EP1448639A2 - Method for continuous anionic polymerization of impact-resistant polystyrene - Google Patents
Method for continuous anionic polymerization of impact-resistant polystyreneInfo
- Publication number
- EP1448639A2 EP1448639A2 EP02779496A EP02779496A EP1448639A2 EP 1448639 A2 EP1448639 A2 EP 1448639A2 EP 02779496 A EP02779496 A EP 02779496A EP 02779496 A EP02779496 A EP 02779496A EP 1448639 A2 EP1448639 A2 EP 1448639A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- rubber
- styrene
- weight
- polymerization
- reactor cascade
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F12/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an aromatic carbocyclic ring
- C08F12/02—Monomers containing only one unsaturated aliphatic radical
- C08F12/04—Monomers containing only one unsaturated aliphatic radical containing one ring
- C08F12/06—Hydrocarbons
- C08F12/08—Styrene
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F287/00—Macromolecular compounds obtained by polymerising monomers on to block polymers
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F279/00—Macromolecular compounds obtained by polymerising monomers on to polymers of monomers having two or more carbon-to-carbon double bonds as defined in group C08F36/00
- C08F279/02—Macromolecular compounds obtained by polymerising monomers on to polymers of monomers having two or more carbon-to-carbon double bonds as defined in group C08F36/00 on to polymers of conjugated dienes
Definitions
- the invention relates to a process for the preparation of impact-resistant molding compositions by anionic polymerization of vinyl-aromatic monomers in the presence of a rubber in a continuously flowed reactor cascade comprising at least two reactors.
- EP-A 595121 describes the transfer to a continuous process in a boiler-boiler-tower-tower cascade, as was known for the radical polymerization of impact-resistant polystyrene.
- the monomer stream is here to split a 'zel- nen reactors.
- larger tower reactors it has been shown that the metered-in monomeric styrene cannot be homogenized quickly enough with the highly viscous polymer solution and therefore uncontrolled reactions can occur.
- WO 96/18666 describes a process in which impact-modified polystyrene is polymerized continuously in a single reactor above the phase inversion point.
- a process for the preparation of impact-resistant molding compositions by anionic polymerization of vinyl aromatic monomers in the presence of a rubber in a continuously flowed reactor cascade from at least two reactors, the vinyl aromatic monomers in partial streams to the reactors of the reactor cascade and an anionic initiator and a rubber to at least the first reactor are supplied, found, the reactor cascade consisting of back-mixing reactors.
- Continuously flowed stirred tanks are suitable as reactors. They ensure a sufficiently rapid mixing of the feeds with the polymerization mixture and an effective removal of the heat of reaction by evaporative cooling. The vapors formed in this way usually run back into the reactor. Some of the solvent-containing condensate can also be removed using the heat of reaction.
- polymerization is preferably carried out in a reactor cascade consisting of two stirred tanks connected in series, the solids content in the first stirred tank being above the phase inversion point.
- the solids content in the first stirred tank is preferably at least twice the weight fraction of the rubber therein and in the second stirred tank in the range of 50-85% by weight.
- the solids content in the first stirred kettle is particularly preferably 5 to 30% by weight above twice the value by weight of the rubber, with a rubber content of 5 to 15% by weight, that is to say in the range from 15 to 60% by weight.
- the solids content in the first stirred tank is below the phase inversion point, in the second stirred tank at least twice the weight fraction of the rubber and in the third stirred tank in the range from 50 to 85% by weight.
- Isomerism in the individual reactors of the reactor cascade is preferably polymerized at temperatures in the range from 50 to 170 ° C., particularly preferably in the range from 70 to 130 ° C. Here will preferably set a higher temperature within the reactor cascade from reactor to reactor.
- the polymerization can be carried out via a degasser at temperatures in the range from 200 to 280 ° C.
- Styrene and styrene derivatives in particular styrene and .alpha.-methylstyrene or mixtures of different styrene derivatives, can be used as vinyl aromatic monomers.
- the vinyl aromatic monomers are fed to the reactors of the reactor cascade in partial flows.
- the monomer conversion in each reactor should be above 95%, preferably above 99%. Since the monomer conversion determines the heat of reaction released, the maximum possible monomer feed to the individual reactors results from their boiling cooling capacities.
- the ratio of the individual sub-streams to one another depends on the desired solids content which one would like to achieve in the individual reactors of the reactor cascade.
- the vinylaromatic partial monomer streams are generally divided in the ratio R2 / R1 of 0.1-15, preferably 1-7, in particular 3-4.
- the distribution is generally in the ratio R3 / R1 and R2 / R1 of 0.1-15, preferably 2-10, in particular 2-3.
- the process according to the invention can be carried out in inert solvents, for example aliphatic, cycloaliphatic or aromatic hydrocarbons or mixtures thereof.
- Preferred hydrocarbons are those with 3 to 12 carbon atoms.
- Preferred solvents are toluene, cyclohexane or methylcyclohexane.
- the usual mono-, bi- or multifunctional alkali metal alkyls, aryls or aralkyls can be used as anionic polymerization initiators.
- Organolithium compounds such as ethyl, propyl, isopropyl, N-butyl, sec-butyl-, tert-butyl-, phenyl-, diphenylhexyl-, hexamethyl-, butadienyl-, isoprenyl or polystyryllithium as well as 1, 4-dilithium-butane, 1, 4-dilithium-2-butene or 1, 4- Dilithium benzene used.
- the required amount depends on the desired molecular weight. As a rule, it is in the range from 0.001 to 5 mol%, based on the total monomer.
- sub-stoichiometric amounts may also be sufficient in view of a particular molecular weight to be achieved due to transfer reactions to the solvent.
- the savings can be up to 50%, based on the stoichiometric amount.
- the anionic initiator is fed to at least the first reactor. However, it can also be divided into partial streams in any ratio among the various reactors in the reactor cascade. This enables bimodal or multimodal molecular weight distributions of the vinylaromatic hard matrix to be achieved.
- Lewis bases such as tetrahydrofuran, tertiary amines or soluble potassium salts, can be added to accelerate the reaction.
- the rubber is also fed to at least the first reactor.
- the rubber used should be compatible with the vinylaromatic matrix.
- Suitable rubbers are styrene block copolymers with at least one block of dienes, such as butadiene, methylbutadiene or isoprene, and copolymer blocks of diene and styrene with a statistical structure.
- Styrene-butadiene block copolymers or a mixture of a styrene-butadiene block copolymer with a polybutadiene are preferably used as the rubber.
- the rubber preferably has a solution viscosity of 120 ml / g or less, preferably less than 40 85 ml / g, measured as a 5% strength by weight solution in styrene.
- the diene content of the rubbers is generally in the range from 10 to 90% by weight, preferably in the range from 65 to 75% by weight.
- the rubber is preferably used in an amount which leads to a diene content in the range from 6 to 12% by weight, based on the impact-resistant molding composition.
- a styrene-butadiene two-block or styrene-butadiene-styrene three-block copolymer with at least one styrene block with a number-average molecular weight M n of at least 35,000, preferably at least 70,000 g / mol is particularly preferably used as the rubber.
- the rubbers used can be produced batchwise using the known methods of sequential anionic polymerization.
- the solvent which is also used for the polymerization of the vinylaromatic hard matrix is preferably used as the solvent.
- the rubber is preferred without isolation, if necessary after chain termination with a proton-active substance or Lewis acid, such as water, alcohols, aliphatic or aromatic carboxylic acids and inorganic acids or carbon dioxide, or by reaction with bi- or polyfunctional coupling agents, such as polyfunctional aldehydes, ketones, Esters, anhydrides or epoxides are fed directly to the reactor cascade.
- a proton-active substance or Lewis acid such as water, alcohols, aliphatic or aromatic carboxylic acids and inorganic acids or carbon dioxide
- bi- or polyfunctional coupling agents such as polyfunctional aldehydes, ketones, Esters, anhydrides or epoxides are fed directly to the reactor cascade.
- Styrene / butadiene / styrene / three-block copolymers were obtained by sequential anionic polymerization in toluene and initiation with sec. -Butyllithium (s-BuLi) manufactured. After the polymerization, the mixture was terminated with isopropanol. The rubber solution was then diluted with styrene.
- the solution contained 130 kg of an SBS three-block copolymer with the block lengths 11,000 / 145,000 / 40,000 g / mol in 390 kg of toluene and 130 kg of styrene.
- the solution contained 80 kg of an SBS three-block copolymer with the block lengths 12,000 / 168,000 / 57,000 g / mol in 240 kg of toluene and 116 kg of styrene. Production of impact-resistant polystyrenes
- a reactor cascade consisting of two stirred tanks Rl and R2 equipped with an anchor stirrer and having a volume of 1 or 1.9 liters was used.
- the styrenic rubber solution and the initiator were fed to the stirred tank R1 via separate feed lines ZI and Z2. Additional monomeric styrene was metered into the second stirred tank R2 via Z3.
- the throughput was about 800 g / h, based on the impact-resistant polystyrene.
Abstract
Description
Claims
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10152116A DE10152116A1 (en) | 2001-10-23 | 2001-10-23 | Process for the continuous anionic polymerization of impact-resistant polystyrene |
DE10152116 | 2001-10-23 | ||
PCT/EP2002/011668 WO2003035709A2 (en) | 2001-10-23 | 2002-10-18 | Method for continuous anionic polymerization of impact-resistant polystyrene |
Publications (1)
Publication Number | Publication Date |
---|---|
EP1448639A2 true EP1448639A2 (en) | 2004-08-25 |
Family
ID=7703320
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP02779496A Withdrawn EP1448639A2 (en) | 2001-10-23 | 2002-10-18 | Method for continuous anionic polymerization of impact-resistant polystyrene |
Country Status (9)
Country | Link |
---|---|
US (1) | US6951901B2 (en) |
EP (1) | EP1448639A2 (en) |
JP (1) | JP2005506415A (en) |
KR (1) | KR20040047947A (en) |
CN (1) | CN1575306A (en) |
AU (1) | AU2002342837A1 (en) |
DE (1) | DE10152116A1 (en) |
MX (1) | MXPA04003318A (en) |
WO (1) | WO2003035709A2 (en) |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE10241850A1 (en) * | 2002-09-09 | 2004-03-18 | Basf Ag | Anionically polymerized tough impact polystyrene, useful for preparation of shaped bodies, films, fibers or foams, comprises initiator composition and has low residual monomers and oligomer content and good injection molding properties |
KR101489954B1 (en) | 2011-12-23 | 2015-02-04 | 제일모직주식회사 | Continuous process for preparing thermoplastic resin from conjugated diene and thermoplastic resin prepared therefrom |
CN104558429B (en) * | 2013-10-18 | 2017-11-07 | 中国石油化工股份有限公司 | Polyphenylacetylene combination production method and thus obtained polyphenylacetylene combination |
CN113698558A (en) * | 2020-05-20 | 2021-11-26 | 中国石油化工股份有限公司 | Butylbenzene copolymer and preparation method and application thereof |
Family Cites Families (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4153647A (en) * | 1977-06-15 | 1979-05-08 | Glukhovskoi Vladimir S | Process for producing-impact polystyrene |
DE4235978A1 (en) * | 1992-10-24 | 1994-04-28 | Basf Ag | Thermoplastic molding compound |
DE4235977A1 (en) * | 1992-10-24 | 1994-04-28 | Basf Ag | Process for the production of impact-resistant polystyrene |
US5990236A (en) * | 1993-10-18 | 1999-11-23 | Basf Aktiengesellschaft | Preparation of impact-resistant polystyrene |
DE59702613D1 (en) * | 1996-08-19 | 2000-12-14 | Basf Ag | METHOD FOR PRODUCING DIEN POLYMERISATE SOLUTIONS IN VINYLAROMATIC MONOMERS |
WO1998007765A2 (en) * | 1996-08-19 | 1998-02-26 | Basf Aktiengesellschaft | Anionic polymerisation process |
DE19701865A1 (en) * | 1997-01-21 | 1998-07-23 | Basf Ag | Continuous process for the production of thermoplastic molding compounds |
BR9907648A (en) * | 1998-02-07 | 2002-04-30 | Basf Ag | Process for preparing impact-modified thermoplastic molding compositions |
DE19804912A1 (en) * | 1998-02-07 | 1999-08-12 | Basf Ag | Continuous process for the production of thermoplastic molding compounds |
CN1092216C (en) * | 1998-11-26 | 2002-10-09 | 中国石油化工集团公司 | nm-class polyolefine-clay composition |
-
2001
- 2001-10-23 DE DE10152116A patent/DE10152116A1/en not_active Withdrawn
-
2002
- 2002-10-18 KR KR10-2004-7005961A patent/KR20040047947A/en not_active Application Discontinuation
- 2002-10-18 MX MXPA04003318A patent/MXPA04003318A/en unknown
- 2002-10-18 EP EP02779496A patent/EP1448639A2/en not_active Withdrawn
- 2002-10-18 CN CNA028209133A patent/CN1575306A/en active Pending
- 2002-10-18 AU AU2002342837A patent/AU2002342837A1/en not_active Abandoned
- 2002-10-18 JP JP2003538222A patent/JP2005506415A/en not_active Withdrawn
- 2002-10-18 US US10/492,620 patent/US6951901B2/en not_active Expired - Fee Related
- 2002-10-18 WO PCT/EP2002/011668 patent/WO2003035709A2/en not_active Application Discontinuation
Non-Patent Citations (1)
Title |
---|
See references of WO03035709A2 * |
Also Published As
Publication number | Publication date |
---|---|
US6951901B2 (en) | 2005-10-04 |
KR20040047947A (en) | 2004-06-05 |
WO2003035709A3 (en) | 2003-09-18 |
DE10152116A1 (en) | 2003-04-30 |
MXPA04003318A (en) | 2004-07-23 |
US20040266946A1 (en) | 2004-12-30 |
JP2005506415A (en) | 2005-03-03 |
CN1575306A (en) | 2005-02-02 |
WO2003035709A2 (en) | 2003-05-01 |
AU2002342837A1 (en) | 2003-05-06 |
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Legal Events
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AX | Request for extension of the european patent |
Extension state: AL LT LV MK RO SI |
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RIN1 | Information on inventor provided before grant (corrected) |
Inventor name: SCHADE, CHRISTIAN Inventor name: DESBOIS, PHILIPPE Inventor name: DEMETER, JUERGEN Inventor name: GAUSEPOHL, HERMANN |
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STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE APPLICATION HAS BEEN WITHDRAWN |
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18W | Application withdrawn |
Effective date: 20060104 |