WO2023136699A1 - 중합체의 제조방법 - Google Patents
중합체의 제조방법 Download PDFInfo
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- WO2023136699A1 WO2023136699A1 PCT/KR2023/000778 KR2023000778W WO2023136699A1 WO 2023136699 A1 WO2023136699 A1 WO 2023136699A1 KR 2023000778 W KR2023000778 W KR 2023000778W WO 2023136699 A1 WO2023136699 A1 WO 2023136699A1
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- Prior art keywords
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- 229920000642 polymer Polymers 0.000 title claims abstract description 117
- 238000002360 preparation method Methods 0.000 title abstract description 40
- 238000006116 polymerization reaction Methods 0.000 claims abstract description 389
- 238000006243 chemical reaction Methods 0.000 claims abstract description 269
- 239000000178 monomer Substances 0.000 claims abstract description 105
- 239000003999 initiator Substances 0.000 claims abstract description 89
- 229920002554 vinyl polymer Polymers 0.000 claims abstract description 62
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 claims abstract description 52
- 230000000977 initiatory effect Effects 0.000 claims abstract description 40
- 230000000379 polymerizing effect Effects 0.000 claims abstract description 4
- 238000004519 manufacturing process Methods 0.000 claims description 30
- 238000000034 method Methods 0.000 claims description 27
- -1 poly(t-butyl peroxy Chemical group 0.000 claims description 17
- HSLFISVKRDQEBY-UHFFFAOYSA-N 1,1-bis(tert-butylperoxy)cyclohexane Chemical compound CC(C)(C)OOC1(OOC(C)(C)C)CCCCC1 HSLFISVKRDQEBY-UHFFFAOYSA-N 0.000 claims description 14
- ZHKCHSNXUCRFSM-UHFFFAOYSA-N 4-[2-[4,4-bis(tert-butylperoxy)cyclohexyl]propan-2-yl]-1,1-bis(tert-butylperoxy)cyclohexane Chemical group C1CC(OOC(C)(C)C)(OOC(C)(C)C)CCC1C(C)(C)C1CCC(OOC(C)(C)C)(OOC(C)(C)C)CC1 ZHKCHSNXUCRFSM-UHFFFAOYSA-N 0.000 claims description 12
- 239000004721 Polyphenylene oxide Substances 0.000 claims description 10
- 229920000570 polyether Polymers 0.000 claims description 10
- 238000010557 suspension polymerization reaction Methods 0.000 claims description 6
- IMYCVFRTNVMHAD-UHFFFAOYSA-N 1,1-bis(2-methylbutan-2-ylperoxy)cyclohexane Chemical compound CCC(C)(C)OOC1(OOC(C)(C)CC)CCCCC1 IMYCVFRTNVMHAD-UHFFFAOYSA-N 0.000 claims description 5
- NALFRYPTRXKZPN-UHFFFAOYSA-N 1,1-bis(tert-butylperoxy)-3,3,5-trimethylcyclohexane Chemical compound CC1CC(C)(C)CC(OOC(C)(C)C)(OOC(C)(C)C)C1 NALFRYPTRXKZPN-UHFFFAOYSA-N 0.000 claims description 5
- 239000000243 solution Substances 0.000 description 142
- 239000002002 slurry Substances 0.000 description 47
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 46
- XYLMUPLGERFSHI-UHFFFAOYSA-N alpha-Methylstyrene Chemical compound CC(=C)C1=CC=CC=C1 XYLMUPLGERFSHI-UHFFFAOYSA-N 0.000 description 45
- 230000000052 comparative effect Effects 0.000 description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 40
- 239000011324 bead Substances 0.000 description 24
- 238000005406 washing Methods 0.000 description 24
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 23
- 230000018044 dehydration Effects 0.000 description 23
- 238000006297 dehydration reaction Methods 0.000 description 23
- 238000001035 drying Methods 0.000 description 23
- 235000019253 formic acid Nutrition 0.000 description 23
- 239000001506 calcium phosphate Substances 0.000 description 18
- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 0.000 description 18
- 238000009826 distribution Methods 0.000 description 16
- 238000002156 mixing Methods 0.000 description 16
- 239000000126 substance Substances 0.000 description 16
- 229910000391 tricalcium phosphate Inorganic materials 0.000 description 16
- 235000019731 tricalcium phosphate Nutrition 0.000 description 16
- 229940078499 tricalcium phosphate Drugs 0.000 description 16
- 239000000375 suspending agent Substances 0.000 description 15
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 14
- 239000000725 suspension Substances 0.000 description 13
- QEQBMZQFDDDTPN-UHFFFAOYSA-N (2-methylpropan-2-yl)oxy benzenecarboperoxoate Chemical compound CC(C)(C)OOOC(=O)C1=CC=CC=C1 QEQBMZQFDDDTPN-UHFFFAOYSA-N 0.000 description 7
- 239000001294 propane Substances 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- 239000004342 Benzoyl peroxide Substances 0.000 description 5
- 235000019400 benzoyl peroxide Nutrition 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 5
- XMNIXWIUMCBBBL-UHFFFAOYSA-N 2-(2-phenylpropan-2-ylperoxy)propan-2-ylbenzene Chemical compound C=1C=CC=CC=1C(C)(C)OOC(C)(C)C1=CC=CC=C1 XMNIXWIUMCBBBL-UHFFFAOYSA-N 0.000 description 4
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 4
- 238000012662 bulk polymerization Methods 0.000 description 4
- OMPJBNCRMGITSC-UHFFFAOYSA-N Benzoylperoxide Chemical compound C=1C=CC=CC=1C(=O)OOC(=O)C1=CC=CC=C1 OMPJBNCRMGITSC-UHFFFAOYSA-N 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- JLBJTVDPSNHSKJ-UHFFFAOYSA-N 4-Methylstyrene Chemical compound CC1=CC=C(C=C)C=C1 JLBJTVDPSNHSKJ-UHFFFAOYSA-N 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- 239000004372 Polyvinyl alcohol Substances 0.000 description 2
- 239000003125 aqueous solvent Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 229910000389 calcium phosphate Inorganic materials 0.000 description 2
- 235000011010 calcium phosphates Nutrition 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 239000000314 lubricant Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 229920002451 polyvinyl alcohol Polymers 0.000 description 2
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 2
- HCXVPNKIBYLBIT-UHFFFAOYSA-N (2-methylpropan-2-yl)oxy 3,5,5-trimethylhexaneperoxoate Chemical compound CC(C)(C)CC(C)CC(=O)OOOC(C)(C)C HCXVPNKIBYLBIT-UHFFFAOYSA-N 0.000 description 1
- KDGNCLDCOVTOCS-UHFFFAOYSA-N (2-methylpropan-2-yl)oxy propan-2-yl carbonate Chemical compound CC(C)OC(=O)OOC(C)(C)C KDGNCLDCOVTOCS-UHFFFAOYSA-N 0.000 description 1
- RQHGZNBWBKINOY-PLNGDYQASA-N (z)-4-tert-butylperoxy-4-oxobut-2-enoic acid Chemical compound CC(C)(C)OOC(=O)\C=C/C(O)=O RQHGZNBWBKINOY-PLNGDYQASA-N 0.000 description 1
- CCNDOQHYOIISTA-UHFFFAOYSA-N 1,2-bis(2-tert-butylperoxypropan-2-yl)benzene Chemical compound CC(C)(C)OOC(C)(C)C1=CC=CC=C1C(C)(C)OOC(C)(C)C CCNDOQHYOIISTA-UHFFFAOYSA-N 0.000 description 1
- OEVVKKAVYQFQNV-UHFFFAOYSA-N 1-ethenyl-2,4-dimethylbenzene Chemical compound CC1=CC=C(C=C)C(C)=C1 OEVVKKAVYQFQNV-UHFFFAOYSA-N 0.000 description 1
- HQOVXPHOJANJBR-UHFFFAOYSA-N 2,2-bis(tert-butylperoxy)butane Chemical compound CC(C)(C)OOC(C)(CC)OOC(C)(C)C HQOVXPHOJANJBR-UHFFFAOYSA-N 0.000 description 1
- DMWVYCCGCQPJEA-UHFFFAOYSA-N 2,5-bis(tert-butylperoxy)-2,5-dimethylhexane Chemical group CC(C)(C)OOC(C)(C)CCC(C)(C)OOC(C)(C)C DMWVYCCGCQPJEA-UHFFFAOYSA-N 0.000 description 1
- OYUNTGBISCIYPW-UHFFFAOYSA-N 2-chloroprop-2-enenitrile Chemical compound ClC(=C)C#N OYUNTGBISCIYPW-UHFFFAOYSA-N 0.000 description 1
- JJRDRFZYKKFYMO-UHFFFAOYSA-N 2-methyl-2-(2-methylbutan-2-ylperoxy)butane Chemical compound CCC(C)(C)OOC(C)(C)CC JJRDRFZYKKFYMO-UHFFFAOYSA-N 0.000 description 1
- RFSCGDQQLKVJEJ-UHFFFAOYSA-N 2-methylbutan-2-yl benzenecarboperoxoate Chemical compound CCC(C)(C)OOC(=O)C1=CC=CC=C1 RFSCGDQQLKVJEJ-UHFFFAOYSA-N 0.000 description 1
- FSGAMPVWQZPGJF-UHFFFAOYSA-N 2-methylbutan-2-yl ethaneperoxoate Chemical compound CCC(C)(C)OOC(C)=O FSGAMPVWQZPGJF-UHFFFAOYSA-N 0.000 description 1
- TVONJMOVBKMLOM-UHFFFAOYSA-N 2-methylidenebutanenitrile Chemical compound CCC(=C)C#N TVONJMOVBKMLOM-UHFFFAOYSA-N 0.000 description 1
- BIISIZOQPWZPPS-UHFFFAOYSA-N 2-tert-butylperoxypropan-2-ylbenzene Chemical compound CC(C)(C)OOC(C)(C)C1=CC=CC=C1 BIISIZOQPWZPPS-UHFFFAOYSA-N 0.000 description 1
- CWPKTBMRVATCBL-UHFFFAOYSA-N 3-[1-[1-[(2-methylphenyl)methyl]piperidin-4-yl]piperidin-4-yl]-1h-benzimidazol-2-one Chemical compound CC1=CC=CC=C1CN1CCC(N2CCC(CC2)N2C(NC3=CC=CC=C32)=O)CC1 CWPKTBMRVATCBL-UHFFFAOYSA-N 0.000 description 1
- XZIIFPSPUDAGJM-UHFFFAOYSA-N 6-chloro-2-n,2-n-diethylpyrimidine-2,4-diamine Chemical compound CCN(CC)C1=NC(N)=CC(Cl)=N1 XZIIFPSPUDAGJM-UHFFFAOYSA-N 0.000 description 1
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 1
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
- 108010010803 Gelatin Proteins 0.000 description 1
- GYCMBHHDWRMZGG-UHFFFAOYSA-N Methylacrylonitrile Chemical compound CC(=C)C#N GYCMBHHDWRMZGG-UHFFFAOYSA-N 0.000 description 1
- 229920003171 Poly (ethylene oxide) Polymers 0.000 description 1
- 239000004793 Polystyrene Substances 0.000 description 1
- DBMJMQXJHONAFJ-UHFFFAOYSA-M Sodium laurylsulphate Chemical compound [Na+].CCCCCCCCCCCCOS([O-])(=O)=O DBMJMQXJHONAFJ-UHFFFAOYSA-M 0.000 description 1
- 229920002125 Sokalan® Polymers 0.000 description 1
- 239000004147 Sorbitan trioleate Substances 0.000 description 1
- PRXRUNOAOLTIEF-ADSICKODSA-N Sorbitan trioleate Chemical compound CCCCCCCC\C=C/CCCCCCCC(=O)OC[C@@H](OC(=O)CCCCCCC\C=C/CCCCCCCC)[C@H]1OC[C@H](O)[C@H]1OC(=O)CCCCCCC\C=C/CCCCCCCC PRXRUNOAOLTIEF-ADSICKODSA-N 0.000 description 1
- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 description 1
- KYIKRXIYLAGAKQ-UHFFFAOYSA-N abcn Chemical compound C1CCCCC1(C#N)N=NC1(C#N)CCCCC1 KYIKRXIYLAGAKQ-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- BXIQXYOPGBXIEM-UHFFFAOYSA-N butyl 4,4-bis(tert-butylperoxy)pentanoate Chemical compound CCCCOC(=O)CCC(C)(OOC(C)(C)C)OOC(C)(C)C BXIQXYOPGBXIEM-UHFFFAOYSA-N 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 239000008367 deionised water Substances 0.000 description 1
- 229910021641 deionized water Inorganic materials 0.000 description 1
- 230000002542 deteriorative effect Effects 0.000 description 1
- 235000019329 dioctyl sodium sulphosuccinate Nutrition 0.000 description 1
- YHAIUSTWZPMYGG-UHFFFAOYSA-L disodium;2,2-dioctyl-3-sulfobutanedioate Chemical compound [Na+].[Na+].CCCCCCCCC(C([O-])=O)(C(C([O-])=O)S(O)(=O)=O)CCCCCCCC YHAIUSTWZPMYGG-UHFFFAOYSA-L 0.000 description 1
- GVGUFUZHNYFZLC-UHFFFAOYSA-N dodecyl benzenesulfonate;sodium Chemical compound [Na].CCCCCCCCCCCCOS(=O)(=O)C1=CC=CC=C1 GVGUFUZHNYFZLC-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000007720 emulsion polymerization reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005227 gel permeation chromatography Methods 0.000 description 1
- 229920000159 gelatin Polymers 0.000 description 1
- 239000008273 gelatin Substances 0.000 description 1
- 235000019322 gelatine Nutrition 0.000 description 1
- 235000011852 gelatine desserts Nutrition 0.000 description 1
- 230000009477 glass transition Effects 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 229910052588 hydroxylapatite Inorganic materials 0.000 description 1
- 239000001866 hydroxypropyl methyl cellulose Substances 0.000 description 1
- 235000010979 hydroxypropyl methyl cellulose Nutrition 0.000 description 1
- 229920003088 hydroxypropyl methyl cellulose Polymers 0.000 description 1
- UFVKGYZPFZQRLF-UHFFFAOYSA-N hydroxypropyl methyl cellulose Chemical compound OC1C(O)C(OC)OC(CO)C1OC1C(O)C(O)C(OC2C(C(O)C(OC3C(C(O)C(O)C(CO)O3)O)C(CO)O2)O)C(CO)O1 UFVKGYZPFZQRLF-UHFFFAOYSA-N 0.000 description 1
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 description 1
- MMCOUVMKNAHQOY-UHFFFAOYSA-L oxido carbonate Chemical compound [O-]OC([O-])=O MMCOUVMKNAHQOY-UHFFFAOYSA-L 0.000 description 1
- XYJRXVWERLGGKC-UHFFFAOYSA-D pentacalcium;hydroxide;triphosphate Chemical compound [OH-].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O XYJRXVWERLGGKC-UHFFFAOYSA-D 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 239000004584 polyacrylic acid Substances 0.000 description 1
- 229920002223 polystyrene Polymers 0.000 description 1
- 229940080264 sodium dodecylbenzenesulfonate Drugs 0.000 description 1
- 235000019333 sodium laurylsulphate Nutrition 0.000 description 1
- 229940035044 sorbitan monolaurate Drugs 0.000 description 1
- 235000019337 sorbitan trioleate Nutrition 0.000 description 1
- 229960000391 sorbitan trioleate Drugs 0.000 description 1
- SWAXTRYEYUTSAP-UHFFFAOYSA-N tert-butyl ethaneperoxoate Chemical compound CC(=O)OOC(C)(C)C SWAXTRYEYUTSAP-UHFFFAOYSA-N 0.000 description 1
- 125000000999 tert-butyl group Chemical group [H]C([H])([H])C(*)(C([H])([H])[H])C([H])([H])[H] 0.000 description 1
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
- C08F212/00—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
- C08F212/02—Monomers containing only one unsaturated aliphatic radical
- C08F212/04—Monomers containing only one unsaturated aliphatic radical containing one ring
- C08F212/06—Hydrocarbons
- C08F212/08—Styrene
- C08F212/10—Styrene with nitriles
-
- 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
- C08F212/00—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
- C08F212/02—Monomers containing only one unsaturated aliphatic radical
- C08F212/04—Monomers containing only one unsaturated aliphatic radical containing one ring
- C08F212/06—Hydrocarbons
- C08F212/12—Monomers containing a branched unsaturated aliphatic radical or a ring substituted by an alkyl radical
-
- 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
- C08F2/00—Processes of polymerisation
- C08F2/12—Polymerisation in non-solvents
- C08F2/16—Aqueous medium
- C08F2/18—Suspension polymerisation
Definitions
- It relates to a method for producing a polymer of the present invention, and relates to a method for producing a polymer having improved mechanical properties and processability by widening the molecular weight distribution while maintaining a weight average molecular weight at an appropriate level.
- the polymer including the vinyl cyanide-based monomer unit and the vinyl aromatic-based monomer unit may be prepared by at least one method selected from the group consisting of bulk polymerization, suspension polymerization, and emulsion polymerization.
- Double bulk polymerization has the advantage of high yield because continuous polymerization is possible and high purity because no additives are added.
- bulk polymerization has disadvantages in that the viscosity of the polymerization solution is high during the reaction, so the degree of polymerization is low and it is difficult to control the heat of reaction.
- a method for preparing a polymer by suspension polymerization has been proposed.
- a method of preparing a heat-resistant polymer by introducing an alkyl-substituted vinyl aromatic monomer unit as a component among vinyl aromatic monomer units in the polymer has been proposed.
- these heat-resistant polymers have poor processability due to their high glass transition temperature.
- the processability of the heat-resistant polymer is related to the flow index.
- a lubricant In order to increase the flow index, a lubricant must be mixed with the heat-resistant polymer or the weight average molecular weight of the heat-resistant polymer must be lowered.
- the use of a large amount of the lubricant and the low weight average molecular weight cause a problem of lowering the heat resistance and chemical resistance of the heat resistant polymer.
- Patent Document 1 KR1646311B
- the problem to be solved by the present invention is to provide a method for producing a polymer having improved mechanical properties and processability by widening the molecular weight distribution while maintaining the weight average molecular weight at an appropriate level.
- the present invention comprises the steps of introducing an alkyl-substituted vinyl aromatic monomer and a vinyl cyanide-based monomer into a reactor and initiating polymerization; and polymerizing while continuously introducing an alkyl-substituted vinyl aromatic monomer and a polyfunctional initiator into the reactor, wherein the starting point of the continuous introduction of the alkyl-substituted vinyl aromatic monomer and the polyfunctional initiator is the point at which the polymerization conversion rate is 10 to 30%. And, the point at which the continuous addition of the alkyl-substituted vinyl aromatic monomer and the multifunctional initiator ends is when the polymerization conversion rate is 70 to 80%.
- the present invention provides a method for producing a polymer according to (1) above, wherein the starting point of the continuous addition of the alkyl-substituted vinyl aromatic monomer and the polyfunctional initiator is the point at which the polymerization conversion rate is 15 to 25%.
- the point at which the continuous addition of the alkyl-substituted vinyl aromatic monomer and the polyfunctional initiator is terminated is the point at which the polymerization conversion rate is 70 to 75%.
- the present invention provides a method for producing a polymer according to any one of (1) to (3) above, wherein the alkyl-substituted vinyl aromatic monomer and the polyfunctional initiator are continuously added in a mixed state.
- the content of the continuously added alkyl-substituted vinyl aromatic monomer is based on 100 parts by weight of the total amount of monomers added in the method for preparing the polymer. For, it provides a method for producing a polymer that is 10 to 30 parts by weight.
- the content of the multifunctional initiator continuously added is 0.1 parts by weight based on 100 parts by weight of the total amount of monomers added in the method for preparing the polymer. to 0.5 parts by weight to provide a method for producing a polymer.
- the present invention provides a method for preparing a polymer according to any one of (1) to (6) above, wherein a multifunctional initiator is added in the step of initiating the polymerization.
- the total content of the multifunctional initiator added in the method for preparing the polymer is 100% by weight of the total amount of monomers added in the method for preparing the polymer.
- it provides a method for producing a polymer that is 0.4 to 0.8 parts by weight.
- the multifunctional initiator is 2,2-di (4,4-di (t-butylperoxy) cyclohexyl) propane, 1, 1-di(t-butylperoxy)cyclohexane, 1,1-di(t-amylperoxy)cyclohexane, 1,1-di(t-butylperoxy)-3,3,5-trimethylcyclohexane
- polyether poly (t-butyl peroxy carbonate) provides a method for producing a polymer that is at least one selected from the group consisting of.
- the present invention provides a method for producing a polymer according to any one of (1) to (9) above, wherein the polymerization is suspension polymerization.
- the polymer according to the production method of the present invention implements a wide molecular weight distribution while maintaining a weight average molecular weight at an appropriate level, processability can be remarkably improved while excellent mechanical properties.
- 'polymerization conversion rate' used in the present invention indicates the degree to which monomers polymerize to form a polymer, and can be calculated by the following formula.
- Polymerization conversion rate (%) [(total weight of monomers added until polymerization was completed)-(total weight of unreacted monomers at the time of measuring polymerization conversion)]/(total weight of monomers added until polymerization was completed) weight) ⁇ 100
- the term 'vinyl cyanide-based monomer' used in the present invention may refer to at least one selected from the group consisting of acrylonitrile, methacrylonitrile, 2-ethyl-acrylonitrile and 2-chloroacrylonitrile. there is.
- the vinyl cyanide-based monomer acrylonitrile is preferable.
- the unit derived from the vinyl cyanide-based monomer may be a vinyl cyanide-based monomer unit.
- alkyl-substituted vinyl aromatic monomer' used in the present invention may mean at least one selected from the group consisting of ⁇ -methyl styrene, p-methyl styrene and 2,4-dimethyl styrene.
- vinyl aromatic monomer ⁇ -methyl styrene is preferred.
- the unit derived from the alkyl-substituted vinyl aromatic monomer may be an alkyl-substituted vinyl aromatic monomer unit.
- 'aqueous solvent' used in the present invention may be ion-exchanged water or deionized water.
- the term 'suspending agent' refers to water-soluble polyvinyl alcohol, partially saponified polyvinyl alcohol, polyacrylic acid, polymers of vinyl acetate and maleic anhydride, hydroxypropyl methylcellulose, gelatin, calcium phosphate, tricalcium phosphate, It may be at least one selected from the group consisting of hydroxyapatite, sorbitan monolaurate, sorbitan trioleate, polyoxyethylene, sodium lauryl sulfate, sodium dodecylbenzenesulfonate and sodium dioctylsulfosuccinate, among which Tricalcium phosphate is preferred.
- a method for producing a polymer according to an embodiment of the present invention includes the steps of introducing an alkyl-substituted vinyl aromatic monomer and a vinyl cyanide-based monomer into a reactor and initiating polymerization; and polymerizing while continuously introducing an alkyl-substituted vinyl aromatic monomer and a polyfunctional initiator into the reactor, wherein the starting point of the continuous introduction of the alkyl-substituted vinyl aromatic monomer and the polyfunctional initiator is the point at which the polymerization conversion rate is 10 to 30%. And, the point at which the continuous addition of the alkyl-substituted vinyl aromatic monomer and the multifunctional initiator ends is when the polymerization conversion rate is 70 to 80%.
- an alkyl-substituted vinyl aromatic monomer and a vinyl cyanide-based monomer are introduced into a reactor, and polymerization is initiated.
- the alkyl-substituted vinyl aromatic monomer and the vinyl cyanide-based monomer are added before polymerization starts, the alkyl-substituted vinyl aromatic monomer is polymerized together during polymerization, so the polymerization conversion rate of the alkyl-substituted vinyl aromatic monomer can be improved from the beginning of polymerization. .
- the total amount of the monomers added before polymerization may be 70 to 90 parts by weight, preferably 75 to 85 parts by weight, based on 100 parts by weight of the total amount of monomers added in the polymer production method.
- a polymer having a uniform composition, excellent color, and high weight average molecular weight can be prepared, thereby improving mechanical properties.
- the amount of the alkyl-substituted vinyl aromatic monomer added before polymerization may be 50 to 75 parts by weight, preferably 55 to 70 parts by weight, based on 100 parts by weight of the total amount of monomers added before polymerization starts.
- the content of the vinyl cyanide-based monomer added before polymerization may be 25 to 50 parts by weight, preferably 30 to 45 parts by weight, with respect to the total amount of monomers added before polymerization starts.
- suspension polymerization is preferred for easy control of the reaction, high yield, and simple washing process.
- the suspension polymerization may be initiated in the presence of initiators, suspending agents and suspending aids.
- the initiator, suspending agent, and suspending aid may be added before initiation of polymerization.
- the initiator is 2,5-dimethyl-2,5-di(t-butylperoxy)hexane, di(t-butylperoxy-isopropyl)benzene, t-butylcumyl peroxide, di-(t-amyl) -Peroxide, dicumyl peroxide, butyl 4,4-di(t-butylperoxy)valerate, t-butylperoxybenzoate, 2,2-di(t-butylperoxy)butane, t-amyl Peroxy-benzoate, t-butylperoxy-acetate, t-butylperoxy-(2-ethylhexyl)carbonate, t-butylperoxy isopropyl carbonate, t-butylperoxy-3,5,5-trimethyl -Hexanoate, t-amyl peroxyacetate, t-amylperoxy-(2-ethylhexyl)
- the amount of the initiator may be 0.1 to 0.5 parts by weight, preferably 0.2 to 0.4 parts by weight, based on 100 parts by weight of the total amount of monomers introduced in the polymer production method. If the above conditions are satisfied, the final polymerization conversion rate of the polymer can be increased, and the polymerization rate can be easily controlled. In addition, it is possible to prevent the color characteristics and weight average molecular weight of the polymer from deteriorating.
- the suspending agent may be present in an amount of 0.7 to 2.0 parts by weight, preferably 1.0 to 1.5 parts by weight, based on 100 parts by weight of the total monomers introduced in the polymer production method. If the above conditions are satisfied, the average particle diameter of the polymer can be adjusted to a desired size, and the dispersion stability can be improved.
- the weight ratio of the suspending agent and the suspending aid may be 200:1 to 300:1, preferably 220:1 to 280:1. If the above conditions are satisfied, the average particle diameter of the polymer can be adjusted to a desired size, and the dispersion stability can be improved.
- polymerization is performed while continuously introducing an alkyl-substituted vinyl aromatic monomer and a multifunctional initiator into the reactor.
- the weight average molecular weight of the polymer may be lowered, and mechanical properties, particularly impact resistance, may be lowered.
- an initiator other than the multifunctional initiator is added, the color characteristic of the polymer is lowered and the molecular weight distribution is narrowed, so that a polymer with improved processability cannot be prepared.
- the multifunctional initiator introduced into the polymerization is smaller than the monomer, it may not be easy to continuously introduce the multifunctional initiator alone. Accordingly, for process convenience, it is preferable to continuously introduce the alkyl-substituted vinyl aromatic monomer and the polyfunctional initiator in a mixed state.
- the alkyl-substituted vinyl aromatic monomer having a low polymerization rate is present in excess at the beginning of polymerization. Not only the polymerization rate is significantly lowered, but also the polymerization conversion rate of the alkyl-substituted vinyl aromatic monomer is significantly lowered at the beginning of the polymerization. This can result in polymers with non-uniform composition and reduced color properties throughout the polymerization.
- an alkyl-substituted vinyl aromatic monomer reacts with a vinyl cyanide-based monomer or the like late in polymerization, and an excess of oligomer may be produced.
- the alkyl-substituted vinyl aromatic monomer when the alkyl-substituted vinyl aromatic monomer is continuously added, the alkyl-substituted vinyl aromatic monomer can be polymerized from the beginning of polymerization, so that the color degradation of the polymer caused by excessive reaction of the vinyl cyanide-based monomer at the beginning of polymerization can be prevented.
- the starting point of continuous addition of the alkyl-substituted vinyl aromatic monomer and the polyfunctional initiator may be a polymerization conversion rate of 10 to 30%, preferably a polymerization conversion rate of 15 to 25%.
- a polymer having a uniform composition and improved color and mechanical properties can be prepared.
- the weight average molecular weight of the polymer may decrease and mechanical properties may deteriorate.
- the continuously introduced monomers are not mixed in the reaction system, and thus the transparency of the polymer is lowered and the polymerization conversion rate is lowered, thereby reducing the production efficiency.
- the point at which the continuous addition of the alkyl-substituted vinyl aromatic monomer and the multifunctional initiator is terminated is when the polymerization conversion rate is 70 to 80%, preferably when the polymerization conversion rate is 70 to 75%.
- a polymer having not only a high final polymerization conversion rate but also a moderate weight average molecular weight and a wide molecular weight distribution can be produced with significantly improved processability.
- the continuous addition ends earlier than the above-mentioned range, the effect due to the continuous addition of the monomer is reduced.
- the monomers do not penetrate into the polymer, resulting in a polymer having a non-uniform composition, thereby reducing the transparency of the polymer.
- the amount of the polyfunctional initiator is small, the alkyl-substituted vinyl aromatic monomer is not continuously added, and the multifunctional initiator is continuously added at a polymerization conversion rate of 10 to 30%, and the alkyl-substituted vinyl aromatic monomer is continuously added. It is not possible for the continuous addition of monomers to be terminated at the point where the polymerization conversion rate is 70 to 80%. Specifically, since the input amount of the multifunctional initiator is small, it is difficult to satisfy the continuous input conditions of current polymerization equipment. For this reason, it is not possible to continuously introduce the multifunctional initiator alone at the above-mentioned time point.
- the continuous introduction of the alkyl-substituted vinyl aromatic monomer is initiated at a polymerization conversion rate of 10 to 30%, and the continuous introduction of the alkyl-substituted vinyl aromatic monomer is performed at a polymerization conversion rate of 70 to 30%. If it ends at the point of 80%, the polymerization rate becomes too fast, so that the weight average molecular weight of the obtained polymer becomes too low. As a result, mechanical properties such as impact resistance of the polymer are lowered.
- the content of the continuously added alkyl-substituted vinyl aromatic monomer may be 10 to 30 parts by weight, preferably 15 to 25 parts by weight, based on 100 parts by weight of the total amount of monomers added in the polymer production method. If the above conditions are satisfied, not only can a polymer with improved color and weight average molecular weight be prepared, but also the final polymerization conversion rate is high, and the manufacturing efficiency can be improved.
- the amount of the multifunctional initiator continuously added may be 0.1 to 0.5 parts by weight, preferably 0.2 to 0.4 parts by weight, based on 100 parts by weight of the total amount of monomers added in the method for preparing the polymer. When the above conditions are satisfied, a polymer having improved weight average molecular weight and color characteristics can be prepared.
- the total content of the multifunctional initiator added in the method for preparing the polymer may be 0.4 to 0.8 parts by weight, preferably 0.5 to 0.7 parts by weight, based on 100 parts by weight of the total amount of monomers added in the method for preparing the polymer. . If the above conditions are satisfied, not only can a polymer with improved color and weight average molecular weight be prepared, but also the final polymerization conversion rate is high, and the manufacturing efficiency can be improved.
- the multifunctional initiator is 2,2-di (4,4-di (t-butylperoxy) cyclohexyl) propane, 1,1-di (t-butylperoxy) cyclohexane, 1,1-di (t -amylperoxy)cyclohexane, 1,1-di(t-butylperoxy)-3,3,5-trimethylcyclohexane and polyether poly(t-butyl peroxy carbonate) selected from the group consisting of may be ideal
- the polymerization may be terminated when the polymerization conversion rate is 95% or more.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator (2,2-di (4,4-di (t-butylperoxy) cyclohexyl ) 0.2 parts by weight of propane)
- propane 1.3 parts by weight of a suspending agent (tricalcium phosphate)
- RS-710 suspending aid
- a second reaction solution was prepared by uniformly mixing 20 parts by weight of ⁇ -methyl styrene (AMS) and 0.4 parts by weight of an initiator (2,2-di(4,4-di(t-butylperoxy)cyclohexyl)propane). .
- AMS ⁇ -methyl styrene
- an initiator 2,2-di(4,4-di(t-butylperoxy)cyclohexyl)propane
- the entire amount of the first reaction solution was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization. After polymerization was initiated, polymerization was performed while continuously introducing the entire amount of the second reaction solution at a constant rate from when the polymerization conversion rate reached 10% to when the polymerization conversion rate reached 75%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 10% was 60 minutes, and the continuous introduction time of the second reaction solution was 420 minutes.
- polymerization was performed while raising the temperature of the reactor to 105 ° C. at a constant rate for 20 minutes, and for 220 minutes while the temperature of the reactor was maintained at 105 ° C. After polymerization, polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- the entire amount of the first reaction solution of Example 1 was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization. After the polymerization was initiated, polymerization was performed while continuously introducing the entire amount of the second reaction solution of Example 1 at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 75%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 120 minutes
- the continuous introduction time of the second reaction solution was 360 minutes.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- the entire amount of the first reaction solution of Example 1 was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization. After polymerization was initiated, polymerization was performed while continuously introducing the entire amount of the second reaction solution of Example 1 at a constant rate from when the polymerization conversion rate reached 30% to 75% polymerization conversion rate.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 30% was 180 minutes
- the continuous introduction time of the second reaction solution was 300 minutes.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- the entire amount of the first reaction solution of Example 1 was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization. After polymerization was initiated, polymerization was performed while continuously introducing the entire amount of the second reaction solution of Example 1 at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 70%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 120 minutes
- the continuous introduction time of the second reaction solution was 300 minutes.
- Example 2 After the continuous introduction of the second reaction solution of Example 1 was completed, the temperature of the reactor was maintained at 100 ° C. for 60 minutes, and then the temperature of the reactor was raised to 105 ° C. for 20 minutes at a constant rate. Polymerization was performed, and after polymerization was performed for 220 minutes while the temperature of the reactor was maintained at 105° C., polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- the entire amount of the first reaction solution of Example 1 was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization. After the polymerization was initiated, polymerization was performed while continuously introducing the entire amount of the second reaction solution of Example 1 at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 80%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 120 minutes, and the continuous introduction time of the second reaction solution was 390 minutes.
- polymerization was performed while raising the temperature of the reactor to 105 ° C. at a constant rate for 20 minutes, and in a state where the temperature of the reactor was maintained at 105 ° C. After polymerization for 190 minutes, polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator (2,2-di (4,4-di (t-butylperoxy) cyclohexyl ) 0.4 parts by weight of propane)
- propane 1.3 parts by weight of a suspending agent (tricalcium phosphate)
- RS-710 suspending aid
- a second reaction solution was prepared by uniformly mixing 20 parts by weight of ⁇ -methyl styrene (AMS) and 0.2 parts by weight of an initiator (2,2-di(4,4-di(t-butylperoxy)cyclohexyl)propane). .
- AMS ⁇ -methyl styrene
- an initiator 2,2-di(4,4-di(t-butylperoxy)cyclohexyl)propane
- the entire amount of the first reaction solution was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization. After polymerization was initiated, polymerization was performed while continuously introducing the entire amount of the second reaction solution at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 75%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 90 minutes, and the continuous introduction time of the second reaction solution was 390 minutes.
- polymerization was performed while raising the temperature of the reactor to 105 ° C. at a constant rate for 20 minutes, and for 220 minutes while the temperature of the reactor was maintained at 105 ° C. After polymerization, polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator (2,2-di (4,4-di (t-butylperoxy) cyclohexyl ) 0.4 parts by weight of propane)
- propane 1.3 parts by weight of a suspending agent (tricalcium phosphate)
- RS-710 suspending aid
- a second reaction solution was prepared by uniformly mixing 20 parts by weight of ⁇ -methyl styrene (AMS) and 0.2 parts by weight of an initiator (polyether poly(t-butyl peroxy carbonate)).
- AMS ⁇ -methyl styrene
- initiator polyether poly(t-butyl peroxy carbonate)
- the entire amount of the first reaction solution was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization. After polymerization was initiated, polymerization was performed while continuously introducing the entire amount of the second reaction solution at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 75%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 90 minutes, and the continuous introduction time of the second reaction solution was 390 minutes.
- polymerization was performed while raising the temperature of the reactor to 110 ° C. at a constant rate for 20 minutes, and for 220 minutes while the temperature of the reactor was maintained at 110 ° C. After polymerization, polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator (1,1-di (t-butylperoxy) cyclohexane) 0.2 parts by weight
- suspension A first reaction solution was prepared by uniformly mixing 1.3 parts by weight of agent (tricalcium phosphate) and 0.005 parts by weight of a suspension aid (RS-710 from TOHO Chemical Industry Co., Ltd).
- a second reaction solution was prepared by uniformly mixing 20 parts by weight of ⁇ -methyl styrene (AMS) and 0.4 parts by weight of an initiator (1,1-di(t-butylperoxy)cyclohexane).
- AMS ⁇ -methyl styrene
- initiator 1,1-di(t-butylperoxy)cyclohexane
- the entire amount of the first reaction solution was introduced into the reactor, and the internal temperature of the reactor was raised to 95° C. to initiate polymerization. After polymerization was initiated, polymerization was performed while continuously introducing the entire amount of the second reaction solution at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 75%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 120 minutes, and the continuous introduction time of the second reaction solution was 360 minutes.
- polymerization was performed while raising the temperature of the reactor to 100 ° C. at a constant rate for 20 minutes, and for 220 minutes while the temperature of the reactor was maintained at 100 ° C. After polymerization, polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator (1,1-di (t-butylperoxy) cyclohexane) 0.4 parts by weight
- suspension A first reaction solution was prepared by uniformly mixing 1.3 parts by weight of agent (tricalcium phosphate) and 0.005 parts by weight of a suspension aid (RS-710 from TOHO Chemical Industry Co., Ltd).
- a second reaction solution was prepared by uniformly mixing 20 parts by weight of ⁇ -methyl styrene (AMS) and 0.2 parts by weight of an initiator (1,1-di(t-butylperoxy)cyclohexane).
- AMS ⁇ -methyl styrene
- initiator 1,1-di(t-butylperoxy)cyclohexane
- the entire amount of the first reaction solution was introduced into the reactor, and the internal temperature of the reactor was raised to 95° C. to initiate polymerization. After polymerization was initiated, polymerization was performed while continuously introducing the entire amount of the second reaction solution at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 75%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 90 minutes, and the continuous introduction time of the second reaction solution was 390 minutes.
- polymerization was performed while raising the temperature of the reactor to 100 ° C. at a constant rate for 20 minutes, and for 220 minutes while the temperature of the reactor was maintained at 100 ° C. After polymerization, polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- the entire amount of the first reaction solution of Example 1 was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization. After polymerization was initiated, polymerization was performed while continuously introducing the entire amount of the second reaction solution of Example 1 at a constant rate from when the polymerization conversion rate reached 7% to when the polymerization conversion rate reached 75%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 7% was 30 minutes, and the continuous introduction time of the second reaction solution was 450 minutes.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- the entire amount of the first reaction solution of Example 1 was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization. After polymerization was initiated, polymerization was performed while continuously introducing the entire amount of the second reaction solution of Example 1 at a constant rate from when the polymerization conversion rate reached 34% to when the polymerization conversion rate reached 75%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 34% was 200 minutes
- the continuous introduction time of the second reaction solution was 280 minutes.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- the entire amount of the first reaction solution of Example 1 was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization. After the initiation of the polymerization, polymerization was performed while continuously introducing the entire amount of the second reaction solution of Example 1 at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 66%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 120 minutes, and the continuous introduction time of the second reaction solution was 270 minutes.
- Example 2 After the continuous introduction of the second reaction solution of Example 1 was completed, the temperature of the reactor was maintained at 100 ° C. for 90 minutes, and then the temperature of the reactor was raised to 105 ° C. for 20 minutes at a constant rate. Polymerization was performed, and after polymerization was performed for 220 minutes while the temperature of the reactor was maintained at 105° C., polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- the entire amount of the first reaction solution of Example 1 was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization. After the initiation of polymerization, polymerization was performed while continuously introducing the entire amount of the second reaction solution of Example 1 at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 83%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 120 minutes, and the continuous introduction time of the second reaction solution was 420 minutes.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator (2,2-di (4,4-di (t-butylperoxy) cyclohexyl ) 0.4 parts by weight of propane)
- propane 1.3 parts by weight of a suspending agent (tricalcium phosphate)
- RS-710 suspending aid
- a second reaction solution was prepared by uniformly mixing 20 parts by weight of ⁇ -methyl styrene (AMS) and 0.2 parts by weight of an initiator (t-butylperoxybenzoate).
- AMS ⁇ -methyl styrene
- initiator t-butylperoxybenzoate
- the entire amount of the first reaction solution was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization. After polymerization was initiated, polymerization was performed while continuously introducing the entire amount of the second reaction solution at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 75%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 90 minutes, and the continuous introduction time of the second reaction solution was 390 minutes.
- polymerization was performed while raising the temperature of the reactor to 110 ° C. at a constant rate for 20 minutes, and for 220 minutes while the temperature of the reactor was maintained at 110 ° C. After polymerization, polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator (2,2-di (4,4-di (t-butylperoxy) cyclohexyl ) 0.4 parts by weight of propane)
- propane 1.3 parts by weight of a suspending agent (tricalcium phosphate)
- RS-710 suspending aid
- a second reaction solution was prepared by uniformly mixing 20 parts by weight of ⁇ -methyl styrene (AMS) and 0.2 parts by weight of an initiator (dicumyl peroxide).
- AMS ⁇ -methyl styrene
- initiator dicumyl peroxide
- the entire amount of the first reaction solution was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization. After polymerization was initiated, polymerization was performed while continuously introducing the entire amount of the second reaction solution at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 75%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 90 minutes, and the continuous introduction time of the second reaction solution was 390 minutes.
- polymerization was performed while raising the temperature of the reactor to 130 ° C. at a constant rate for 40 minutes, and for 200 minutes while the temperature of the reactor was maintained at 130 ° C. After polymerization, polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator (1,1-di (t-butylperoxy) cyclohexane) 0.4 parts by weight
- suspension A first reaction solution was prepared by uniformly mixing 1.3 parts by weight of agent (tricalcium phosphate) and 0.005 parts by weight of a suspension aid (RS-710 from TOHO Chemical Industry Co., Ltd).
- a second reaction solution was prepared by uniformly mixing 20 parts by weight of ⁇ -methyl styrene (AMS) and 0.2 parts by weight of an initiator (t-butylperoxybenzoate).
- AMS ⁇ -methyl styrene
- initiator t-butylperoxybenzoate
- the entire amount of the first reaction solution was introduced into the reactor, and the internal temperature of the reactor was raised to 95° C. to initiate polymerization.
- polymerization was performed while continuously introducing the entire amount of the second reaction solution at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 75%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 90 minutes, and the continuous introduction time of the second reaction solution was 390 minutes.
- polymerization was performed while raising the temperature of the reactor to 120 ° C. at a constant rate for 30 minutes, and for 210 minutes while the temperature of the reactor was maintained at 120 ° C. After polymerization, polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator (2,2-di (4,4-di (t-butylperoxy) cyclohexyl ) 0.6 parts by weight of propane)
- propane 1.3 parts by weight of a suspending agent (tricalcium phosphate)
- RS-710 suspending aid
- the entire amount of the first reaction solution was introduced into the reactor, and the internal temperature of the reactor was raised to 100° C. to initiate polymerization.
- 20 parts by weight of ⁇ -methyl styrene (AMS) was continuously added at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 75%.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 60 minutes, and the continuous addition of ⁇ -methyl styrene was 420 minutes.
- Polymerization was performed while the temperature of the reactor was raised to 110° C. at a constant rate for 20 minutes, and polymerization was performed for 220 minutes while the temperature of the reactor was maintained at 110° C., and then polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator (1,1-di (t-butylperoxy) cyclohexane) 0.6 parts by weight
- suspension A first reaction solution was prepared by uniformly mixing 1.3 parts by weight of agent (tricalcium phosphate) and 0.005 parts by weight of a suspension aid (RS-710 from TOHO Chemical Industry Co., Ltd).
- the entire amount of the first reaction solution was introduced into the reactor, and the internal temperature of the reactor was raised to 95° C. to initiate polymerization.
- 20 parts by weight of ⁇ -methyl styrene (AMS) was continuously added at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 75%.
- Polymerization was performed while continuously introducing the entire amount of the second reaction solution at a constant rate.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 120 minutes, and the continuous injection time of ⁇ -methyl styrene (AMS) was 360 minutes.
- Polymerization was performed while the temperature of the reactor was raised to 100° C. at a constant rate for 20 minutes, and polymerization was performed for 220 minutes while the temperature of the reactor was maintained at 100° C., and then polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator benzoyl peroxide
- suspending agent tricalcium phosphate
- suspension A first reaction solution was prepared by uniformly mixing 0.005 parts by weight of an auxiliary agent (RS-710 from TOHO Chemical Industry Co., Ltd).
- the entire amount of the first reaction solution was introduced into the reactor, and the internal temperature of the reactor was raised to 75° C. to initiate polymerization.
- 20 parts by weight of ⁇ -methyl styrene (AMS) was continuously introduced at a constant rate from when the polymerization conversion rate reached 20% to 60% polymerization conversion rate.
- Polymerization was performed while continuously introducing the entire amount of the second reaction solution at a constant rate.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 120 minutes, and the continuous injection time of ⁇ -methyl styrene (AMS) was 360 minutes.
- Polymerization was performed while the temperature of the reactor was raised to 90° C. at a constant rate for 20 minutes, polymerization was performed for 220 minutes while the temperature of the reactor was maintained at 90° C., and polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator polyether poly (t-butyl peroxy carbonate)
- suspending agent tri
- a first reaction solution was prepared by uniformly mixing 1.3 parts by weight of calcium phosphate) and 0.005 parts by weight of a suspension aid (RS-710 from TOHO Chemical Industry Co., Ltd).
- the entire amount of the first reaction solution was introduced into the reactor, and the internal temperature of the reactor was raised to 105° C. to initiate polymerization.
- 20 parts by weight of ⁇ -methyl styrene (AMS) was continuously added at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 75%.
- Polymerization was performed while continuously introducing the entire amount of the second reaction solution at a constant rate.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 120 minutes, and the continuous injection time of ⁇ -methyl styrene (AMS) was 360 minutes.
- Polymerization was performed while the temperature of the reactor was raised to 110° C. at a constant rate for 20 minutes, and polymerization was performed for 220 minutes while the temperature of the reactor was maintained at 110° C., and then polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator t-butylperoxybenzoate
- suspending agent tricalcium phosphate
- the entire amount of the first reaction solution was introduced into the reactor, and the internal temperature of the reactor was raised to 110 °C to initiate polymerization.
- 20 parts by weight of ⁇ -methyl styrene (AMS) was continuously added at a constant rate from when the polymerization conversion rate reached 20% to when the polymerization conversion rate reached 75%.
- Polymerization was performed while continuously introducing the entire amount of the second reaction solution at a constant rate.
- the time required from the initiation of polymerization until the polymerization conversion rate reached 20% was 120 minutes, and the continuous introduction time of ⁇ -methyl styrene (AMS) was 360 minutes.
- Polymerization was performed while the temperature of the reactor was raised to 120° C. at a constant rate for 20 minutes, and polymerization was performed for 220 minutes while the temperature of the reactor was maintained at 120° C., and then polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator (2,2-di (4,4-di (t-butylperoxy) cyclohexyl ) 0.6 parts by weight of propane)
- propane 1.3 parts by weight of a suspending agent (tricalcium phosphate)
- RS-710 suspending aid
- the entire amount of the first reaction solution was introduced into the reactor, and polymerization was initiated by raising the internal temperature of the reactor to 100° C., followed by polymerization for 480 minutes. Subsequently, polymerization was performed while raising the temperature of the reactor to 105° C. at a constant rate for 20 minutes, and polymerization was performed for 220 minutes while the temperature of the reactor was maintained at 105° C., and then polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- AMS ⁇ -methyl styrene
- AN acrylonitrile
- ion-exchanged water 150 parts by weight
- initiator (1,1-di (t-butylperoxy) cyclohexane) 0.6 parts by weight
- suspension A first reaction solution was prepared by uniformly mixing 1.3 parts by weight of agent (tricalcium phosphate) and 0.005 parts by weight of a suspension aid (RS-710 from TOHO Chemical Industry Co., Ltd).
- the entire amount of the first reaction solution was introduced into the reactor, and polymerization was initiated by raising the internal temperature of the reactor to 95° C., followed by polymerization for 480 minutes. Subsequently, polymerization was performed while the temperature of the reactor was raised to 100° C. at a constant rate for 20 minutes, polymerization was performed for 220 minutes while the temperature of the reactor was maintained at 100° C., and polymerization was terminated to obtain a polymerization slurry.
- Formic acid was added to the reactor to adjust the pH of the polymerization slurry to 2.5, followed by washing with water, dehydration, and drying to prepare a polymer in the form of beads.
- Polymerization conversion rate ⁇ (total weight of monomers added until polymerization was completed)-(total weight of unreacted monomers at the time of measuring polymerization conversion) ⁇ /(total weight of monomers added until polymerization was completed) ⁇ 100
- Weight average molecular weight (g/mol) The polymer was prepared by dissolving it in tetrahydrofuran (THF), and then measured by gel permeation chromatography (model name: PL GPC220, manufacturer: Agilent Technologies) at 40 ° C. polystyrene was used.
- Example 9 1st reaction solution (parts by weight) ⁇ -methyl styrene 50 50 50 50 50 Acrylonitrile 30 30 30 30 30 t-BPCP 0.4 0.4 0.0 0.0 t-BPC 0.0 0.0 0.2 0.4 Second reaction solution (parts by weight) ⁇ -methyl styrene 20 20 20 20 t-BPCP 0.2 0.0 0.0 0.0 PEP (t-BPC) 0.0 0.2 0.0 0.0 t-BPC 0.0 0.0 0.4 0.2 Start point of continuous introduction of the second reaction solution (polymerization conversion rate, %) 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20 20
- the starting point of the continuous addition of the alkyl-substituted vinyl aromatic monomer and the multifunctional initiator is the point at which the polymerization conversion rate is 10 to 30%, and the continuous addition of the alkyl-substituted vinyl aromatic monomer and the multifunctional initiator.
- Examples 1 to 9, in which the polymerization conversion rate is 70 to 80% at the end point, have high final polymerization conversion rates, excellent color characteristics, and excellent mechanical properties due to high weight average molecular weight, wide molecular weight distribution, and fluidity. Since the index was high, it was found that the processability was excellent.
- Comparative Example 1 in which the polymerization conversion rate was 7% at the start of the continuous introduction of the alkyl-substituted vinyl aromatic monomer and the polyfunctional initiator, had a lower weight average molecular weight compared to Examples, resulting in lower mechanical properties, narrow molecular weight distribution, and low flow index. Therefore, it was found that the machinability was reduced.
- Comparative Example 3 in which the continuous addition of the alkyl-substituted vinyl aromatic monomer and the polyfunctional initiator was completed at a polymerization conversion rate of 66%, color characteristics were lowered compared to Examples, and processability was lowered due to a low flow index. there was.
- Comparative Example 4 in which the polymerization conversion rate was 83% at the end of the continuous addition of the alkyl-substituted vinyl aromatic monomer and the polyfunctional initiator, had lower color characteristics and lowered weight average molecular weight compared to Example, mechanical properties were lowered, It was found that the processability was deteriorated because the molecular weight distribution was narrow and the flow index was low.
- Comparative Examples 5 to 7 which did not use a multifunctional initiator during continuous addition, had lower color characteristics compared to Examples, lowered mechanical properties due to low weight average molecular weight, and reduced processability due to narrow molecular weight distribution and low flow index. could find out
- Comparative Examples 8 and 9 in which the initiator was added only before polymerization initiation and in which the initiator was not continuously added after polymerization initiation, had lower weight average molecular weights compared to Examples and mechanical properties were deteriorated.
- Comparative Example 10 in which benzoyl peroxide, which is not a multifunctional initiator, was used before polymerization initiation and in which the initiator was not continuously added after polymerization initiation, the final polymerization conversion rate was significantly lowered compared to Examples, and the weight average molecular weight was significantly lower, resulting in lower mechanical properties. It became.
- Comparative Example 11 in which a multifunctional initiator was used before polymerization initiation and in which the initiator was not continuously added after polymerization initiation, had significantly lowered color characteristics compared to Examples, and significantly lowered mechanical properties due to significantly lower weight average molecular weight.
- Comparative Example 12 in which t-butyl peroxybenzoate, not a multifunctional initiator, was used before polymerization initiation, and in which the initiator was not continuously added after polymerization initiation, had significantly lowered color characteristics and significantly lower weight average molecular weight compared to Examples. The mechanical properties were significantly deteriorated.
- Comparative Examples 13 and 14 in which ⁇ -methyl styrene and a multifunctional initiator were not continuously added after the polymerization was initiated, had significantly reduced color characteristics compared to Examples, and decreased mechanical properties due to low weight average molecular weight.
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Abstract
Description
구분 | 실시예 1 | 실시예 2 | 실시예 3 | 실시예 4 | 실시예 5 | |
제1 반응 용액 (중량부) |
α-메틸 스티렌 | 50 | 50 | 50 | 50 | 50 |
아크릴로니트릴 | 30 | 30 | 30 | 30 | 30 | |
t-BPCP | 0.2 | 0.2 | 0.2 | 0.2 | 0.2 | |
제2 반응 용액 (중량부) |
메틸 스티렌 | 20 | 20 | 20 | 20 | 20 |
t-BPCP | 0.4 | 0.4 | 0.4 | 0.4 | 0.4 | |
제2 반응 용액의 연속 투입 개시 시점(중합전환율, %) | 10 | 20 | 30 | 20 | 20 | |
제2 반응 용액의 연속 투입 종료 시점(중합전환율, %) | 75 | 75 | 75 | 70 | 80 | |
총 중합 시간(분) | 720 | 720 | 720 | 720 | 720 | |
물성 | 최종 중합전환율(%) | 97.9 | 98.1 | 98.0 | 98.3 | 96.3 |
색상 | ○ | ○ | ○ | ○ | ○ | |
중량 평균 분자량 | 116,000 | 118,000 | 121,000 | 119,000 | 126,000 | |
분자량 분포 | 2.5 | 2.6 | 2.6 | 2.6 | 2.5 | |
유동지수 | 13.2 | 13.5 | 13.8 | 13.5 | 14.0 | |
t-BPCP: 2,2-디(4,4-디(t-부틸퍼옥시)시클로헥실)프로판 |
구분 | 실시예 6 | 실시예 7 | 실시예 8 | 실시예 9 | |
제1 반응 용액 (중량부) |
α-메틸 스티렌 | 50 | 50 | 50 | 50 |
아크릴로니트릴 | 30 | 30 | 30 | 30 | |
t-BPCP | 0.4 | 0.4 | 0.0 | 0.0 | |
t-BPC | 0.0 | 0.0 | 0.2 | 0.4 | |
제2 반응 용액 (중량부) |
α-메틸 스티렌 | 20 | 20 | 20 | 20 |
t-BPCP | 0.2 | 0.0 | 0.0 | 0.0 | |
PEP(t-BPC) | 0.0 | 0.2 | 0.0 | 0.0 | |
t-BPC | 0.0 | 0.0 | 0.4 | 0.2 | |
제2 반응 용액의 연속 투입 개시 시점(중합전환율, %) | 20 | 20 | 20 | 20 | |
제2 반응 용액의 연속 투입 종료 시점(중합전환율, %) | 75 | 75 | 75 | 75 | |
총 중합 시간(분) | 720 | 720 | 720 | 720 | |
물성 | 최종 중합전환율(%) | 98.2 | 98.4 | 97.8 | 98.0 |
색상 | ○ | ○ | ○ | ○ | |
중량 평균 분자량 | 114,000 | 112,000 | 125,000 | 119,000 | |
분자량 분포 | 2.7 | 2.7 | 2.4 | 2.6 | |
유동지수 | 14.1 | 14.9 | 13.1 | 13.4 | |
t-BPCP: 2,2-디(4,4-디(t-부틸퍼옥시)시클로헥실)프로판 PEP(t-BPC): 폴리에테르 폴리(t-부틸 퍼옥시 카보네이트) t-BPC: 1,1-디(t-부틸퍼옥시)시클로헥산 |
구분 | 비교예 1 | 비교예 2 | 비교예 3 | 비교예 4 | |
제1 반응 용액 | α-메틸 스티렌 | 50 | 50 | 50 | 50 |
아크릴로니트릴 | 30 | 30 | 30 | 30 | |
t-BPCP | 0.2 | 0.2 | 0.2 | 0.2 | |
제2 반응 용액 (중량부) |
α-메틸 스티렌 | 20 | 20 | 20 | 20 |
t-BPCP | 0.4 | 0.4 | 0.4 | 0.4 | |
제2 반응 용액의 연속 투입 개시 시점(중합전환율, %) | 7 | 34 | 20 | 20 | |
제2 반응 용액의 연속 투입 종료 시점(중합전환율, %) | 75 | 75 | 66 | 83 | |
총 중합 시간(분) | 720 | 720 | 720 | 720 | |
물성 | 최종 중합전환율(%) | 98.4 | 97.7 | 98.7 | 95.7 |
색상 | ○ | △ | △ | ○ | |
중량 평균 분자량 | 111,000 | 118,000 | 117,000 | 106,000 | |
분자량 분포 | 2.42 | 2.4 | 2.4 | 2.1 | |
유동지수 | 11.7 | 12.8 | 12.5 | 12.0 | |
t-BPCP: 2,2-디(4,4-디(t-부틸퍼옥시)시클로헥실)프로판 |
구분 | 비교예 5 | 비교예 6 | 비교예 7 | 비교예 8 | 비교예 9 | |
제1 반응 용액 (중량부) |
α-메틸 스티렌 | 50 | 50 | 50 | 50 | 50 |
아크릴로니트릴 | 30 | 30 | 30 | 30 | 30 | |
t-BPCP | 0.4 | 0.4 | 0.0 | 0.6 | 0.0 | |
t-BPC | 0.0 | 0.0 | 0.4 | 0.0 | 0.6 | |
제2 반응 용액 (중량부) |
α-메틸 스티렌 | 20 | 20 | 20 | 20 | 20 |
t-BPCP | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | |
t-BPB | 0.2 | 0.0 | 0.2 | 0.0 | 0.0 | |
DCP | 0.0 | 0.2 | 0.0 | 0.0 | 0.0 | |
제2 반응 용액의 연속 투입 개시 시점(중합전환율, %) | 20 | 20 | 20 | 20 | 20 | |
제2 반응 용액의 연속 투입 종료 시점(중합전환율, %) | 75 | 75 | 75 | 75 | 75 | |
총 중합시간(분) | 720 | 720 | 720 | 720 | 720 | |
물성 | 최종 중합전환율(%) | 97.6 | 96.8 | 97.4 | 98.3 | 98.1 |
색상 | × | × | × | ○ | ○ | |
중량 평균 분자량 | 107,000 | 109,000 | 112,000 | 101,000 | 104,000 | |
분자량 분포 | 2.2 | 2.1 | 2.2 | 2.1 | 2.1 | |
유동지수 | 11.5 | 11.9 | 11.2 | 13.2 | 12.9 | |
t-BPCP: 2,2-디(4,4-디(t-부틸퍼옥시)시클로헥실)프로판 PEP(t-BPC): 폴리에테르 폴리(t-부틸 퍼옥시 카보네이트) t-BPC: 1,1-디(t-부틸퍼옥시)시클로헥산 t-BPB: t-부틸 퍼옥시벤조에이트 DCP: 디쿠밀 퍼옥사이드 |
구분 | 비교예 10 | 비교예 11 | 비교예 12 | 비교예 13 | 비교예 14 | |
제1 반응 용액 (중량부) |
α-메틸 스티렌 | 50 | 50 | 50 | 70 | 70 |
아크릴로니트릴 | 30 | 30 | 30 | 30 | 30 | |
t-BPCP | 0.0 | 0.0 | 0.0 | 0.6 | 0.0 | |
t-BPC | 0.0 | 0.0 | 0.0 | 0.0 | 0.6 | |
PEP(t-BPC) | 0.0 | 0.6 | 0.0 | 0.0 | 0.0 | |
BPO | 0.6 | 0.0 | 0.0 | 0.0 | 0.0 | |
t-BPB | 0.0 | 0.0 | 0.6 | 0.0 | 0.0 | |
제2 반응 용액 (중량부) |
α-메틸 스티렌 | 20 | 20 | 20 | 0 | 0 |
t-BPCP | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | |
TBPB | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | |
DCP | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | |
제2 반응 용액의 연속 투입 개시 시점(중합전환율, %) | 20 | 20 | 20 | 연속 투입 × | 연속 투입 × | |
제2 반응 용액의 연속 투입 종료 시점(중합전환율, %) | 60 | 75 | 75 | 연속 투입 × | 연속 투입 × | |
총 중합시간(분) | 720 | 720 | 720 | 720 | 720 | |
물성 | 최종 중합전환율(%) | 80.4 | 97.1 | 92.2 | 97.1 | 96.9 |
색상 | ○ | △ | × | △ | △ | |
중량 평균 분자량 | 69,000 | 101,000 | 87,000 | 85,000 | 89,000 | |
분자량 분포 | 1.8 | 2.2 | 1.8 | 1.9 | 2.0 | |
유동지수 | 33.2 | 13.4 | 22.6 | 25.5 | 20.9 | |
t-BPCP: 2,2-디(4,4-디(t-부틸퍼옥시)시클로헥실)프로판 PEP(t-BPC): 폴리에테르 폴리(t-부틸 퍼옥시 카보네이트) t-BPC: 1,1-디(t-부틸퍼옥시)시클로헥산 t-BPB: t-부틸 퍼옥시벤조에이트 DCP: 디쿠밀 퍼옥사이드 BPO: 벤조일 퍼옥사이드 |
Claims (10)
- 반응기에 알킬 치환 비닐 방향족계 단량체 및 비닐 시아나이드계 단량체를 투입하고 중합을 개시하는 단계;상기 반응기에 알킬 치환 비닐 방향족계 단량체 및 다관능성 개시제를 연속 투입하면서 중합하는 단계를 포함하고,상기 알킬 치환 비닐 방향족계 단량체 및 다관능성 개시제의 연속 투입 개시 시점은 중합전환율이 10 내지 30 %인 시점이고,상기 알킬 치환 비닐 방향족계 단량체 및 다관능성 개시제의 연속 투입 종료 시점은 중합전환율이 70 내지 80 %인 시점인 중합체의 제조방법.
- 청구항 1에 있어서,상기 알킬 치환 비닐 방향족계 단량체 및 다관능성 개시제의 연속 투입 개시 시점은 중합전환율이 15 내지 25 %인 시점인 것인 중합체의 제조방법.
- 청구항 1에 있어서,상기 알킬 치환 비닐 방향족계 단량체 및 다관능성 개시제의 연속 투입 종료 시점은 중합전환율이 70 내지 75 %인 시점인 것인 중합체의 제조방법.
- 청구항 1에 있어서,상기 알킬 치환 비닐 방향족계 단량체와 다관능성 개시제를 혼합한 상태로 연속 투입하는 것인 중합체의 제조방법.
- 청구항 1에 있어서,상기 연속 투입하는 알킬 치환 비닐 방향족계 단량체의 함량은, 상기 중합체의 제조방법에서 투입하는 단량체의 총 함량 100 중량부에 대하여, 10 내지 30 중량부인 것인 중합체의 제조방법.
- 청구항 1에 있어서,상기 연속 투입하는 다관능성 개시제의 함량은, 상기 중합체의 제조방법에서 투입하는 단량체의 총 함량 100 중량부에 대하여, 0.1 내지 0.5 중량부인 것인 중합체의 제조방법.
- 청구항 1에 있어서,상기 중합을 개시하는 단계에서 다관능성 개시제를 투입하는 것인 중합체의 제조방법.
- 청구항 1에 있어서,상기 중합체의 제조방법에서 투입하는 다관능성 개시제의 총 함량은, 상기 중합체의 제조방법에서 투입하는 단량체의 총 함량 100 중량부에 대하여, 0.4 내지 0.8 중량부인 것인 중합체의 제조방법.
- 청구항 1에 있어서,상기 다관능성 개시제는 2,2-디(4,4-디(t-부틸퍼옥시)시클로헥실)프로판, 1,1-디(t-부틸퍼옥시)시클로헥산, 1,1-디(t-아밀퍼옥시)시클로헥산, 1,1-디(t-부틸퍼옥시)-3,3,5-트리메틸시클로헥산 및 폴리에테르 폴리(t-부틸 퍼옥시 카보네이트)로 이루어진 군에서 선택되는 1종 이상인 것인 중합체의 제조방법.
- 청구항 1에 있어서,상기 중합은 현탁 중합인 것인 중합체의 제조방법.
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KR20120032668A (ko) * | 2010-09-29 | 2012-04-06 | 주식회사 엘지화학 | Abs계 그라프트 공중합체의 제조방법 |
JP2013513680A (ja) * | 2009-12-10 | 2013-04-22 | アクゾ ノーベル ケミカルズ インターナショナル ベスローテン フエンノートシャップ | スチレンの重合方法 |
KR20150037459A (ko) * | 2013-09-30 | 2015-04-08 | 주식회사 엘지화학 | 내열성 san 공중합체의 제조방법 |
KR101646311B1 (ko) | 2013-09-04 | 2016-08-05 | 주식회사 엘지화학 | 내열 san 수지의 제조방법 |
KR20180076645A (ko) * | 2016-12-28 | 2018-07-06 | 주식회사 엘지화학 | 내열성 스티렌계 수지 제조방법 |
-
2023
- 2023-01-17 EP EP23740542.8A patent/EP4286429A1/en active Pending
- 2023-01-17 WO PCT/KR2023/000778 patent/WO2023136699A1/ko active Application Filing
- 2023-01-17 US US18/280,845 patent/US20240150504A1/en active Pending
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
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JP2006522844A (ja) * | 2003-04-14 | 2006-10-05 | アクゾ ノーベル ナムローゼ フェンノートシャップ | スチレンが重合される縣濁プロセスへのパーオキシドの配量 |
JP2013513680A (ja) * | 2009-12-10 | 2013-04-22 | アクゾ ノーベル ケミカルズ インターナショナル ベスローテン フエンノートシャップ | スチレンの重合方法 |
KR20120032668A (ko) * | 2010-09-29 | 2012-04-06 | 주식회사 엘지화학 | Abs계 그라프트 공중합체의 제조방법 |
KR101646311B1 (ko) | 2013-09-04 | 2016-08-05 | 주식회사 엘지화학 | 내열 san 수지의 제조방법 |
KR20150037459A (ko) * | 2013-09-30 | 2015-04-08 | 주식회사 엘지화학 | 내열성 san 공중합체의 제조방법 |
KR20180076645A (ko) * | 2016-12-28 | 2018-07-06 | 주식회사 엘지화학 | 내열성 스티렌계 수지 제조방법 |
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US20240150504A1 (en) | 2024-05-09 |
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