kde kde kde where

R are independently selected from the group consisting of hydrogen, hydrocarbyl, silahydrocarbyl or hydrocarbylsilyl containing up to 30, preferably from 1 to 20, more preferably from 1 to 10 carbon or silicon atoms, or two R groups together form a divalent derivative of one of the aforementioned wherein R is independently of each other (including any isomer) that is selected from the group consisting of hydrogen, methyl, ethyl, propyl, butyl, pentyl, hexyl, benzyl, phenyl or silyl or (where appropriate) two such R groups are joined together to form a fused ring system such as indenyl, fluorenyl, tetrahydroindenyl, tetrahydrofluorenyl or octahydrofluorenyl.

Particularly preferred catalysts include, for example, racemic (dimethylsilandiyl) -bis (2-methyl-4-phenylindenyl) zirconium dichloride, racemic 1,4-diphenyl-1,3-butadiene complex with (dimethylsilandiyl) -bis (2-methyl-4-phenylindenyl) zirconium , racemic dialkyl (dimethylsilandiyl) -bis (2-methyl-4-phenylindenyl) zirconium, wherein the alkyl groups in this complex contain 1 to 4 carbon atoms, racemic dialkoxy (dimethylsilandiyl) -bis (2-methyl-4-phenylindenyl) zirconium, wherein the alkoxide groups in this complex contain 1 to 4 carbon atoms and a combination of said compounds.

The following limited geometry catalysts based on titanium compounds may also be used:

dimethyl [N- (1,1-dimethylethyl) -1,1-dimethyl-1 - [(1,2,3,4,5-η) 1,5,6,7-tetrahydro-s-indacen-1- yl] silanaminato (2-) -N] titanium; dimethyl (1-indenyl) (t-butylamido) dimethylsilanethane; dimethyl ((3-tert-butyl) (1,2,3,4,5-η) -1indenyl) (t-butylamido) dimethylsilanethane and dimethyl ((3-isopropyl) (1,2,3,4,5- η) -1-indenyl) (target, butylamido) dimethylsilanethane or combinations thereof.

Other methods for preparing substantially statistical interpolymers used in the present invention have been described in the literature. In articles published in Makromol. Chem., 1990, 191, 2387-2396 (Longo and Grassi) and Journal of Applied Polymer Science, 1995, 58, 1701-1706 (D'Anniello et al.) Have described the use of a catalyst system based on methylalumoxane (MAO) and cyclopentadienyltitanium trichloride ( CpTiCl₃) in the manufacture of an ethylene styrene copolymer.

In an article published in Polymer Preprints, Am. Chem. Soc., Div. Polym. Chem., 1994, 35, 686-687 (Xu and Lin) have described copolymerization using a catalyst comprising a combination of magnesium chloride (MgCl 2), titanium tetrachloride (TiCl 2)₄), neodymium chloride (NdCl₃) and triisobutyl aluminum (Al (iBu)₃), which results in random copolymers of styrene and propylene. In an article published in the Journal of Applied Polymer Science, 1994, 53, 1453-1460 (Lu et al.), Ethylene-styrene copolymerization using a catalyst comprising a combination of titanium tetrachloride (TiCl) was described₄), neodymium chloride (NdCl₃), magnesium chloride (MgCl₂) and triethyl aluminum (Al (Et)₃). In Makromol. Chem. Phys, 1997, 197, 1071-1083 (Sernetz and Mulhaupt), the effect of polymerization conditions on the course of copolymerization of styrene with ethylene in the presence of Ziegler-Natta catalysts based on

Me₂Si (Me₄Cp) (N-tert-butyl) TiCl₂methylalumoxoxane. Ethylene-styrene copolymers produced using bridged metallocene catalysts have been described in Polymer Preprints, Am. Chem. Soc., Div. Polym. Chem., 1997, 38, 349-350 (Arai, Toshiaki and Suzuki) and U.S. Pat. No. 5,652,315 (Mitsui Toatsu Chemicals, Inc.). The preparation of α-olefin / vinylaromatic interpolymers such as propylene styrene copolymer and butenstyrene copolymer is described in U.S. Patent No. 5,244,996 (Mitsui Petrochemical Industries Ltd.) or U.S. Patent No. 5,652,315 (Mitsui Petrochemical Industries Ltd.) or in U.S. Pat. German Patent Application Publication No. DE 19711339 A1 (Denki Kagaku Kogyo KK). It is also possible to use the ethylene-styrene random copolymers described in Polymer Preprints, 1998, 39, No. 1, although the copolymers are highly isotactic and therefore cannot be described as &amp; quot; substantially statistical &amp; quot;

In preparing the substantially statistical interpolymers, some atactic vinylaromatic homopolymer may be formed by homopolymerizing the vinylaromatic monomer at elevated temperature. The presence of the vinylaromatic homopolymer is usually not detrimental to the purposes of the present invention and can be tolerated. If desired, the resulting vinyl aromatic homopolymer may be separated from said interpolymer by extraction techniques such as selective precipitation from solution with a solvent in which either said interpolymer or said vinylaromatic homopolymer is not dissolved. For the purposes of the present invention, it is preferred that said interpolymers contain less than 30 weight percent, preferably less than 20 weight percent, based on the total weight of said interpolymer, an atactic vinylaromatic homopolymer.

Production of foams according to the present invention

The compositions of the present invention may be used in the manufacture of extruded thermoplastic polymeric foam, foamable thermoplastic foam particles or foamed thermoplastic foams, and moldings formed by foaming and / or agglomerating and welding the particles.

The foams of the present invention may have any known physical shape such as an extruded plate, a rod, an elongate blank, foils, and various profiles. The foam structure of the present invention may also be formed by welding the foamable particles to any shape, including the shapes just mentioned.

If desired, the foams of the present invention may be modified to form a plurality of channels or perforations in the foam structure for rapid curing and rapid release of the blowing agent.

<img file="CZ20011985A3_D0009.tif" />

they extend from the surface of the foam to its internal structure, the channels having no particular direction with respect to the longitudinal expansion of the foam. An excellent description of these modifications is described in U.S. Pat. No. 5,424,016 and International Publication Nos. WO 92/19439 and WO 97/22455.

The foam structures of the present invention can be produced by a conventional extrusion foaming process. The foam structure is typically produced by melt blending, which heats the alkenylaromatic polymeric material of the present invention and one or more substantially random interpolymers to form a softened or molten polymeric material, which is subsequently incorporated into a blowing agent to form a foamable gel, which is subsequently extruded through a slot to form a foam product. Prior to extrusion, the gel is cooled to an optimum temperature, and to form a foam it is optimal that the temperature be equal to or higher than the glass transition temperature or melting point of the polymer blend. The optimum foaming temperature for the foams of the present invention is in the absence of warping of the foam structure. The blowing agent may be incorporated or mixed into the molten polymer material by any known means such as an extruder, mixer, mixer and the like. The blending of the blowing agent with the molten polymer occurs at an elevated pressure sufficient to prevent substantial foaming of the molten polymer material and to distribute the blowing agent homogeneously throughout the melt volume. Optionally, a nucleating agent may be admixed into the polymer melt, or the nucleating agent may be admixed dry with the polymer material prior to softening or melting. The substantially random interpolymers may be dry blended with the polymer material prior to entering the extruder or fed to the extruder in the form of a polymer concentrate or carrier material comprising the interpolymer and the color pigment. The aforesaid foamable gel is usually cooled to a lower temperature in order to optimize the physical characteristics of the foam structure of the present invention. The gel may be cooled directly in an extruder or other mixer or in separate chillers. Subsequently, the gel is extruded or conveyed through a slit of the desired shape into a zone of reduced or lower pressure to form a foam structure. The pressure in said low pressure zone is lower than the pressure at which the foamable gel is maintained prior to extrusion through the slit. This low pressure may be higher than atmospheric pressure or lower than atmospheric pressure (vacuum), but preferably this pressure is approximately equal to atmospheric pressure.

The foam structures of the present invention may be formed in the form of agglomerated strips by extruding the compositions of the present invention through a slot with multiple orifices. The apertures of the slit are arranged so that during the process of forming the foam structure there is contact between adjacent streams of molten exudate and that the contacting surfaces adhere to each other with such an adhesion that results in a homogeneous foam structure. The streams of molten exudate that leave the aperture are in the form of strips or profiles that foam, agglomerate or agglomerate as necessary to form a homogeneous structure. It is desirable that the individual agglomerated strips or profiles remain joined to form a homogeneous structure in order to prevent delamination of the web under stress to which it is subjected in the manufacture, shaping and use of the foam structure. Apparatuses for manufacturing and methods of making foamed structures in the form of an agglomerated strip are described in U.S. Patent Nos. 3573152 and 4824720.

The foam structures of the present invention may also be formed by the bulk extrusion process described in U.S. Patent No. 4,323,528. This method produces low density foam structures having large lateral cross-sectional areas, the method comprising: 1) forming a gel from the compositions of the present invention and a blowing agent at elevated pressure and at a temperature at which the viscosity of the gel is sufficient to the blowing agent maintained in the gel structure during its foaming;

2) extruding the resulting gel into a standby zone in which temperature and pressure are maintained that do not allow foaming of the gel, the standby zone comprising an exit slot defining an orifice opening into a depressurized zone in which the gel foams and an opening closure which closes the opening of the slot; 3) periodically opening said opening closure; 4) substantially co-acting the mechanical pressure exerted by the movable plunger on the gel to push it out of the standby zone through the aperture into the depressurized zone at a rate greater than the rate at which the foam in the aperture is substantially foamed than the speed at which significant irregularities occur in the cross-sectional area or shape of the foam structure formed; and 5) retention

<img file="CZ20011985A3_D0010.tif" />

of the extruded gel in at least one direction free to foam to form a foam structure according to the present invention.

The foam structures of the present invention can also be made in the form of foam particles suitable for forming into various products by foaming the foamed particles containing a blowing agent. Said particles may be shaped during their foaming to form differently shaped articles. Methods for making foamed particles and molded articles from foamed foam particles have been described in Frisch and Sounders: Plastic Foams, Part II, pp. 544-585, Marcel Dekker, Inc. (1973) and Brydson: Plastic Materials, 5th Edition, pp. 426-429, Butterworths (1989).

The foamable and foamed particles can be produced by a batch (or batch) process or an extrusion process. The batch process used in the production of foamable particles is essentially the same as the process used in the production of foamable polystyrene (EPS). In this production process, the granules of the polymer blend which have been preformed either by blending or mixing in the reactor are impregnated in the form of an aqueous suspension or in the dry state with a blowing agent, which impregnation occurs in a pressure vessel at elevated temperature and pressure. The impregnated granules are then quickly removed from the pressure vessel to the reduced pressure area where they are foamed to form foam particles, or are cooled and removed from the pressure vessel in the form of non-foamed particles. The non-foamed particles are subsequently heated in a suitable manner (for example by steam or hot air), thereby foaming them. The above extrusion process is essentially the same as the conventional foam extrusion process described in the preceding paragraphs, except for the orifice of the slit. Said slot has several openings. In order to form non-foamed particles, the foamable strips exiting the mouth of the slot are immediately introduced into the water bath to prevent foaming, and then processed into pellets. Alternatively, the strips are converted into foam particles by cutting on the slit side and then allowing foaming.

Said foam particles may then be shaped by any known method, such as comprising filling the mold with foam particles, compressing the mold to compress the particles and heating the particles, for example by steam, to agglomerate and weld them to form the desired article. Optionally, the particles may be impregnated with air or other blowing agent at elevated pressure and elevated temperature prior to filling the mold with particles. Further, it is possible to heat the particles before filling them into the mold. Thereafter, the foam particles may be formed into blocks or shaped articles using suitable shaping techniques known in the art. (Some of these methods are described in U.S. Pat. Nos. 3504068 and 3953558.) Excellent descriptions of the above processes and molding methods are given in the above publication on pages 191, 197-198 and 227-229 (CP Park.

In the manufacture of said foam particles, mixtures of alkenylaromatic polymers with one or more substantially random interpolymers are formed into separate polymer particles such as granules or pellets; taking this method · · · · · způsob způsob způsob způsob způsob způsob způsob způsob způsob způsob způsob způsob způsob způsob způsob · · · · Comprising suspending said particles in a liquid medium in which the particles are substantially insoluble, such as water; impregnating the suspended particles with a blowing agent by feeding the blowing agent into said liquid medium, said impregnation being carried out at elevated pressure and at elevated temperature in an autoclave or other pressure vessel; rapidly transferring the mixture contained in the autoclave or other pressure vessel to an atmospheric or reduced pressure site, thereby foaming the particles and forming the foam particles of the present invention. This method is well described in U.S. Patent Nos. 4379859 and 4464484.

U.S. Pat. No. 4,168,353 discloses a process in which foamed particles are made from a graft polymer of polyethylene and polystyrene. In this process, it is also possible to use styrene monomer to form a polymer grafted with one or more substantially random interpolymers, and the graft polymer thus formed can be used to produce foam particles. The process comprises the following steps:

(I) impregnating the styrene monomer into suspended pellets of one or more substantially random interpolymers, impregnating in a suitable vessel, at elevated temperature and in the presence of a peroxide initiator to form a graft polymer of polystyrene and a substantially random polymer;

(II) impregnating the product of step (I) with one or more blowing agents;

······························································································· (III) cooling and recovering the product of step (II) in the form of non-foamed particles; and (IV) foaming and shaping the particles of step (III) to form a foam.

Another method of making foamable thermoplastic particles comprises using an alkenylaromatic monomer and optionally at least one other monomer that differs from but is polymerizable with said monomer; dissolving the substantially random interpolymers of the invention in at least one of said monomers; polymerizing said first and second monomers to form thermoplastic particles; introducing a blowing agent into the thermoplastic particles during and after the polymerization; and cooling the thermoplastic particles so produced to form foamable particles.

The alkenylaromatic monomer is used in an amount of at least 50 weight percent, preferably at least 70 weight percent, more preferably at least 90 weight percent, based on the total weight of the polymerizable monomers.

Another method of making foamable thermoplastic particles comprises heating mixtures of alkenylaromatic polymers with one or more substantially random interpolymers to form a molten polymer material; introducing a blowing agent into the molten polymeric material to form a foamable gel, wherein the blowing agent is added at elevated temperature; cooling said gel to an optimum temperature, a temperature at which foaming cannot occur;

extruding the cooled gel through a slot containing one or more orifices to form one or more substantially continuous foamable thermoplastic sheets; and pelletizing said foamable thermoplastic sheets to form foamable thermoplastic particles.

Alternatively, it is possible to form foamed thermoplastic foam particles by cooling the gel prior to extrusion through the slit to an optimum temperature, which in this case is equal to or greater than the glass transition temperature of the blend or the melting point of the blend. The temperature range within which said optimum foaming temperature of the foamed thermoplastic foam particles of the present invention is sufficient to prevent the foam structure from collapsing.

The foam structures of the present invention may also be used to produce foamed films for packaging bottles and other containers using the blown or flat film process. The films may also be produced by a co-extrusion process to produce articles comprising a foam core and one or two surface layers, which may or may not consist of the polymer blends of the present invention.

The blowing agents suitable for forming the foams of the present invention include inorganic blowing agents, organic blowing agents and chemical blowing agents. Suitable inorganic blowing agents include nitrogen, sulfur hexafluoride (SF₆), argon, water, air, and helium. Organic blowing agents include carbon dioxide, C 1 -C 3 aliphatic hydrocarbons, C 1 -C 3 aliphatic alcohols, and fully or partially halogenated C 1 -C 4 aliphatic hydrocarbons. Aliphatic hydrocarbons include methane, ethane, propane, n-butane, isobutane, n-pentane, isopentane and neopentane. Aliphatic alcohols include methanol, ethanol, n-propanol, and isopropyl alcohol. The group of fully or partially halogenated aliphatic hydrocarbons includes fluorinated hydrocarbons, chlorinated hydrocarbons and chlorofluorocarbons. Examples of the fluorocarbon include methyl fluoride, perfluoromethane, ethyl fluoride, 1,1-difluoroethane (HFC-152a), fluoroethane (HFC-161), 1,1,1-trifluoroethane (HFC-143a),

1,1,1,2-tetrafluoroethane (HFC-134a), 1,1,2,2-tetrafluoroethane (HFC-134), 1,1,1,3,3-pentafluoropropane, pentafluoroethane (HFC-125), difluoromethane (HFC-32), perfluoroethane, 2,2-difluoropropane, 1,1,1-trifluoropropane, perfluoropropane, dichloropropane, difluoropropane, perfluorobutane, perfluorocyclobutane. Partially halogenated chlorinated hydrocarbons and chlorofluorocarbons suitable for use herein include methyl chloride, methylene chloride, ethyl chloride,

1,1,1-trichloroethane, 1,1-dichloro-1-fluoroethane (HCFC-141b), 1-chloro-1,1-difluoroethane (HCFC-142b), chlorodifluoromethane (HCFC-22), 1,1-dichloro -2,2,2-trifluoroethane (HCFC-123) a

1-chloro-1,2,2,2-tetrafluoroethane (HCFC-124). The group of fully halogenated chlorofluorocarbons includes trichlorofluoromethane (CFC-11), dichlorodifluoromethane (CFC-12), trichlorotrifluoroethane (CFC-113), dichlorotetrafluoroethane (CFC-114), chlorheptafluoropropane and dichlorhexafluoropropane. The group of chemical blowing agents includes azodicarbonamide, azodiisobutyronitrile, benzenesulfonhydrazide,

4,4-oxybenzenesulfonylsemicarbazide, p-toluenesulfonylsemicarbazide, barium azodicarboxylate, N, Ν'-dimethyl-N, Ν'-dinitrosoterephthalamide, trihydrazinotriazine, and mixtures of citric acid and sodium bicarbonate, such as various products sold under the trade name Hydrocerring® Ing. All of the above blowing agents may be used singly or in any mixture including such blowing agents or in admixture with other auxiliary blowing agents.

The amount of blowing agents incorporated into said molten polymer material to form a foam-forming polymer gel is from 0.4 gram-mol / kg to 5.0 gram-mol / kg of polymer, preferably from

0.6 gram-mol / kg to 3.0 gram-mol / kg of polymer, more preferably from 0.8 gram-mol / kg to 2.5 gram-mol / kg of polymer.

In addition, nucleating agents for regulating the size of the foam cells may be added to the foam structures of the present invention. Preferred nucleating agents include inorganic compounds such as calcium carbonate, talc, clay, silica, barium stearate, calcium stearate, diatomaceous earth, and mixtures of citric acid and sodium bicarbonate. The amount of nucleating agent used may range from 0 to 5 parts by weight of reagent per

100 ALIGN! % by weight of the polymer, preferably from 0 to 3 parts by weight.

Various additives such as inorganic fillers, pigments, antioxidants, acid scavengers, agents may be added to the foam structure of the present invention.

<img file="CZ20011985A3_D0011.tif" />

• · • ·

<img file="CZ20011985A3_D0012.tif" />

ultraviolet absorbers, flame retardants, processability enhancers, extrudability enhancers, permeability modifiers, antistatic agents, and other thermoplastic polymers. An example of permeability modifying agents is glycerol monoesters, which may also serve as static-reducing agents during foam production, without being limited thereto. Examples of another thermoplastic polymer are alkenylaromatic homopolymers or copolymers (having a molecular weight of from 2000 to 50,000) and ethylene polymers.

The foam density of the present invention, determined according to ASTM D-1622-88, is in the range of 10 kilograms / m³ up to 95 kilograms / m³preferably from 10 kilograms / m³ up to 80 kilograms / m^J.

The average foam cell size, determined according to ASTM D-3576-77, is in the range of 0.05 millimeter to 5 millimeter, preferably 0.1 millimeter to 2.0 millimeter, and more preferably 0.2 millimeter to 1.8 millimeter. .

The foams of the present invention are particularly suitable for producing elongate blanks or sheets having a thickness, or shorter cross-sectional dimension, of 1 millimeter or more, preferably 2 millimeters or more or even more preferably as desired

2.5 millimeters or more. The foam width of the present invention may be up to 1.5 meters.

• ·

The open cell content of the foams of the present invention, as determined according to ASTM D2856-94, is in the range of 0 to 100 percent.

The hardness of the foams of the present invention was measured using a Asker C durometer, which measures the hardness of cell rubbers and yarn according to the ASTM D2240-97 standard (but in the case of the foams of the present invention, a spherical needle with a diameter of about 5 millimeters was used). The hardness of the Asker C foams of the present invention is less than about 65, preferably less than about 60, more preferably less than about 55.

The foams produced according to the present invention can be used in many products, the group of which includes resilient packing, sports and recreational products, egg cartons, meat pads, building products (eg thermal insulation, sound insulation), insulation pipes, gaskets, vibration-damping pads, luggage liners, desk mats, shoe soles, gymnastic mats, insulating foils used in greenhouses, box inserts, foams used in shop windows, etc. Examples of products used in the construction industry include, among others, wall cladding (thermal insulation of houses), materials under roofing, insulation of foundations and permanent insulating mats. Other products include insulating materials used in refrigerator production, buoyancy products (such as body lift boards, floating docks and rafts), and various products used in the florist and small craft industries. However, it should be noted that the use of the foams of the present invention is not limited to the aforementioned product examples.

» · « · * · « « · · « • ·

Properties of the interpolymer and blended compositions used in preparing the foams of the present invention

The polymer blends used in preparing the foams of the present invention comprise from 30 weight percent to 70 weight percent, preferably from 32 weight percent to 68 weight percent, more preferably from 35 weight percent to 65 weight percent, based on the total weight of the substantially random interpolymer and alkenylaromatic homopolymers. or copolymers, one or more alkenylaromatic homopolymers or copolymers.

Molecular weight distribution, expressed as the ratio of the weight average molecular weight to the number average molecular weight (M_w/ M_n) of said alkenylaromatic homopolymers or copolymers used in preparing the foams of the invention is from 2 to 7.

Weight average molecular weight (M_w) of said alkenylaromatic homopolymers or copolymers used in preparing the foams of the invention is from 100,000 to 500,000, preferably from 120,000 to 350,000, more preferably from 130,000 to 325,000.

The alkenylaromatic polymeric material used in preparing the foams of the present invention contains more than 50 weight percent, preferably more than 70 weight percent alkenylaromatic monomer units. Most preferably, said alkenylaromatic polymeric material consists only of alkenylaromatic monomer units.

• · • Λ · ·

R r r (((((* * * * &lt;&lt;&lt;&lt;&lt;&lt;&lt;&lt;&lt;&lt;&lt;&lt;&lt;

The polymer blends used in preparing the foams of the present invention comprise from 30 weight percent to weight percent, preferably from 32 weight percent to 68 weight percent, more preferably from 35 weight percent to 65 weight percent, based on the total weight of substantially random interpolymers and alkenylaromatic homopolymers; copolymers, one or more substantially random interpolymers.

The substantially statistical interpolymers used to form the foams of the present invention typically comprise from 8 mole percent to 45 mole percent, preferably from 10 mole percent to 43 mole percent, more preferably from 13 mole percent to 40 mole percent of at least one vinyl or vinylidene aromatic monomer and / or an aliphatic or cycloaliphatic vinyl or vinylidene monomer and from 55 mole percent to 92 mole percent, preferably from 57 mole percent to 90 mole percent, more preferably from 60 mole percent to 87 mole percent ethylene and / or at least one aliphatic α-olefin containing from 3 to 20 carbon atoms.

Melt flow index₂) of said substantially statistical interpolymer used to form the foams of the present invention is from 0.1 gram / 10 minutes to 50 gram / 10 minutes, preferably from 0.3 gram / 10 minutes to 30 gram / 10 minutes, more preferably from 0.5 gram / 10 minutes to 10 grams / 10 minutes.

Molecular weight distribution, expressed as the ratio of weight-average molecular weight to number-average, · 4 · · 4 ·························· Molecular weight (M_w/ M_n) of said substantially statistical interpolymer used to form the foams of the present invention is from 1.5 to 20, preferably from 1.8 to 10, more preferably from 2 to 5.

In addition, minor amounts of alkenylaromatic homopolymers or copolymers having a molecular weight of from 2,000 to 50,000, preferably from 4,000 to 25,000, may be added to the foams of the present invention, and the amount of such homopolymers or copolymers does not exceed 20% by weight based on the total weight. a random interpolymer and various alkenylaromatic homopolymers or copolymers.

DETAILED DESCRIPTION OF THE INVENTION

The following examples are provided to better illustrate the present invention without limiting its scope in any way.

Testing methods

a) Measurement of density and melt index

The molecular weight of the substantially statistical polymers used in the present invention is commonly expressed as a melt flow index determined in accordance with ASTM D-1238, 190 ° C / 2.16 kilogram (formally known as "Conditions (E)" and also known as melt flow index) AND₂). The melt index is inversely proportional to the molecular weight of the polymer. This means that the greater the molecular weight, the lower the melt index, but the relationship between the two variables is not linear.

·· ··· ··· • · ···· · ·

The Gottfert melt index (G, cm) is also useful for expressing the molecular weight of the substantially statistical interpolymers of the present invention.³(10 minutes), which is measured in a similar manner to the melt index I₂ according to ASTM D-1238 for automated plastometers with a set melt density of 0.7632, which is the melt density of polyethylene at 190 ° C.

The relationship between melt density and styrene content in ethylene styrene interpolymers was measured as a function of total styrene content at 190 ° C and for the range of 29.8 to 81.8 weight percent styrene. These samples usually contained 10 or less percent by weight of atactic polystyrene. Due to such a low content of atactic polystyrene, its influence was assumed to be minimal. Also, the melt density of the atactic polystyrene and the melt density of said samples with an overall high styrene content were very similar. In the method of determining the density of the melt, a Gottfert melt index measuring instrument having a set density value of 0.7632 was used and the amount of melt accumulated was measured as a function of time under the weight used to determine the melt index I₂. For each melt strand, its weight and the time it took to collect this amount were recorded and converted to grams per 10 minutes. The melt index I values ​​were also recorded₂ measured with the above apparatus. The actual melt density was calculated according to equation = 5 (), 7632^x I2 / I2 Gottfert where δο, 7632 - 0.7632 a

AND₂ cottfert ⁼ the melt flow index value displayed.

By linearizing the dependence of the calculated melt density on the total styrene content by the least-squares method, an equation with a correlation coefficient of 0.91 was obtained for the equation:

δ = 0.00299 x S + 0.723 where

S = the styrene content of the polymer, expressed as a percentage by mass.

The relationship between the total styrene content and the melt density can be used to determine the actual melt flow index using the equations given and the known styrene content.

Thus, for a polymer containing a total of 73 percent styrene with a measured melt index (the so-called "Gottfert number"), the calculation began:

x = 0.00299 x 73 + 0723 = 0.9412 where

0.9412 / 0.7632 = I₂/ measured number Gottfert = 1.23 • · · ··· 0 · 0 · 0 0 0 0 »« ·· • 0 0 0 0 * 0 * • &lt;· * ·· ···

0000000 * 0 * · * * · · p

b) Styrene analysis

The styrene content of the interpolymer and the concentration of atactic polystyrene were determined by proton magnetic nuclear resonance (hereinafter referred to as ¹1 H NMR). All samples for G NMR spectra were prepared by dissolving in 1,1,2,2-tetrachloroethane-d.₂ (referred to hereinafter as TCE-d₂). The resulting solutions contained 1.6-3.2 weight percent polymer. The melt index I was the guide for determining the sample concentration₂. Thus, if the melt index was I₂ greater than 2 grams / 10 minutes, milligrams of interpolymer were used; if the melt index was I₂ in the range of from 1.5 grams / 10 minutes to grams / 10 minutes, 30 milligrams of the interpolymer were used, and if the melt index I was₂ smaller than

1.5 grams / 10 minutes, 20 milligrams of interpolymer were used. The individual interpolymers were bound directly into sample tubes of 5 mm diameter. 0.75 ml of TCE-d was added to the weighed sample₂ and the tube was closed with a tight fit polyethylene cap. To soften the interpolymer, the samples were heated in a water bath to 85 ° C. To ensure mixing, the sealed samples were brought to boiling from time to time using a hot air gun.

Proton NMR spectra were measured on a Varian VXR 300 instrument at a sample temperature of 80 ° C and referred to the residual proton signal TCE-d.₂whose chemical shift is 5.99 ppm. The delay time varied within 1 second and three measurements were taken for each sample. The following instrumental conditions were used to analyze the interpolymer samples:

• · ♦ »

Varian VXR-300, standard ^XH:

Frequency range: 5,000 Hz

Measurement time: 3,002 seconds Pulse width: 8 microseconds Frequency: 300 MHz Delay: 1 second Number of transitions: 16

The total analysis time for each sample was 10 minutes.

At the beginning it was measured ¹1 H NMR spectrum of a sample of polystyrene having a weight average molecular weight (M_w) about 192000, with a 1 second delay. Individual protons were "labeled as shown in Figure 1: b-proton bound to the carbon atom on which the branching occurred, α-proton bound to the α-carbon atom, o-proton bound in the ortho position, m-proton bound in the meta position, the p-proton bound in the para position.

<img file="CZ20011985A3_D0013.tif" />

Figure 1

The regions of the proton signals indicated in Figure 1 have been integrated, with the letter "A" indicating atactic polystyrene (aPS). The integral (aromatic region, chemical shift of approximately 7.1 ppm) was considered to be the signal of the three protons in the ortho and para positions; and the integral (the aromatic region). A chemical shift of approximately 6.6 ppm) was considered to be a signal of two protons in the meta position. The chemical shift of the two aliphatic protons designated as α was 1.5 ppm; and the chemical shift of the single proton labeled b was 1.9 ppm. The aliphatic region of the spectrum was integrated from a chemical shift value of 0.8 ppm to 2.5 ppm and designated as A_al. Theoretical ratio₇, i: A_E, ₆: A_andi is 3: 2: 3 and 1.5: 1: 1.5, respectively, and correlated very well with the ratios observed when measuring the spectra of said polystyrene sample for several lag times of 1 second. To calculate the integration and verify the correct assignment of the individual signals, the ratio calculations were performed by dividing the integral by the integral Αβ, 6 · Ratio A_r is the ratio Αγ, ι / Αβ, β ·

The area A6.6 was designated as value 1. The ratio A1 is the ratio A_andi / A₆6 All spectra obtained had the expected ratio of integrals of proton signals (o + p): m: (α + b) 1.5: 1: 1.5. The ratio of aromatic to aliphatic protons was 5 to 3. Based on the number of protons identified as protons a and b respectively in Figure 1, the expected ratio of aliphatic protons was 2 to 1. This ratio was also found when two aliphatic proton signals were integrated separately .

In the case of ethylene styrene interpolymers, the integrals in ^±1 H NMR spectra measured with a 1 second delay time denoted by C₇, i, Cg, 6 and C_andas defined by integrating the 7.1 ppm chemical shift signal including all aromatic proton signals of said copolymer and proton signals α and atactic polystyrene (aPS). Similarly, the integration of C signals_andeven in the aliphatic region of the spectrum, it included both atactic polystyrene (aPS) signals and those of the interpolymers, and it was not possible to distinguish the baseline of the signal of neither polymer. Signal integral with a chemical shift of 6.6 ppm denoted as C_{S; 6}it was well distinguished from other signals in the aromatic region and was considered to be a separate signal of an atactic polystyrene homopolymer (probably protons in the meta position).

(Based on comparison with signal of sample of polystyrene with weight average molecular weight (M_w) approximately 192000, this signal was assigned to the atactic polystyrene signal with a chemical shift of 6.6 ppm and its integral was designated as A₆6) This assumption was based on the observation that at a very low content of atactic polystyrene, only a very weak signal was observed in this region and therefore the phenyl protons of the copolymer could not contribute to the intensity of this signal. Based on this assumption, the value of the integral A has become_6|6 basis for quantitative determination of atactic polystyrene (aPS).

The following equations were used to determine the degree of styrene incorporation into the sample structure of ethylene styrene interpolymers:

(C phenyl) = C₇, i + A₇, i - (1.5 x A₆, s) (C aliphatic) = C_al - (1.5 x A₆₍₆) s_C = (C phenyl) / 5 e_C = (C aliphatic) - (3 xs_C) ) / 4

E = e_C / (e_C + s_C)

Sc - S_C / (6_C + Sc)

The molar percentage of ethylene and styrene in the interpolymers was calculated according to the following equations:

Weight Percentage E = [(E x 28) x 100] / [(E x 28) + (S_C x 104)]

<img file="CZ20011985A3_D0014.tif" />

and

Weight Percentage S = [(S_C x 104) x 100] / [(E x 28) + (S_C x 104)] where p_C ae_C are fractions of styrene and ethylene protons, respectively, contained in a given interpolymer

WITH_C and E molar fractions of styrene monomer and ethylene monomer, respectively, in said interpolymers.

The weight percent of atactic polystyrene (aPS) in the said interpolymers was calculated according to the equation

Weight % aPS = {[wt. % S x [(Ag. S / 2) / sec_C]] / [100+ wt. % S x [(A₆.₆/ 2) / p_C]]} x 100

Total styrene content was also determined by quantitative Fourier transform infrared spectroscopy (FTIR).

Preparation of ethylene styrene interpolymers (ESI) used in the following examples and comparative examples of the present invention

Ethylene styrene interpolymers (ESI) Nos. 1 to 7 were essentially statistical ethylene styrene interpolymers prepared using the catalysts below.

• · · «· · · · · • · · · ··· «·· • · · ♦ · · · · ·

Catalyst A - dimethyl [N- (1,1-dimethylethyl) -1,1-dimethyl-1 [(1,2,3,4,5-η) -1,5,6,7-tetrahydro-3-phenyl] -s-indacen-lyl] silanaminato (2 -) - N] -tetane

1) 3,5,6,7-Tetrahydro-s-hydrindacen-1 (2H) -one

94.00 grams (0.7954 mol) of indane and 100.99 grams (0.7954 mol) of 3-chloropropionyl chloride were stirred at 0 ° C in 300 ml of methylene chloride (CH).₂NO. 1₂) and under these conditions 130.00 grams (0.9750 mol) of aluminum chloride were slowly added to the mixture under a stream of nitrogen. The resulting mixture was then allowed to stir at room temperature for 2 hours. The volatiles were removed from the mixture, the residue was cooled to 0 ° C and slowly added

500 milliliters of concentrated sulfuric acid. The solid formed had to be frequently broken with a spatula, as stirring was interrupted at the very beginning of this step. The mixture was left under nitrogen at room temperature overnight and then heated to a temperature corresponding to 90 ° C read from the thermometers. These conditions were maintained for 2 hours, during which the mixture was regularly mixed with a spatula. After this time, ice mash was added to the mixture and mixed with the entire volume. The mixture was transferred to a beaker, washed alternately with water and ethyl ether, and the individual fractions were filtered and combined. The mixture was washed with 2 x 200 ml of water, the organic layers were separated and the volatiles removed. Recrystallization from hexane at 0 ° C isolated 22.36 g (16.3 percent) of the desired product as pale yellow crystals.

• · ···· ·· ······· ·· ·· ·· ¹HNMR (CDCl3): d2.04-2.19 (m, 2H), 2.65 (t, ³JKh = 5.7 Hz, 2H), 2.84-3.0 (m, 4H), 3.03 (t, ³J_HH= 5.5 Hz, 2H), 7.26 (s, 1H).

7.53 (s, 1 H).

¹³C NMR (CDCl3): d25.71, 26.01, 32.19, 33.24, 36.93, 118.90, 122.16, 135.88, 144.06, 152.89, 154.36, 206,50.

GC-MS: calcd for C12H12O 172.09, found 172.05.

2) 1,2,3,5-Tetrahydro-7-phenyl-s-indacene

12.00 grams (0.06967 mol) of 3,5,6,7-tetrahydrohydrindacen-1 (2H) -one was stirred in 200 ml of diethyl ether at 0 ° C and 35 was added slowly under these conditions. 00 ml of a 3.0 molar solution (0.105 mol) of phenylmagnesium bromide (PhMgBr) in diethyl ether. The resulting mixture was allowed to stir overnight at room temperature. After the reaction time, the mixture was quenched by pouring onto ice. The resulting mixture was acidified to pH 1 with hydrochloric acid and stirred vigorously for 2 hours. The separated organic layer was washed with 2 x 100 mL water and dried over anhydrous magnesium sulfate. After filtration and subsequent removal of the volatiles, 14.68 g (90.3 percent) of the desired product was obtained as a dark oil.^:1 H NMR (CDCl 3): d2.0-2.2 (m, 2H), 2.8-3.1 (m, 4H),

6.54 (s, 1H); 7.2-7.6 (m, 7H).

GC-MS: calculated for C18H16 232.13, found 232.05.

3) 1,2,3,5-tetrahydro-7-phenyl-s-indacene di-lithium salt

14.68 g (0.06291 mol) of 1,2,3,5-tetrahydro-7-phenyl-sindacene was stirred in 150 ml of hexane and to this mixture was slowly added 40.00 ml of a 2.0 molar solution

<img file="CZ20011985A3_D0015.tif" />

(0.080 mol) n-butyllithium (n-BuLi) in cyclohexane. The resulting mixture was allowed to stir overnight and after the reaction time, 12.2075 g (81.1 percent) of a solid was collected by suction filtration as a yellow solid which was washed with hexane, dried in vacuo and used in the next step without further purification; analysis.

4) Chlorodimethyl (1,5,6,7-tetrahydro-3-phenyl-s-indacen-1-yl) silane

A solution of 12.2075 grams (0.05102 mol) of dilithium salt

1,2,3,5-tetrahydro-7-phenyl-s-indacene in 50 ml tetrahydrofuran (THF) was added dropwise to a solution of 19.5010 g (0.1511 mol) of dichlorodimethylsilane (Me) at 0 ° C.₂SiCl 2) in 100 mL tetrahydrofuran (THF). The resulting mixture was allowed to stir overnight at room temperature. After the reaction time, the volatiles were removed, the distillation residue was extracted with hexane and filtered. After removal of hexane, 15.1492 g (91.1 percent) of the desired product was isolated.

<td>^and1 H NMR (</td><td>CDCl 3): d 0, 33 (s,</td><td colspan="2">3H), 0.38</td><td>(with,</td><td colspan="2">3H),</td>

<td>2.20 (p,</td><td>³J_hh= 7.5 Hz, 2H)</td><td> 2,</td><td> 9-3, 1</td><td>(m,</td><td>4H),</td><td>3.84 (s, 1 H),</td>

<td>6.69 (d,</td><td>³J_hh= 2.8 Hz, 1H)</td><td> 7,</td><td> 3-7,6</td><td>(m,</td><td>7H),</td><td></td>

<td>7.68 (d,</td><td>³ J HH = 7.4 Hz, 2H).</td><td></td><td></td><td></td><td></td><td></td>

<td>¹³C NMR</td><td>(CDCl 3): d 0.24, 0,</td><td> 38,</td><td> 26, 28</td><td> , 33</td><td> /05,</td><td> 33,18, 46,13,</td>

116,42, 119,71, 127,51, 128,33, 128,64, 129,56, 136,51,

141,31, 141,86, 142,17, 142,41, 144,62.

GC-MS: calcd₂oH₂iC1Si 324.11, found 324.05.

• ·· · · ·· ·· ♦ · ♦ · ··· ♦ · · • · ····· ·· • · · · · · · · ······· ·· ·· ·· ···

5) N- (1,1-Dimethylethyl) -1,1-dimethyl-1- (1,5,6,7-tetrahydro-3-phenyl-s-indacen-1-yl) silanamine

10.8277 grams (0.03322 moles) of chlorodimethyl (1,5,6,7-tetrahydro-3-phenyl-s-indacen-1-yl) silane was stirred in 150 ml of hexane and 3.5123 grams (0 , 03471 mol) triethylamine (Et₃N) and 2.6074 grams (0.03565 mol) of butylamine target. The resulting mixture was allowed to stir for 24 hours, filtered and after removal of the volatiles, 10.6551 g (88.7 percent) of the desired product was isolated as a thick red-yellow oil.

^X1 H NMR (CDCl 3)?₃): d 0.02 (s, 3H), 0.04 (s, 3H), 1.27 (s, 9H),

2.16 (p, ³J_hh= 7.2 Hz, 2H), 2.9-3.0 (m, 4H), 3.68 (s, 1H),

6.69 (s, 1H); 7.3-7.5 (m, 4H); 7.63 (d, ³JHH = 7.4Hz, 2H). ¹³C NMR (CDCl 3): d-0.32, -0.09, 26, 28, 33.39, 34.11, 46, 46,

47,54, 49,81, 115,80, 119,30, 126,92, 127,89, 128,46, 132,99,

137,30, 140,20, 140,81, 141,64, 142,08, 144,83.

6) N- (1,1-dimethylethyl) -1,1-dimethyl-1- (1,5,6,7-tetrahydro-3-phenyl-s-indacen-1-yl) silanamine di-lithium salt

10.6551 g (0.02947 mol) of N- (1,1-dimethylethyl) -1,1-dimethyl-1- (1,5,6,7-tetrahydro-3-phenyl-s-indacen-lyl) silanamine were stirred in 100 ml of hexane and to this mixture was slowly added 35.00 ml of a 2.0 molar solution (0.070 mol) of n-butyllithium (n-BuLi) in cyclohexane. The resulting mixture was allowed to stir overnight, during which time no salts precipitated out of the dark red solution. After the reaction time, the volatiles were removed from the mixture and the residue was washed rapidly with 2 x 50 mL hexane. Vacuum drying of a dark red residue was obtained

<img file="CZ20011985A3_D0016.tif" />

9.6517 g (87.7 percent) of the product used in the next step without further purification or analysis.

7) Dichloro [N- (1,1-dimethylethyl) -1,1-dimethyl-1 - [(1,2,3,4,5-η) -1,5,6,7-tetrahydro-3-phenyl] -s-indacen-lyl] silanaminato (2 -) - N] -tetane

A solution of 4.5355 grams (0.01214 mol) of the dilithium salt of N- (1,1-dimethylethyl) -1,1-dimethyl-1- (1,5,6,7-tetrahydro-3-phenylsindacen-1-yl) of silanamine in 50 mL of tetrahydrofuran (THF) was added dropwise to a suspension of 4.5005 g (0.01214 mol) of TiCl 3 (THF) 3 in 100 mL of tetrahydrofuran (THF). The mixture was stirred for 2 hours and then 1.7136 grams (0.006162 mol) of lead chloride was added and the mixture was allowed to stir for an additional hour. After the reaction time, the volatiles were removed from the mixture, the residue was extracted with toluene and filtered. After removal of toluene, a dark residue was isolated, which was suspended in hexane, and the resulting suspension was cooled to 0 ° C. 2.5280 g (43.5 percent) of the desired product was isolated by filtration as a reddish brown crystalline solid.

NMR (CDCl3)₃): d0.71 (s, 3H), 0.97 (s, 3H), 1.37 (s, 9H), 2.0-2.2 (m, 2H), 2.9-3.2 ( m, 4H), 6.62 (s, 1H), 7.35-7.45 (m, 1H), 7.50 (t, ³J_hh= 7.8 Hz, 2H), 7.57 (s, 1H).

7.70 (t, ³J_Hh = 7.1 Hz, 2H), 7.78 (s, 1H).

<td>¹H</td><td>NMR</td><td>(C₆D₆)</td><td>: dO</td><td>, 44 (s,</td><td>&gt; 3H), 0</td><td> 68</td><td>(s, 3H)</td><td> 1,35</td><td>(s, 9H)</td>

<td> 1,</td><td> 6-1, 9</td><td>(m,</td><td>2H),</td><td> 2,5-3,</td><td>9 (m, 4H)</td><td> ) ,</td><td>6.65 (s,</td><td>1H),</td><td></td>

<td> 7,</td><td> 1-7,2</td><td>(m,</td><td>1H),</td><td> 7,24</td><td>(t, 'Jhh⁼7</td><td> ,1</td><td>Hz, 2H)</td><td> 7,61</td><td>(s, 1 H),</td>

<td> 7,</td><td>69 (p</td><td>, 1H)</td><td> , 7,</td><td> 77-7,8</td><td>(m, 2H).</td><td></td><td></td><td></td><td></td>

<td colspan="2">¹³C NMR</td><td>(CDC.</td><td>h):</td><td>dl, 29,</td><td> 3,89, 26</td><td> ,47</td><td> , 32,62,</td><td> 32,84</td><td> , 32,92,</td>

<img file="CZ20011985A3_D0017.tif" />

<img file="CZ20011985A3_D0018.tif" />

63,16, 98,25, 118,70, 121,75, 125,62, 128,46, 128,55, 128,79, 129,01, 134,11, 134,53, 136,04, 146,15, 148,93.

¹³C NMR (C₆D₆): d0, 90, 3.57, 26.46, 32.56, 32.78, 62.88, 98, 14,

119,19, 121,97, 125,84, 127,15, 128,83, 129,03, 129,55,

134,57, 135,04, 136,41, 136,51, 147,24, 148,96.

8) Dimethyl [N- (1,1-dimethylethyl) -1,1-dimethyl-1 - [(1,2,3,4,5η) -1,5,6,7-tetrahydro-3-phenyl-s] (indacen-1-yl) silanaminato (2-) N] titanium

0.4970 grams (0.001039 mol) dichloro [N- (1,1-dimethylethyl) -1,1-dimethyl-1 - [(1,2,3,4,5-η) -1,5,6,7-tetrahydro] 3-phenyl-s-indacen-1-yl] silanaminato (2 -) - N] titanium was stirred in 50 ml diethyl ether and 0.70 ml of a 3.0 molar solution (0.0021 mol) was slowly added. of methylmagnesium bromide (MeMgBr) in diethyl ether. The resulting mixture was stirred for 1 hour. After the reaction time, the volatiles were removed from the mixture and the residue was extracted with hexane and filtered. Removal of the hexane gave 0.4546 g (66.7 percent) of the desired product as a golden yellow solid.

¹HNMR (C₆D₆): d 0.071 (s, 3H), 0.49 (s, 3H), 0.70 (s, 3H),

0.73 (s, 3H), 1.49 (s, 9H), 1.7-1.8 (m, 2H), 2.5-2.8 (m, 4H),

6.41 (s, 1H); 7.29 (t, ³J_HK= 7.4 Hz, 2H), 7.48 (s, 1H),

7.72 (t, ³J_hh= 7.4 Hz, 2H), 7.92 (s, 1H).

¹³C NMR (C₆D_WITH): d2.19, 4, 61, 27.12, 32.86, 33.00, 34.73, 58, 68, 58.82, 118.62, 121.98, 124.26, 127.32, 128.63, 128.98, 131.23,

134,39, 136,38, 143,19, 144,85.

···· · · · · · · • · · · · · · ··

Catalyst Β - (ΙΗ-cyclopenta [1] phenanthren-2-yl) dimethyl (tert-butylamido) silanetitanium 1,4-diphenylbutadiene

1) (1H-Cyclopenta [1] phenanthren-2-yl) lithium

In a 250 ml round - bottomed flask containing

1.42 g (0.00657 mol) of 1H-cyclopenta [1] phenanthrene a

120 ml of benzene was added dropwise to 4.2 ml

1.60 molar solution of n-butyllithium (n-BuLi) in hexanes. The solution was allowed to stir overnight. The resulting lithium salt was isolated by filtration, washed twice with 25 ml of benzene and dried under vacuum. The isolated yield was 1.426 grams (97.7 percent). Analysis³By NMR spectroscopy it was found that the predominant isomer was substituted at the 2-position.

2) (1H-Cyclopenta [1] phenanthren-2-yl) dimethylchlorosilane

In a 500 ml round - bottomed flask containing

4.16 g (0.0322 mol) of dimethyldichlorosilane (Me₂SiCl₂ and

250 ml of tetrahydrofuran (THF) was added dropwise

1.45 g (0.0064 mol) of (1H-cyclopenta [1] phenanthren-2-yl) lithium in tetrahydrofuran (THF). The resulting solution was stirred for about 16 hours, after which time the solvent was removed in vacuo. The residual oily solid was extracted with toluene, filtered through diatomaceous earth (Celite®), washed twice with toluene and dried under reduced pressure. 1.98 g (99.5 percent) of product was isolated.

• to • •• to ·

3) (1H-Cyclopenta [1] phenanthren-2-yl) dimethyl (tert-butylamino) silane

In a 500 ml round-bottom flask containing 1.98 g (0.0064 mol) of (1H-cyclopenta [1] phenanthren-2-yl) dimethylchlorosilane and 250 ml of hexane were added 2.00 ml (0.0160 mol) of the target, butylamine. The reaction mixture was allowed to stir for several days and was then filtered through diatomaceous earth filter aid (Celite®), washed twice with hexane. After removal of solvent residues under reduced pressure, 1.98 g (88.9 percent) of the product was isolated.

4) Dilithio (1H-cyclopenta [1] phenanthren-2-yl) dimethyl (tert-butylamido) silane

A 250 ml round bottom flask containing 1.03 g (0.0030 mol) of (1H-cyclopenta [1] phenanthren-2-yl) dimethyl (tert-butylamino) silane and 120 ml of benzene was added dropwise to 3.90 ml 1, 60 molar solution of n-butyllithium (n-BuLi) in hexanes. The mixture was stirred for approximately 16 hours. The resulting product was isolated by filtration, washed twice with benzene and dried in vacuo. The isolated yield was 1.08 g (100 percent).

5) (1H-Cyclopenta [1] phenanthren-2-yl) dimethyl (tert-butylamido) silanetitanium dichloride

In a 250 ml round - bottomed flask containing

1.17 g (0.0030 mol) TiCl₃3THF and about 120 milliliters of tetrahydrofuran (THF) were added dropwise at a rapid rate with milliliters of a tetrahydrofuran solution of 1.08 grams of dilithio (1H-cyclopenta [1] phenanthren-2-yl). Dimethyl (t-butylamido) silane. The mixture was stirred at 20 ° C for 1.5 hours, during which time 0.55 g (0.002 mol) of solid lead chloride was added. The mixture was stirred for an additional 1.5 hours and then tetrahydrofuran (THF) was removed in vacuo. The residue was extracted with toluene, filtered and dried under reduced pressure. It was obtained

1.31 g (93.5 percent) of the product as an orange solid.

6) (1H-Cyclopenta [1] phenanthren-2-yl) dimethyl (tert-butylamido) silanetitanium 1,4-diphenylbutadiene

To a suspension of 3.48 g (0.0075 mol) of (ΙΗ-cyclopenta [1] phenanthren-2-yl) dimethyl (tert-butylamido) silanetitanium dichloride and 1.551 g (0.0075 mol)

1,4-diphenylbutadiene in 80 ml of toluene was added at 70 ° C 9.9 ml of a 1.6 molar solution (0.0150 mol) of n-butyllithium (n-BuLi). The mixture immediately darkened, the temperature was raised so that the reaction mixture refluxed and this temperature was maintained for 2 hours. Subsequently, the mixture was cooled to -20 ° C and the volatiles removed in vacuo. The residue was suspended at 20 ° C in 60 ml of hexanes and stirred for about 16 hours. The mixture was cooled to -25 ° C for 1 hour and the solids were collected by vacuum filtration through a glass frit and dried under reduced pressure. The dried solids were placed in a glass fiber cartridge and continuously extracted with hexanes in a Soxhlet extractor. After six hours of extraction, a crystalline solid was observed in the cooking vessel. The blend was "" "", "", "", "", "", "", " After cooling to -20 ° C, a solid was isolated from the cold mixture by filtration and dried under reduced pressure to give 1.62 g of a dark crystalline solid. The filtrate obtained was set aside. The solids remaining in the extractor were mixed, and further extraction with a supplemented amount of hexanes gave an additional 0.46 g of the desired product as a dark crystalline solid.

Polymerization of ethylene styrene interpolymers (ESI) 1 and 2

Ethylene styrene interpolymers (ESI) 1 and 2 were produced in an autoclave continuously stirred tank reactor (CSTR) of 22.7 liters (6 gallons) with oil jacket. Mixing was provided by a magnetically coupled stirrer with Lightning A-320 blades. The reactor was charged with liquid at a pressure of 3275 kilopascals (475 psig). The process was arranged such that the inlet of the reactor was located at its bottom and the outlet of the reactor was located at its top. The heat transfer oil circulated through the housing to remove heat released during the reaction. A microkinetic flow meter was placed at the reactor outlet to measure the flow rate and density of the solution. All pipes at the reactor outlet were heated with water pressure of 344.7 kilopascals (50 psi) and isolated.

The toluene solvent was fed to the reactor at a pressure of 207 kPa (30 psig). The amount of feed fed to the reactor was measured by a mass flow meter

Micro-Motion and feed rate were controlled by an adjustable diaphragm pump. At the outlet of the solvent pump were: · · · · · · «· w · · · · · · · · · a · a a And a side stream is taken to provide a purge of the catalyst feed line (at a rate of 1 pound / hour) and the reactor stirrer. (at a rate of 0.34 kilograms / hour (0.75 pounds / hour)). These flow rates were measured by differential pressure flow meters and controlled by manually adjusting micro flow needle valves. The uninhibited styrene monomer was fed to the reactor at a pressure of 207 kilopascals (30 psig). The feed rate fed to the reactor was measured with a Micro-Motion mass flowmeter and the feed rate was controlled by an adjustable diaphragm pump. The styrene stream was mixed with the remaining solvent stream.

Ethylene was fed to the reactor under pressure

4137 kilopascals (600 psig). The amount of ethylene feed was measured with a Micro-Motion mass flow meter just in front of the Research Flow Control Valve. A Brooks flowmeter / flow controller was used to add hydrogen to the ethylene stream at the outlet of the ethylene control valve. The ethylene / hydrogen mixture was combined with the solvent / styrene stream at ambient temperature. The temperature of the solvent / monomer mixture stream was lowered to about 5 ° C at the inlet of the reactor via a -5 ° C glycol-filled heat exchanger located on the reactor jacket. This stream was injected into the bottom of the reactor.

The three-component catalyst system and solvent flushing stream was also fed to the bottom of the reactor, but at a location different from the point where the monomer stream was fed into the reactor.

The preparation of the catalyst components was carried out in a container with an inert 9 [deg.] C. &amp; lt; tb &amp; gt; &amp; lt; tb &amp; gt; · 4 «4« “3« · «·· ·· ··« 4 · »· atmosphere. The diluted components were placed in nitrogen-filled cylinders and fed to the catalyst pressure vessels at the process site. From these catalyst pressure vessels, the catalyst was extruded by piston pumps, and the catalyst flow rate was measured by Micro-Motion mass flow meters. Said streams were mixed with each other and with a catalyst flushing stream just prior to feed into the reactor through a single feed line.

The polymerization was stopped by adding a catalyst poison, which was mixed with water to the solvent, into the product discharge line from the reactor after measuring the density of the solution with a microkinetic flow meter. Other polymeric additives could be added along with the catalyst poison. The static mixer located on this line provided the catalyst poison dispersion in the reactor effluent. This outlet stream further entered the heaters downstream of the reactor, which were the source of additional energy needed to evaporate the solvent. This evaporation occurred as the outlet stream exited the heater downstream of the reactor and once the pressure in the reactor pressure control valve decreased from 3275 kilopascals (475 psig) to approximately 333.31 kilopascals (250 millimeters absolute pressure). The polymer from which the solvents were thus evaporated was introduced into a volatile removal apparatus equipped with an oil jacket and approximately 85 percent of the volatiles were removed from the polymer. The volatile components have left the device for removal from the top of the device. The stream of volatile components was condensed in a glycol-coated heat exchanger, sucked in by a vacuum pump, and discharged into a solvent separation vessel and a blend comprising styrene and ethylene that was &amp; lt; Desc / Clms Page number 3 &amp; gt; It is provided with a glycol-filled sheath. Solvent and styrene were removed from the bottom of the vessel while ethylene was removed from the top of the vessel. The ethylene stream was measured with a Micro-Motion mass flow meter and its composition was analyzed. The measurement of the amount of degassed ethylene together with the calculated amount of dissolved gases in the stream, which included solvent and styrene, served to calculate the conversion of ethylene. The polymer separated in the devolatilizer was pumped by a gear pump into a vacuum extruder for the devolatilizer ZSK-30. In this extruder, the dry polymer was in the form of a single strip which was cooled by stretching through a water bath. The excess water was blown out of the strip by air, which was then cut into pellets using a strip cutter.

Polymerization of ethylene styrene interpolymers (ESI) 3 to 7

Ethylene styrene interpolymers (ESI) Nos. 3 to 7 were produced in a 139.3 liter (36.8 gallon) continuous loop reactor. Mixing was provided by a Ingersoll-Dresser twin-screw pump. The reactor was completely filled with liquid and operated at a pressure of 3275 kilopascals (475 psig) with a residence time of approximately 25 minutes. Single streams including feedstock and catalyst / cocatalyst mixture were fed through Kenics injectors and static mixers into the intake manifold of the two-screw pump, which led to a 2 inch diameter line to feed two Chemineer heat exchangers. -Kenics 10-38 Type BEM Multi-Tube plugged in series. To increase the heat transfer, the tubes in these heat exchangers were provided with coiled tapes. After the output • · · · · · φφφφ

<img file="CZ20011985A3_D0019.tif" />

from the last heat exchanger, the loop current was returned through injectors and static mixers to the pump suction line. The temperature probe temperature measurement of the loop current, which was located just before entering the first heat exchanger, was ensured by the heat transfer oil circulated in the heat exchanger shells. The loop reactor current was split between two heat exchangers and its flow and density were measured with a Micro-Motion device.

The solvent was fed to the reactor from two sources. A fresh stream of toluene was fed through a 8480-SE Pulsafeeder diaphragm pump at a rate measured by a MicroMotion flow meter at a rate such that the reactor caps were flushed, namely 9.1 kilograms / hour (20 lb / hour). The recycled solvent was mixed with uninhibited styrene monomer on the suction side of five parallel-connected 8480-SE Pulsafeeder diaphragm pumps, and the five Pulsafeeder pumps supplied the solvent together with styrene to the reactor at a pressure of 4583 kilopascal (650 psig). The flow of fresh styrene was measured with a Micro-Motion flowmeter, with the total current flow, including recycled solvent and styrene, measured with a separate Micro-Motion flowmeter. Ethylene was fed to the reactor under a pressure of 4838 kilopascals (687 psig) and was measured with a MicroMotion mass flowmeter. A Brooks flowmeter / regulator was used to add hydrogen to the ethylene stream at the outlet of the ethylene flow control valve.

The combination of ethylene and hydrogen with a stream comprising a mixture of solvent and styrene occurred at ambient temperature.

• Φ Φ φ · · Φ ·· φ φ φ φ φ φ φ φφ

The temperature of the resulting stream at the inlet to the reactor was reduced to 2 ° C, which was achieved by means of a heat exchanger whose jacket contained glycol cooled to -10 ° C. The above catalyst components were prepared in three separate vessels: fresh solvent and a concentrated premixed catalyst / cocatalyst mixture were added to the respective reaction vessels in which they were mixed and injected via a variable speed membrane pump 680-S-AEN7 Pulsafeeder into the reactor. As mentioned above, the three-component catalyst system was fed to the reactor loop through a twin-screw pump, the intake manifold of which entered the injector and static mixer. The feed stream was also injected into the reactor loop using an injector and a static mixer located downstream of the catalyst feed point but upstream of the twin screw pump suction line.

The polymerization was stopped by adding catalyst poison, which was mixed with the solvent, to the product line from the reactor after measuring the density of the solution with a Micro-Motion flow meter. The static mixer located on this line provided the catalyst poison dispersion in the reactor effluent. This outlet stream further entered the heaters downstream of the reactor, which were the source of additional energy needed to evaporate the solvent. This evaporation occurred as the outlet stream exited the heater downstream of the reactor and once the pressure in the reactor pressure control valve decreased from 3275 kilopascals (475 psig) to 60 kilopascals (450 millimeters of mercury).

The polymer from which the solvents were thus vaporized entered the first of two volatile removal devices equipped with shells filled with hot oil. The volatile components exiting the first volatile component removal apparatus condensed in a glycol-cooled heat exchanger, passed through the vacuum pump suction line and were fed to a solvent separation vessel and a mixture comprising ethylene and styrene. The mixture comprising solvent and styrene was removed at the bottom of the vessel and served as a recycled solvent while ethylene was removed from the top of the vessel. The ethylene stream was measured with a Micro-Motion mass flow meter. Measurement of the amount of degassed ethylene along with the calculated amount of dissolved gases in the stream that included solvent and styrene served to calculate the conversion of ethylene. The polymer separated in the volatile removal device, together with the solvent residues, was pumped by a gear pump into the second volatile removal device. In order to evaporate the solvent residues, the pressure in this second solvent removal device was reduced to 0.7 kilopascal (5 millimeters of mercury). This solvent was condensed in a glycol-cooled heat exchanger and was transferred to another container for disposal in a container ready for disposal. The dry polymer (total volatile content &amp; lt; 1000 ppm) was fed by a gear pump to a pelletizing machine in which the polymer was cooled by drawing through a water bath and equipped with a six-hole slot. The pellets formed were centrifuged and collected in crates weighing 453.6 kilograms (1000 pounds).

Table 1 lists the various catalysts, cocatalysts, and polymerization process conditions that were

<img file="CZ20011985A3_D0020.tif" />

used in the manufacture of said ethylene-styrene interpolymers (ESI) Nos. 1 to 7. The properties of these polymers are shown in Table 2.

Table 1

<td>ESI number</td><td>Temperature in the reactor Deň: 32 ° C</td><td>Solvent flow rate kg / h (lb / h)</td><td>Ethylene flow kg / hour (lb / hour)</td><td>Hydrogen flow cm³/ min</td><td>Styrene flow kg / h (lb / h)</td>

<td> 1</td><td> 93,0</td><td> 17,2 (37,9)</td><td> 1,4 (3,1)</td><td> 13, 5</td><td> 3,1 (6,9)</td>

<td> 2</td><td> 79, 0</td><td> 14,2 (31,3)</td><td> 0,8 (1,7)</td><td> 4,3</td><td> 6,1 (13,5)</td>

<td> 3</td><td> 88,0</td><td> 268 (590)</td><td> 25 (55)</td><td> 250</td><td> 60 (133)</td>

<td> 4</td><td> 83</td><td> 202 (445)</td><td> 19,5 (43)</td><td> 235</td><td> 41 (91)</td>

<td> 5</td><td> 61</td><td> 175,0 (386)</td><td> 9,1 (20,0)</td><td> 0</td><td> 45 (100)</td>

<td> 6</td><td> 87,0</td><td> 363 (800)</td><td> 38 (83)</td><td> 569</td><td> 89 (197)</td>

<td> 7</td><td> 81,0</td><td> 362 (799)</td><td> 29 (65)</td><td> 500</td><td> 112 (247)</td>

<img file="CZ20011985A3_D0021.tif" />

Table 1 - Completion

<td>ESI number</td><td>Ethylene conversion O. 0</td><td>Ratio B / Ti</td><td>Ratio MMAO^d/ Ti</td><td>Catalyst</td><td>Cocatalyst</td>

<td> 1</td><td> 96,21</td><td> 2, 99</td><td> 7,0</td><td>AND^and</td><td>C^C</td>

<td> 2</td><td> 95, 1</td><td> 3,51</td><td> 9,0</td><td>AND^and</td><td>C^C</td>

<td> 3</td><td> 94, 0</td><td> 3, 50</td><td> 4,9</td><td>B °</td><td>C^b</td>

<td> 4</td><td> 94,0</td><td> 6, 0</td><td> 16,0</td><td>(B)^b</td><td>C^C</td>

<td> 5</td><td> 88</td><td> 3, 50</td><td> 2, 5</td><td>(B)^b</td><td>C^C</td>

<td> 6</td><td> 93, 0</td><td> 4,00</td><td> 6,0</td><td>(B)^b</td><td>C^C</td>

<td> 7</td><td> 95</td><td> 3,70</td><td> 6, 0</td><td>(B)^b</td><td>C^C</td>

and Catalyst A was dimethyl [N- (1,1-dimethylethyl) -1,1-dimethyl-1 - [(1,2,3,4,5-η) -1,5,6,7-tetrahydro-3-phenyl] -sindacen-1-yl] silanaminato (2 -) - N] -titan b Catalyst B was (1H-cyclopenta [1] phenanthren-2-yl) dimethyl (tert-butylamido) silanetitanium

1,4-Diphenylbutadiene c Cocatalyst C was tris (pentafluorophenyl) borane (CAS 001109-15-5) d Modified methylaluminoxane, commercially available as

MMA0-3A by Akzo Nobel (CAS 146905-79-5)

Table 2

Properties of ethylene styrene interpolymers (ESI) 1 to 7

<td>ESI number</td><td>Styrene content (% by weight)</td><td>Content styrene (mole%)</td><td>Content of aPS¹(wt%)</td><td>Melt flow index₂(g / 10 min)</td><td>Number Góttfert (cmV10 min)</td>

<td> 1</td><td> 47,4</td><td> 19, 5</td><td> 0,5</td><td></td><td> 1,54</td>

<td> 2</td><td> 69, 0</td><td> 37,5</td><td> 1,6</td><td></td><td> 1,36</td>

<td> 3</td><td> 44,6</td><td> 17,8</td><td> 11,5</td><td> 1,52</td><td></td>

<td> 4</td><td> 63,7</td><td> 32,1</td><td>ON</td><td> 0,61</td><td></td>

<td> 5</td><td> 69, 5</td><td> 38,0</td><td> 8,9</td><td> 0,94</td><td></td>

<td> 6</td><td> 61,7</td><td> 30,2</td><td> 2,9</td><td> 0,63</td><td></td>

<td> 7</td><td> 70, 6</td><td> 39,3</td><td>t - 1 kO</td><td> 1,17</td><td></td>

aPS = atactic polystyrene

N / A Not available

Other components of the mixture

PS 1 was a granulated polystyrene having a weight average molecular weight (M_w) was approximately 192000 and whose polydispersity expressed as the ratio of weight average molecular weight to number average molecular weight (M_w/ M_n) was approximately 2.

PS 2 was a granulated polystyrene having a weight average molecular weight (M_w) was approximately 305000 and whose polydispersity expressed as the ratio of the weight average molecular weight to the number average molecular weight (M_w/ M_n) was approximately 2.

4 · · 4 4 · · 4 • 4444444 • 4 4444 4 4·

4· · · 4 4 4 44

4444444

4444444 44 44 4 · 444

LDPE 1 was a low density polyethylene whose melt index I₂ was 1.8 grams / 10 minutes with a weight average molecular weight of 117600, a number average molecular weight of 17200 and a density of 0.9230 grams / cm³.

LDPE 2 was a low density polyethylene whose melt index I₂ was 2.4 grams / 10 minutes, having a weight average molecular weight of 98300, a number average molecular weight of 13300 and a density of 0.9241 grams / cm³.

Examples 1 to 4

In these examples, a foaming method was used to form the foam, using a single screw extruder, mixer, cooler and slot. Isobutane was used as a blowing agent for foaming the LDPE and PS / ESI mixtures

7.5 parts per 100 parts polymer (phr). Table 3 summarizes the properties of the individual foams. All of these foams were soft and resilient to the touch, at the same time consisting of small cell size, fine surface, good dimensional stability, and a wide range of open cell content values. In contrast to a comparative sample of non-crosslinked foam made from low density polyethylene (LDPE) (Comparative Example 1), there was no significant shrinkage of the foams of the present invention (i.e. foams) as measured by volume change (calculated from weight and density of the foam). according to Examples 1 to 4) during their curing at room temperature.

• · • · ·· ···· · · ······· · · · · · · ·

Table 3 Foams formed from mixtures of polystyrene (PS) and ethylene styrene interpolymers (ESI) in which isobutane was used as a blowing agent

<td>Example</td><td>Composition of the mixture (wt%)</td><td>Foaming temperature (° C)</td><td>Foam density (kilogram / m³)</td>

<td> 1</td><td>50% PS1 / 50% ESIl</td><td> 122</td><td> 46,2</td>

<td> 2</td><td>50% PS1 / 50% ESIl</td><td> 112</td><td> 54,7</td>

<td> 3</td><td>50% PS1 / 50% ESI2</td><td> 112</td><td> 65,2</td>

<td> 4</td><td>50% PS1 / 50% ESI2</td><td> 102</td><td> 74,4</td>

<td> 1*</td><td>100% LDPE1</td><td> 112</td><td> 37,7</td>

<td>Example</td><td>Percentage of open cells</td><td>Cell size (millimeter)</td><td>Maximum volume change at 23 ° C (v / v)</td>

<td> 1</td><td> 54,6</td><td> 0,21</td><td> -3,2</td>

<td> 2</td><td> 87,3</td><td> 0,30</td><td> -3,2</td>

<td> 3</td><td> 81,1</td><td> 0,09</td><td> -3,4</td>

<td> 4</td><td> 65, 9</td><td> 0,12</td><td> -2,3</td>

<td> 1*</td><td> 4,5</td><td> 1, 63</td><td> -28,5</td>

Comparative experiment

Examples 5 to 9

To produce foam elongate blanks, a foaming method was used in these examples, including using a single screw extruder, mixer, coolers and slots. Isobutane and HCFC-142b were used as a blowing agent for foaming low density polyethylene (LDPE) and a mixture of polystyrene and ethylene styrene interpolymers (ESI). In addition to the blends of Examples 5-9 and Comparative Example 2, an additive was added to the blends of Examples 5 to 9 and Comparative Example 2. ·· ·· ·· ·

Irganox® 1010 (manufactured by Ciba-Geigy) in an amount of 0.06 parts per 100 parts polymer (phr). In Comparative Example 2, 0.2 parts per 100 parts polymer (phr) of Hydrocerol® CF40E (manufactured by Boehringer Ingelheim), which served as a nucleating agent, and 0.5 parts per 100 parts polymer (phr) of glycerol monostearate were also used. , which served as a permeability modification agent. In Comparative Example 3, the following additives were used: hexabromocyclododecane (2.5 parts per 100 parts polymer (phr)), barium stearate (0.2 parts per 100 parts polymer (phr)), blue pigment (0.15 parts per 100 parts) parts of polymer (phr)), sodium pyrophosphate (0.2 parts per 100 parts polymer (phr)), linear low density polyethylene (0.4 parts per 100 parts polymer (phr)). In all examples, the foams whose properties are summarized in Table 4 were soft and resilient and whose Asker C hardness was close to that of conventional low density polyethylene (LDPE) foams used for the production of resilient fillers, such a foam being prepared. in Comparative Example 2. At the same time, the foams were much softer than the foam prepared in Comparative Example 3, which was a foam formed on the basis of a 80:20 mixture of polystyrene and ethylene styrene interpolymer (ESI).

9 9 9

Table 4 Properties of PS / ESI based foams

<td>Percentage of open cells</td><td>03 / OJ</td><td colspan="2"> 03</td><td colspan="2"> 30,8</td><td colspan="2"> 34,4</td><td> 58,3</td><td colspan="2">Γ —Ι — 1</td><td> 03</td>

<td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td>μ</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td></td><td>O</td><td>O</td><td></td><td> 00</td><td></td><td>O</td><td></td><td>O</td><td>SX&gt;</td><td></td><td>IX</td>

<td></td><td>r-</td><td>kO</td><td></td><td>lC</td><td></td><td>kO</td><td></td><td>lD</td><td></td><td></td><td></td>

<td>&gt; ω</td><td>r * 4</td><td> &lt;—1</td><td></td><td>i — 1</td><td></td><td> !-----1</td><td></td><td>i — 1</td><td>t — l</td><td></td><td>i — 1</td>

<td>• r-1</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td> £</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td>rrj M • MX</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td>V)&gt; 01</td><td>cn</td><td>OJ</td><td></td><td>r4</td><td></td><td>OJ</td><td></td><td>O</td><td> 1------1</td><td></td><td> 03</td>

<td>D · Η O rH i-1 -H H £</td><td>i-4</td><td>OJ</td><td></td><td>C\</td><td></td><td>OJ</td><td></td><td>OJ</td><td>CN</td><td></td><td> 03</td>

<td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td>her? x; cC?. o £</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td>φ \</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td>^and CE</td><td>03 / •with</td><td> 1—1</td><td></td><td>k £&gt;</td><td></td><td>3Ώ</td><td></td><td>what</td><td>WHAT</td><td></td><td>O with.</td>

<td>o ° ý ko o</td><td>10 OJ</td><td>lD OJ</td><td></td><td>sr OJ</td><td></td><td>OJ</td><td></td><td>co OJ</td><td>cn CN</td><td></td><td>CJ 03 /</td>

<td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td>= &amp; s</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td>² 1 0 x Γ?</td><td>• ^ r</td><td></td><td></td><td>LD</td><td></td><td></td><td></td><td>O</td><td>i — 1</td><td></td><td>r ~ 1</td>

<td>L oo</td><td></td><td></td><td></td><td>t — 1</td><td></td><td>t-4</td><td></td><td>and-</td><td>t — 1</td><td></td><td>OJ</td>

<td>&gt; U &lt; ^at £ ~</td><td>t — l</td><td>i — 1</td><td></td><td>t — 1</td><td></td><td>i — 1</td><td></td><td>and-</td><td> 1—1</td><td></td><td>i — 1</td>

<td>C</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td>0 i — 1</td><td>C</td><td>C</td><td></td><td>C</td><td></td><td>C</td><td></td><td>C</td><td>C</td><td rowspan="2">and</td><td rowspan="2">X</td>

<td>Ό</td><td>φ M</td><td>Γ0</td><td></td><td>rO</td><td></td><td> 05</td><td>and</td><td></td><td>ω</td>

<td>Π3</td><td>4-&gt; X!</td><td> 4-&gt;</td><td> £</td><td> 4-&gt;</td><td>X!</td><td>4-S</td><td>x</td><td>and&gt; x</td><td> 4-1</td><td>X</td><td>S £</td>

<td> &gt;</td><td>2 ft</td><td></td><td>CL</td><td></td><td>Λ</td><td> 5</td><td>and,</td><td>da</td><td> •3</td><td>Cl</td><td> 7 ^and</td>

<td></td><td>Xi</td><td>X</td><td></td><td>Xi</td><td></td><td>X!</td><td></td><td>Xi</td><td>r&gt;</td><td></td><td rowspan="2"></td>

<td>O</td><td>O o</td><td>O</td><td>O</td><td> 0</td><td>O</td><td> 0</td><td>C</td><td>0 o</td><td>O</td><td>O</td>

<td>Ό</td><td>CO r-1</td><td>what</td><td>r — 1</td><td>what</td><td>i — 1</td><td>WHAT</td><td>i — 1</td><td>CO r-4</td><td>what</td><td>r — 1</td><td rowspan="3">WITH ^MTO</td>

<td>rú</td><td>• H</td><td>• H</td><td></td><td> •1—1</td><td></td><td>• H</td><td></td><td>-H</td><td>-H</td><td></td>

<td>of</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td></td><td> 03</td><td></td><td></td><td>'ντ</td><td></td><td></td><td></td><td></td><td></td><td></td><td>ui3</td>

<td>• H</td><td> 1-4</td><td> 1—1</td><td></td><td>h-4</td><td></td><td>h4</td><td></td><td>M</td><td></td><td></td><td> 1-4</td>

<td>what</td><td>ω</td><td>ω</td><td></td><td>WHAT</td><td></td><td>ω</td><td></td><td>ω</td><td rowspan="3">CJ ω Ch</td><td></td><td>ω</td>

<td rowspan="2">&gt; ω ,,</td><td>ω</td><td>the</td><td></td><td>the</td><td></td><td>ω</td><td></td><td>ω</td><td></td><td>the</td>

<td>ο \ °</td><td>o \ o</td><td></td><td>O \ o</td><td></td><td>ο \ °</td><td></td><td>ο \ °</td><td></td><td>o \ o</td>

<td></td><td>O</td><td>O</td><td></td><td>O</td><td></td><td>O</td><td></td><td>O</td><td> 0</td><td></td><td>O</td>

<td rowspan="2"> . ^Cc + - o</td><td></td><td></td><td></td><td>lD</td><td></td><td>m</td><td></td><td>ιη</td><td> 0</td><td></td><td>OJ</td>

<td>i — 1</td><td>t — 1</td><td></td><td>\ t—!</td><td></td><td>r-4</td><td></td><td>\ and-</td><td>o \ °</td><td></td><td>i-4</td>

<td></td><td>ω</td><td>ω</td><td></td><td>ω</td><td></td><td>ω</td><td></td><td>ω</td><td></td><td></td><td>ω</td>

<td rowspan="2">&gt; N p about you</td><td>(X</td><td>Pj</td><td></td><td>Dli</td><td></td><td>CL</td><td></td><td>CL</td><td></td><td></td><td> 04</td>

<td>Ο \ ο</td><td>o \ °</td><td></td><td>o \ P</td><td></td><td>o \ o</td><td></td><td>o \ °</td><td></td><td></td><td> 0\°</td>

<td>r — 1</td><td>O</td><td>O</td><td></td><td>O</td><td></td><td>O</td><td></td><td>O</td><td></td><td></td><td>O</td>

<td>C / 3</td><td>kO</td><td>kO</td><td></td><td>lD</td><td></td><td>iD</td><td></td><td>lD</td><td></td><td></td><td>what</td>

<td>Ό</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td>i — 1</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td rowspan="2"> 03</td><td>-TO</td><td></td><td> *</td>

<td></td><td>10)</td><td>kO</td><td></td><td></td><td></td><td>WHAT</td><td></td><td>OJ</td><td></td><td>m</td>

<td>&gt; C4</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

<td>Cl</td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td><td></td>

···· ··· · · · • · · · · · · · · ·· ···· · · · ······· · · · · · · ···

Table 4 Properties of PS / ESI based foams - Finish

<td>Thermal conductivity λ (10 ° C mW / mK)</td><td> 32,6</td><td> 31,8</td><td> 34,2</td><td> 34,7</td><td> 34,3</td><td>of</td><td> 28,3</td>

<td>Maximum longitudinal change at 70 ° C (percentage)</td><td> + 2,0</td><td>OJ r-4 1</td><td>WHAT CN 1</td><td>kO CN 1</td><td>CN WHAT 1</td><td>O no. 1 1</td><td>ON</td>

<td>Hardness (Asker C) and</td><td>lT)</td><td> 43</td><td> 32</td><td> 33</td><td> 33</td><td> 28</td><td>rkO</td>

<td>Compression set after 60 days (percentage)²</td><td>WHAT kD</td><td>Γ ·</td><td> 15, 3</td><td>CN</td><td> 17,4</td><td>CN LO</td><td>&lt; of</td>

<td>Average compressive strength after 60 days (kilopascal)¹</td><td>0 ** cn</td><td> 93</td><td> 52</td><td> 56 1</td><td> 46</td><td> 63</td><td>C of</td>

<td>Average cell size (millimeter)</td><td>0.57 and</td><td> 0,46</td><td> 0, 51</td><td>WHAT O</td><td> 0,62</td><td> 1,23</td><td> 0,26</td>

<td>Example</td><td>10</td><td></td><td>r-</td><td> 00</td><td>cn</td><td>-X CN</td><td>-TO 00</td>

m ΓΙΟ cn

S řH ω

C

Ό

Fart

Ό

CO + -&gt;

cn

------ i --------- 1

Ό OJ

O Γ (d ID m

O ID

C

O z&gt; U HH&gt; φ Q e

- Ό -H • HUO

<td></td><td>C</td><td>rO</td><td>Ή</td>

<td>Ό</td><td>φ</td><td>Ό</td><td>N</td>

<td>O</td><td>&gt; u</td><td>C</td><td>O</td>

<td>l ------ f</td><td> (0</td><td>Φ</td><td>d</td>

<td></td><td> &lt;—1</td><td> +-&gt;</td><td>OT</td>

<td>Ή</td><td>-P</td><td>cn</td><td>H</td>

<td>&gt; U</td><td>cn</td><td></td><td>Ό</td>

<td>d</td><td></td><td>Φ 1—1</td><td>d!</td>

<td>Ή</td><td>C</td><td>Ό</td><td></td>

<td>O</td><td>+ J</td><td> 0</td><td>Ή</td>

<td>O</td><td>C</td><td>! d</td><td>C</td>

<td> &gt;</td><td>Φ</td><td></td><td>φ</td>

<td>Ό</td><td>O</td><td>O</td><td>C</td>

<td>C</td><td>O</td><td>C</td><td></td>

<td> &gt;</td><td>Cl</td><td>Φ</td><td>m</td>

<td>O</td><td>(d</td><td></td><td>Φ</td>

<td>AT</td><td>LO</td><td>&gt; Φ</td><td>Ό</td>

<td>ω</td><td> 04</td><td>WITH</td><td>O</td>

&lt;

Ý r - CN Z

Example 10

To produce foam elongate blanks, a foaming method was employed in these examples, including the use of a single screw extruder, mixer, coolers and slots. Isobutane or isobutane / carbon dioxide (CO2) mixture was used as a blowing agent for foaming a mixture of polystyrene and ethylene styrene interpolymers (ESI) in this case. was about 50 or less. The properties of the foams obtained are summarized in Table 5.

· Φ · · · · · · · · · · • co&gt; &lt;υ £ co ο Xi φ

C ε

φ c

X ν

X

Ο ω

-Η

X ο c&gt; φ&gt; φ α

Φ c

Ι-Η ω Ν ω CU * r1

V)&gt; φ £ co

Ή ____

Ν7!

'Π5Ο

XΟ φ

C £&gt; φ-Η χ&gt; υ

Ή • Η &lt;—I

XX &lt;ηα ο

C £ χω coχ

ΦΉ&gt; —IX&gt; Ο

X

Φ χ ι — I

X

Φ

<td>Width (millimeter)</td><td> 93</td><td> 93</td>

<td>Thickness (millimeter)</td><td> 27</td><td> 20</td>

<td>Foam density after 7 days (kilogram / m³)</td><td> | 29, 17</td><td> 28,05</td>

<td>Foaming temperature (° C)</td><td> 115 1</td><td> 120</td>

<td>Blowing agent</td><td>5 X - «XOX X ° ^and-χ &lt;0</td><td>isobutane (10 phr)</td>

<td>Composition of the mixture (wt%)</td><td>kO H ω ω o \ o O 10 (N ω cu o lD</td><td>ΓΗ ω ω ο \ θ Ο LO CM CO IX o \ o O LT)</td>

<td>Example</td><td> 10</td><td> 11</td>

<td>Hardness (Asker C)</td><td> 40</td><td> 50</td>

<td>Total compressive strength after 60 days (kilopascal)²</td><td> 354</td><td> 973</td>

<td>Average cell size (millimeter)</td><td> 0,44</td><td> 0,52</td>

<td>Percentage of open cells¹</td><td> 81,1</td><td> 22,3 1</td>

<td>Example</td><td> 10 1</td><td> 11</td>

Measured according to ASTM D2856-94

Measured according to ASTM D1621-94 standard 9 · 9 · 9 · 9 · 9 · 9 · 9 · 9 · 9 ····· · · · · · ···

PATENT CLAIMS