WO2001004169A1 - Verfahren zur herstellung von schlagzäh modifizierten polymeren in gegenwart von lösungsmitteln - Google Patents
Verfahren zur herstellung von schlagzäh modifizierten polymeren in gegenwart von lösungsmitteln Download PDFInfo
- Publication number
- WO2001004169A1 WO2001004169A1 PCT/EP2000/005894 EP0005894W WO0104169A1 WO 2001004169 A1 WO2001004169 A1 WO 2001004169A1 EP 0005894 W EP0005894 W EP 0005894W WO 0104169 A1 WO0104169 A1 WO 0104169A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- weight
- rubber
- polymerization
- monomers
- solvent
- Prior art date
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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
- C08F285/00—Macromolecular compounds obtained by polymerising monomers on to preformed graft 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
- C08F279/04—Vinyl aromatic monomers and nitriles as the only monomers
Definitions
- the invention relates to a method for producing impact modified
- ABS polymers or “ABS molding compounds” (ABS from “acrylonitrile-butadiene-styrene”).
- ABS bulk polymerization or ABS solution polymerization is characterized by ecological and economic advantages and by products with a low intrinsic color, with a lower content of products that can sweat out during processing, with favorable processing behavior, with high rubber effectiveness and with high heat resistance ,
- a problem of bulk or solution polymerization of monoalkenyl compounds and ethylenically saturated nitriles in the presence of soluble rubbers, which research and technology have long been concerned with, is the adjustment of the molar mass distribution of the resin phase and the shape and size distribution of the grafted rubber particles distributed in the resin phase.
- the processing behavior, surface gloss, hardness / rubber / toughness ratios depend on this.
- the solution polymerization in combination with a modern, economical polymer evaporation technology has the advantage over the bulk polymerization technique known from high impact polystyrene ("HI-PS") the advantages of reaction security and the simpler polymerization technique in stirred tank reactors.
- HI-PS high impact polystyrene
- the technical ABS solution processes are carried out continuously in reactor cascades consisting of continuously operated, mixed tank reactors (CSTR), pumped loop reactors, piston flow reactors (so-called tower reactors).
- CSTR mixed tank reactors
- pumped loop reactors piston flow reactors
- tower reactors piston flow reactors
- the solution polymerization is terminated if the conversions are incomplete.
- Solvents, monomers and residues on molecular weight regulators are separated using an evaporation technique and some of them are returned to the process.
- the solvent is used in the process right at the start of the polymerization.
- portions of recovered monomers, molecular weight regulators and solvents are recycled and inserted into the first reaction stage before the rubber phase reversal.
- the rubber phase reversal (phase inversion) is understood to mean the process that the rubber phase passes from the outer continuous phase into the inner divided phase and correspondingly the other phase from the inner divided phase into the outer continuous phase.
- the invention was based on the object of making available a generic method for producing impact-modified polymers, in which products with better processing behavior, with lower surface mattness or increased gloss and with improved rubber / toughness / hardness ratio.
- the solvent (or solvents) is preferably added after the rubber phase reversal.
- Recovered monomers and / or molecular weight regulators can also be introduced and recycled into the process together with the solvent.
- the advantage of adding the solvent for the solution polymerization after a conversion of 6 to 30% by weight is particularly evident in the production of ABS through the continuous process in at least 3 reactors connected in series, the monoalkenyl aromatic copolymer in the ABS containing more than 25% by weight of built-in ethylenically unsaturated nitrile monomers.
- the process according to the invention for the production of impact-modified ABS molding materials by non-aqueous solution polymerization can in particular be carried out in several stages in the following steps:
- Solvents to be used are polymerization-inert organic compounds with boiling points of about 60 to 160 ° C., which alone or in the presence of the ethylenically unsaturated nitrile monomer keep the resin phase in solution.
- organic compounds are e.g.
- the polymerization can be carried out batchwise.
- the polymerization can also be carried out batchwise in the feed.
- the polymerization is preferably carried out continuously (continuously) in at least 3 reactors connected in series, the first reactor for the multi-stage process preferably being a continuously flowed and well-mixed tank reactor (CSTR) or pumped-around loop reactor and in which the operating state with stationary monomer conversions from 6 to 30 wt .-% can be kept.
- CSTR continuously flowed and well-mixed tank reactor
- the rubber dissolved in monomers forms a coherent phase when it enters the first solvent-free reaction stage.
- the solvent or solvent mixture and possibly further monomer components and / or recirculated monomers and molecular weight regulators are metered into the mixed second reaction stage, preferably after the rubber phase reversal (in the case of continuous operation: CSTR or pumped reactor loop).
- Good mixing with intensely mixing stirring elements and / or with is essential Inline mixer installed in a loop with static mixing elements or with movable and rotating mixing elements as they are state of the art.
- the so-called “fmishing” reactor in which monomer conversions up to the desired final conversion, which can be from 50 to 98%, are achieved, can be both mixed tank reactors, pumped-around reactor loops and reactors with piston flow characteristics , so-called “plug flow” or “tower reactors".
- plug flow so-called "tower reactors”.
- the state of reactor technology is described by Gerrens in Chem. Ing. Techn. 1980, 52, 477-488, (1980).
- Solvents, residual monomers and other volatile constituents can be achieved after reaching monomer conversions of 50 to a maximum of 98% according to conventional techniques, e.g. on heat exchange evaporators, flash evaporators, strand evaporators, thin-film or thin-layer evaporators, screw evaporators and are removed, if appropriate after conversions of 6 to 30% have taken place, preferably after the originally connected rubber phase has passed into the divided phase, into the second and / or recycled one of the following reaction stages.
- Usual molecular weight regulators such as mercaptans, allyl compounds, dimeric ⁇ -methylstyrenes, terpinols are added in amounts of 0.01 to about 1.5% by weight, based on the monomers a) and b), in the course of the manufacturing process.
- the polymerization is triggered by free radicals.
- Graft-active radical initiators which disintegrate at low temperatures, in particular peroxides such as peroxycarbonates, peroxydicarbonates, diacyl peroxides, perketals, peresters, dialkyl peroxides and / or azo compounds or mixtures thereof, are preferably used. Examples include Tert.-butyl perpivalate, peroctoate, perbenzoate, perneodecanoate. These initiators are used in amounts of 0.01 to 1 wt .-%, based on the
- Monomers a) and b) used can also be carried out in whole or in part by thermally initiated free-radical polymerization.
- thermal initiation as it is state of the art; see. K. Kirchner and K. Riedel, Angew. Makromol. Chem. 111, 1-16 (1983):
- thermo initiation can be used in particular in the third and approximately further reaction stages
- the polymerization is carried out at temperatures of about 60 to 160 ° C. It has proven to be advantageous to carry out the first solvent-free reaction stage (conversion 6 to 30%) at temperatures below 120 ° C., preferably at 70 to 90 ° C.
- the polymerization times until the desired final conversion are 2 to 12 hours, preferably 3 to 6 hours.
- customary additives such as dyes, antioxidants, lubricants such as e.g. Hydrocarbon oils, stabilizers, etc. are added.
- Soluble, gel-free butadiene polymers are polybutadienes and styrene-butadiene
- Aromatic monoalkenyl compounds are preferably styrene, ⁇ -methylstyrene, nucleus-substituted alkylstyrenes, nucleus-substituted chlorostyrenes.
- Ethylenically unsaturated nitriles are preferably acrylonitrile, methacrylonitrile.
- Copolymerizing monomers are e.g. Acrylic esters such as methyl (meth) acrylate, ethyl (meth) acrylate, tert-butyl (meth) acrylate, esters of fumaric acid, itaconic acid, maleine derivatives such as maleic anhydride, maleic acid esters, N-substituted maleimides such as advantageously N-cyclohexyl or N- Phenyl-maleimide, nucleus-substituted N-alkylphenyl-maleimides, further acrylic acid, methacrylic acid, (meth) acrylamides, fumaric acid, itaconic acid or their amides.
- Acrylic esters such as methyl (meth) acrylate, ethyl (meth) acrylate, tert-butyl (meth) acrylate, esters of fumaric acid, itaconic acid, maleine derivatives such as maleic anhydride, maleic acid est
- the invention also relates to the thermoplastically processable molding compositions prepared by the process according to the invention with a rubber content of 6 to 25% by weight and a preferred content of ethylenically unsaturated nitrile monomers in the monoalkenyl aromatic copolymer of more than 25% by weight.
- the products according to the invention are notable for a high rubber graft layer with a high internal graft content of the rubber particles, given by the quotient of the gel content minus the rubber content to the rubber content:
- the gel content means the proportion of crosslinked rubber component which is insoluble in tetrahydrofuran and is loaded with graft branches.
- the quotient of the products according to the invention is 0.4 to 2.0.
- the rubber particle size and distribution are measured by measuring the turbidity of a sample dispersion in propylene carbonate in a "Particle Size Distribution Analyzer CAPA 700", from HORLBA Europe GmbH, 61449 Steinbach.
- ABS resins are particularly narrow compared to processes in which the solvent had been added at the beginning of the solution polymerization before the rubber phase reversal.
- the advantage of the multi-stage process according to the invention is that almost no rubber particles below 100 nm and none above 1 ⁇ m are produced. It is known to the person skilled in the art that such distributions have a positive effect on the surface gloss of molding compositions.
- phase structure of the ABS systems is determined by measuring the complex shear modulus depending on the temperature in the range between -150 ° C and 200 ° C with the Dynamic Analyzer RDA II from Rheometrics.
- the mechanically effective soft phase fraction in the ABS can be determined from the area under the rubber-glass transition peak of the loss factor tan ⁇ or from the module level at RT. If the rubber content is known, the styrene copolymer content (internal graft) enclosed in the rubber particles can be determined from this.
- the rubber particles Compared to the processes in which solvents are added at the start of the reaction, the rubber particles have an increased proportion of internal graft enclosed in the particles.
- the pure rubber component is increased by a styrene copolymer component enclosed in the particles to a soft phase component increased by a factor> 1.5, preferably> 1.7.
- the person skilled in the art is furthermore aware that the increase in the soft phase fraction due to enclosed styrene copolymer regions in the rubber particles with unchanged rubber fraction and with suitable TGV leads to an increase in the work load in the ABS under deformation stress (eg notched impact strength), ie to an increase in the rubber efficiency.
- FIG. 1 shows the rubber particle size distribution (TGV) according to Example 1 before evaporation
- Figure 2 shows the TGV prior to evaporation.
- FIG. 3 shows the TGV in the end product according to.
- FIG. 5 shows the TGV in the end product according to Example 7
- FIG. 6 shows the TGV in the end product according to.
- a cascade consisting of 2 continuously operated mixed reactors connected in series and then a batch-operated mixed reactor.
- the fill level in the first stirred tank is 0.66 kg, in the second tank 1.14 kg and in the batch operated reactor 1.52 kg.
- the solution is delivered at a rate of 0.63 kg / h in the first, with an anchor stirrer at 80 rpm. stirred reactor added.
- the reaction temperature is kept at 75 ° C under atmospheric pressure.
- 0.50 g of tert-butyl perpivalate are metered in as a 25% solution in a mixture of hydrocarbons and methyl ethyl ketone per hour.
- the fill level is kept at 0.66 kg.
- the solids content is 31% by weight, corresponding to a conversion of 23% by weight, based on styrene and acrylonitrile.
- the operating state is after the phase reversal.
- the reaction material from the first reactor is continuously fed into the second, using a wire basket stirrer at 200 rpm. stirred reactor, which is kept at 75 ° C and atmospheric pressure.
- a mixture of 99.4 parts by weight of acrylonitrile, 268.6 parts by weight of styrene, 80 parts by weight of methyl ethyl ketone and 0.92 parts by weight of dimeric alphamethylstyrene is added to the reactor at a metering rate of 0.45 kg / h, and 0.33 is separated g of tert-butyl perpivalate is metered in as a 1% strength solution in methyl ethyl ketone.
- the fill level is kept at 1.14 kg.
- the solids content is 27% by weight, corresponding to a conversion of 25% by weight, based on styrene and acrylonitrile.
- the entry and exit flows are switched off.
- the temperature is raised to 78 ° C. and a mixture of 270 g of methyl ethyl ketone and 4.6 g of dimeric alphamethylstyrene is fed in within 20 minutes.
- 2.2 g of tert-butyl perpivalate in 60 g of methyl ethyl ketone are metered in separately over the course of 2 hours.
- the mixture is then polymerized for 4 hours at 78 ° C. to a final conversion of 73.6% by weight, based on styrene and acrylonitrile.
- reaction mixture is evaporated on a 32 mm laboratory twin-shaft co-rotating screw.
- ABS is obtained with 10.8% by weight of rubber (infrared spectroscopic determination); 27% by weight acrylonitrile in poly-SAN (infrared spectroscopic
- Distribution analyzer CAPA-700 is shown in FIG. 1 (abscissa: diameter d in ⁇ m; ordinate: relative weight fraction).
- Example No. 4 Comparative example to Examples Nos. 1 to 3, not according to the inventive method
- the same tank cascade is used as in example 1.
- the fill level is 1.03 kg
- in the second tank 1.44 kg
- the solution is delivered at a rate of 1.0 kg / h in the first, with an anchor stirrer at 80 rpm. stirred reactor added.
- the reaction temperature is kept at 75 ° C under atmospheric pressure.
- 0.98 g of tert-butyl perpivalate are metered in as a 3% solution in methyl ethyl ketone per hour.
- the fill level is kept at 1.03 kg.
- the solids content is 21% by weight, corresponding to a conversion of 19% by weight, based on styrene and acrylonitrile.
- the operating state is after the phase reversal.
- the reaction material from the first reactor is continuously fed into the second, using a wire basket stirrer at 200 rpm. stirred reactor, which is kept at 75 ° C and atmospheric pressure.
- the entry and exit flows are switched off.
- the temperature is raised to 78 ° C. and 3.32 g of tert-butyl perpivalate in 60 g of methyl ethyl ketone are metered in over the course of 2 hours.
- the mixture is then polymerized for 4 hours at 78 ° C. to a final conversion of 61.5% by weight, based on styrene and acrylonitrile.
- a mixture of 10 g of methylethylkekeoonoon, 11.0 g of LRGANOX 1076® (Ciba Geigy, Switzerland) and 7.24 g of paraffin oil is stirred into the reactor contents.
- reaction mixture is evaporated on a 32 mm laboratory twin-shaft co-rotating screw.
- test under CO2 is carried out in a continuous laboratory system consisting of two continuously operated, mixed reactors connected in series, followed by a stirred 4-liter reactor with a piston flow residence time characteristic.
- a starting mixture is prepared from 53.1 parts by weight of linear poly-cis-butadiene with 11% 1,2-vinyl content (BUNA CB HX 502C®, Bayer Elastomeres France) and 22.8 parts by weight of a linear polybutadiene-polystyrene block polymer 30% by weight polystyrene block fraction (BUNA BL 8497®, Bayer France), 646 parts by weight styrene, 227 parts by weight acrylonitrile, 0.15 parts by weight 2,6-di-tert-butyl-4- methylphenol and 2.18 parts by weight of dimeric alphamethylstyrene.
- BUNA CB HX 502C® linear polybutadiene-polystyrene block polymer 30% by weight polystyrene block fraction
- the laboratory system is continuously running at 1 kg / h of this starting mixture, which in one
- Heat exchanger is heated to 60 ° C, charged.
- the fill level is kept at 1 kg and 0.16 g of tert-butyl perpivalate is added continuously as a 25% solution in a mixture of hydrocarbons and methyl ethyl ketone.
- the first reactor is kept at 75 ° C under atmospheric pressure. After three average residence times, a conversion of 16% by weight, based on styrene and acrylonitrile, is established.
- the second reactor is kept at 75 ° C under atmospheric pressure.
- the product stream from the first reactor is fed continuously to the second reactor and at the same time 0.33 g / h of tert-butyl perpivalate as a 25% solution in a mixture of hydrocarbons and methyl ethyl ketone, and separately 0.87 g / h of dimeric alphamethylstyrene and 140 g / h of methyl ethyl ketone stirred in. After three average residence times, a conversion of 25% by weight, based on styrene and acrylonitrile, is established.
- the outlet of the piston flow reactor is continuously in an inline mixer 0.08 g / h 2,6-di-tert-butyl-4-methylphenol, 0.95 g / h IRGANOX 1076® (Ciba Geigy) and 6.9 g / h paraffin oil in 10 g / h methyl ethyl ketone added.
- the solution is evaporated on a 32 mm laboratory twin-shaft co-rotating screw.
- Vinyl double bonds (Buna HX 502, Bayer France) are used.
- the second laboratory reactor is stirred with an anchor stirrer, 100 rpm, in addition with a high-speed dispersing head of 20 mm in diameter and 800 rpm. touched.
- a conversion of 15% by weight is established in the first reactor and 27% by weight based on styrene and acrylonitrile in the second reactor.
- the final conversion after the third reaction stage is 62% by weight, based on styrene and acrylonitrile.
- ABS with 12.1% by weight of rubber is obtained; 26% by weight acrylonitrile in poly
- ABS with 9.9% by weight of rubber is obtained; 28% by weight acrylonitrile in poly
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- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Graft Or Block Polymers (AREA)
- Polymerization Catalysts (AREA)
- Polymerisation Methods In General (AREA)
Abstract
Description
Claims
Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA002378296A CA2378296A1 (en) | 1999-07-07 | 2000-06-26 | Method for producing polymers with a modified shock resistance in the presence of solvents |
BR0012170-3A BR0012170A (pt) | 1999-07-07 | 2000-06-26 | Processo para a preparação de polìmeros modificados tenazes ao choque na presença de solventes |
AU59786/00A AU5978600A (en) | 1999-07-07 | 2000-06-26 | Method for producing polymers with a modified shock resistance in the presence of solvents |
KR1020027000143A KR20020019948A (ko) | 1999-07-07 | 2000-06-26 | 용매 존재 하에서의 내충격성-강화 중합체 제조 방법 |
JP2001509778A JP2003504496A (ja) | 1999-07-07 | 2000-06-26 | 溶媒の存在下における耐衝撃性付与重合体の製造法 |
MXPA01013437A MXPA01013437A (es) | 1999-07-07 | 2000-06-26 | Procedimiento para la preparacion de polimeros modificados resistentes a los impactos en presencia de disolventes. |
EP00945821A EP1200497A1 (de) | 1999-07-07 | 2000-06-26 | Verfahren zur herstellung von schlagzäh modifizierten polymeren in gegenwart von lösungsmitteln |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19931254A DE19931254A1 (de) | 1999-07-07 | 1999-07-07 | Verfahren zur Herstellung von schlagzäh modifizierten Polymeren in Gegenwart von Lösungsmitteln |
DE19931254.0 | 1999-07-07 |
Publications (1)
Publication Number | Publication Date |
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WO2001004169A1 true WO2001004169A1 (de) | 2001-01-18 |
Family
ID=7913883
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2000/005894 WO2001004169A1 (de) | 1999-07-07 | 2000-06-26 | Verfahren zur herstellung von schlagzäh modifizierten polymeren in gegenwart von lösungsmitteln |
Country Status (11)
Country | Link |
---|---|
EP (1) | EP1200497A1 (de) |
JP (1) | JP2003504496A (de) |
KR (1) | KR20020019948A (de) |
CN (1) | CN1360604A (de) |
AR (1) | AR025194A1 (de) |
AU (1) | AU5978600A (de) |
BR (1) | BR0012170A (de) |
CA (1) | CA2378296A1 (de) |
DE (1) | DE19931254A1 (de) |
MX (1) | MXPA01013437A (de) |
WO (1) | WO2001004169A1 (de) |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH069732A (ja) * | 1992-06-24 | 1994-01-18 | Nippon Steel Chem Co Ltd | ゴム変成スチレン・アクリロニトリル系共重合樹脂の製造法 |
EP0632072A2 (de) * | 1993-06-29 | 1995-01-04 | MITSUI TOATSU CHEMICALS, Inc. | Kontinuierliches Verfahren zur Herstellung von gummimodifizierten Styrolharzen und dadurch erzeugte Produkte |
-
1999
- 1999-07-07 DE DE19931254A patent/DE19931254A1/de not_active Withdrawn
-
2000
- 2000-06-26 CA CA002378296A patent/CA2378296A1/en not_active Abandoned
- 2000-06-26 WO PCT/EP2000/005894 patent/WO2001004169A1/de not_active Application Discontinuation
- 2000-06-26 BR BR0012170-3A patent/BR0012170A/pt not_active Withdrawn
- 2000-06-26 CN CN00810027A patent/CN1360604A/zh active Pending
- 2000-06-26 EP EP00945821A patent/EP1200497A1/de not_active Withdrawn
- 2000-06-26 AU AU59786/00A patent/AU5978600A/en not_active Abandoned
- 2000-06-26 MX MXPA01013437A patent/MXPA01013437A/es not_active Application Discontinuation
- 2000-06-26 JP JP2001509778A patent/JP2003504496A/ja active Pending
- 2000-06-26 KR KR1020027000143A patent/KR20020019948A/ko not_active Application Discontinuation
- 2000-07-04 AR ARP000103409A patent/AR025194A1/es unknown
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH069732A (ja) * | 1992-06-24 | 1994-01-18 | Nippon Steel Chem Co Ltd | ゴム変成スチレン・アクリロニトリル系共重合樹脂の製造法 |
EP0632072A2 (de) * | 1993-06-29 | 1995-01-04 | MITSUI TOATSU CHEMICALS, Inc. | Kontinuierliches Verfahren zur Herstellung von gummimodifizierten Styrolharzen und dadurch erzeugte Produkte |
Non-Patent Citations (1)
Title |
---|
PATENT ABSTRACTS OF JAPAN vol. 018, no. 209 (C - 1190) 13 April 1994 (1994-04-13) * |
Also Published As
Publication number | Publication date |
---|---|
KR20020019948A (ko) | 2002-03-13 |
CN1360604A (zh) | 2002-07-24 |
MXPA01013437A (es) | 2002-07-30 |
JP2003504496A (ja) | 2003-02-04 |
BR0012170A (pt) | 2002-03-19 |
EP1200497A1 (de) | 2002-05-02 |
DE19931254A1 (de) | 2001-01-11 |
CA2378296A1 (en) | 2001-01-18 |
AU5978600A (en) | 2001-01-30 |
AR025194A1 (es) | 2002-11-13 |
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