WO1999024495A1 - Modified thermoplastic resin composition and method of producing the same - Google Patents
Modified thermoplastic resin composition and method of producing the same Download PDFInfo
- Publication number
- WO1999024495A1 WO1999024495A1 PCT/JP1998/005035 JP9805035W WO9924495A1 WO 1999024495 A1 WO1999024495 A1 WO 1999024495A1 JP 9805035 W JP9805035 W JP 9805035W WO 9924495 A1 WO9924495 A1 WO 9924495A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- thermoplastic resin
- modifier
- mixing
- polyester
- polymer
- Prior art date
Links
- 229920005992 thermoplastic resin Polymers 0.000 title claims abstract description 185
- 238000000034 method Methods 0.000 title claims abstract description 170
- 239000011342 resin composition Substances 0.000 title claims abstract description 51
- 238000002156 mixing Methods 0.000 claims abstract description 240
- 239000003607 modifier Substances 0.000 claims abstract description 122
- 229920005989 resin Polymers 0.000 claims abstract description 77
- 239000011347 resin Substances 0.000 claims abstract description 77
- 239000000203 mixture Substances 0.000 claims abstract description 29
- 238000001914 filtration Methods 0.000 claims abstract description 22
- 238000002844 melting Methods 0.000 claims abstract description 11
- 230000008018 melting Effects 0.000 claims abstract description 11
- 230000003068 static effect Effects 0.000 claims description 99
- 238000004898 kneading Methods 0.000 claims description 79
- 238000006116 polymerization reaction Methods 0.000 claims description 55
- 239000002245 particle Substances 0.000 claims description 43
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 41
- 229920000728 polyester Polymers 0.000 claims description 41
- 238000003756 stirring Methods 0.000 claims description 41
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 claims description 37
- -1 alkylbenzene sulfonate Chemical class 0.000 claims description 28
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical class OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 27
- 239000003795 chemical substances by application Substances 0.000 claims description 27
- 238000004519 manufacturing process Methods 0.000 claims description 23
- 238000012546 transfer Methods 0.000 claims description 20
- 239000002253 acid Substances 0.000 claims description 13
- QQVIHTHCMHWDBS-UHFFFAOYSA-N isophthalic acid Chemical compound OC(=O)C1=CC=CC(C(O)=O)=C1 QQVIHTHCMHWDBS-UHFFFAOYSA-N 0.000 claims description 12
- 229920001223 polyethylene glycol Polymers 0.000 claims description 12
- 239000002202 Polyethylene glycol Substances 0.000 claims description 10
- 239000011734 sodium Substances 0.000 claims description 9
- 229910052708 sodium Inorganic materials 0.000 claims description 9
- 239000000126 substance Substances 0.000 claims description 7
- WNLRTRBMVRJNCN-UHFFFAOYSA-N adipic acid Chemical compound OC(=O)CCCCC(O)=O WNLRTRBMVRJNCN-UHFFFAOYSA-N 0.000 claims description 6
- 229920001225 polyester resin Polymers 0.000 claims description 6
- 239000004645 polyester resin Substances 0.000 claims description 6
- CXMXRPHRNRROMY-UHFFFAOYSA-N sebacic acid Chemical compound OC(=O)CCCCCCCCC(O)=O CXMXRPHRNRROMY-UHFFFAOYSA-N 0.000 claims description 6
- 230000002441 reversible effect Effects 0.000 claims description 5
- 229920001577 copolymer Polymers 0.000 claims description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- 239000001361 adipic acid Substances 0.000 claims description 3
- 235000011037 adipic acid Nutrition 0.000 claims description 3
- 150000008052 alkyl sulfonates Chemical class 0.000 claims description 3
- IISBACLAFKSPIT-UHFFFAOYSA-N bisphenol A Chemical class C=1C=C(O)C=CC=1C(C)(C)C1=CC=C(O)C=C1 IISBACLAFKSPIT-UHFFFAOYSA-N 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 claims description 3
- 150000004996 alkyl benzenes Chemical class 0.000 claims description 2
- 150000003839 salts Chemical class 0.000 claims description 2
- 229910052799 carbon Inorganic materials 0.000 claims 2
- 150000004714 phosphonium salts Chemical group 0.000 claims 2
- YWWDBCBWQNCYNR-UHFFFAOYSA-N trimethylphosphine Chemical compound CP(C)C YWWDBCBWQNCYNR-UHFFFAOYSA-N 0.000 claims 2
- LZDKZFUFMNSQCJ-UHFFFAOYSA-N 1,2-diethoxyethane Chemical compound CCOCCOCC LZDKZFUFMNSQCJ-UHFFFAOYSA-N 0.000 claims 1
- 229940077388 benzenesulfonate Drugs 0.000 claims 1
- 150000002148 esters Chemical class 0.000 claims 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims 1
- 238000013019 agitation Methods 0.000 abstract description 5
- 229910052751 metal Inorganic materials 0.000 abstract description 2
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- 230000000630 rising effect Effects 0.000 abstract 1
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- 239000004594 Masterbatch (MB) Substances 0.000 description 38
- 238000011156 evaluation Methods 0.000 description 38
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 22
- 238000009987 spinning Methods 0.000 description 20
- 239000000654 additive Substances 0.000 description 18
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- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 239000003963 antioxidant agent Substances 0.000 description 6
- 238000000465 moulding Methods 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000011362 coarse particle Substances 0.000 description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 4
- 239000004743 Polypropylene Substances 0.000 description 4
- 239000004793 Polystyrene Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 230000007423 decrease Effects 0.000 description 4
- 230000006866 deterioration Effects 0.000 description 4
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- 239000000843 powder Substances 0.000 description 4
- 238000002407 reforming Methods 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 229920002292 Nylon 6 Polymers 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
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- VSGNNIFQASZAOI-UHFFFAOYSA-L calcium acetate Chemical compound [Ca+2].CC([O-])=O.CC([O-])=O VSGNNIFQASZAOI-UHFFFAOYSA-L 0.000 description 3
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- 235000011092 calcium acetate Nutrition 0.000 description 3
- 229960005147 calcium acetate Drugs 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 3
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- 150000001875 compounds Chemical class 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 description 3
- 239000000975 dye Substances 0.000 description 3
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- 239000000454 talc Substances 0.000 description 3
- 229910052623 talc Inorganic materials 0.000 description 3
- WVLBCYQITXONBZ-UHFFFAOYSA-N trimethyl phosphate Chemical compound COP(=O)(OC)OC WVLBCYQITXONBZ-UHFFFAOYSA-N 0.000 description 3
- 229920002554 vinyl polymer Polymers 0.000 description 3
- WBIQQQGBSDOWNP-UHFFFAOYSA-N 2-dodecylbenzenesulfonic acid Chemical compound CCCCCCCCCCCCC1=CC=CC=C1S(O)(=O)=O WBIQQQGBSDOWNP-UHFFFAOYSA-N 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 239000004952 Polyamide Substances 0.000 description 2
- 239000004698 Polyethylene Substances 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- ADCOVFLJGNWWNZ-UHFFFAOYSA-N antimony trioxide Chemical compound O=[Sb]O[Sb]=O ADCOVFLJGNWWNZ-UHFFFAOYSA-N 0.000 description 2
- TZCXTZWJZNENPQ-UHFFFAOYSA-L barium sulfate Chemical compound [Ba+2].[O-]S([O-])(=O)=O TZCXTZWJZNENPQ-UHFFFAOYSA-L 0.000 description 2
- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid Chemical compound OC(=O)C1=CC=CC=C1 WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 description 2
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- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 2
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
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- 238000002360 preparation method Methods 0.000 description 2
- YGSDEFSMJLZEOE-UHFFFAOYSA-N salicylic acid Chemical compound OC(=O)C1=CC=CC=C1O YGSDEFSMJLZEOE-UHFFFAOYSA-N 0.000 description 2
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- HVLLSGMXQDNUAL-UHFFFAOYSA-N triphenyl phosphite Chemical compound C=1C=CC=CC=1OP(OC=1C=CC=CC=1)OC1=CC=CC=C1 HVLLSGMXQDNUAL-UHFFFAOYSA-N 0.000 description 2
- 239000000326 ultraviolet stabilizing agent Substances 0.000 description 2
- QPFMBZIOSGYJDE-UHFFFAOYSA-N 1,1,2,2-tetrachloroethane Chemical compound ClC(Cl)C(Cl)Cl QPFMBZIOSGYJDE-UHFFFAOYSA-N 0.000 description 1
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- RNFJDJUURJAICM-UHFFFAOYSA-N 2,2,4,4,6,6-hexaphenoxy-1,3,5-triaza-2$l^{5},4$l^{5},6$l^{5}-triphosphacyclohexa-1,3,5-triene Chemical compound N=1P(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP=1(OC=1C=CC=CC=1)OC1=CC=CC=C1 RNFJDJUURJAICM-UHFFFAOYSA-N 0.000 description 1
- VZSRBBMJRBPUNF-UHFFFAOYSA-N 2-(2,3-dihydro-1H-inden-2-ylamino)-N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]pyrimidine-5-carboxamide Chemical compound C1C(CC2=CC=CC=C12)NC1=NC=C(C=N1)C(=O)NCCC(N1CC2=C(CC1)NN=N2)=O VZSRBBMJRBPUNF-UHFFFAOYSA-N 0.000 description 1
- DEXFNLNNUZKHNO-UHFFFAOYSA-N 6-[3-[4-[2-(2,3-dihydro-1H-inden-2-ylamino)pyrimidin-5-yl]piperidin-1-yl]-3-oxopropyl]-3H-1,3-benzoxazol-2-one Chemical compound C1C(CC2=CC=CC=C12)NC1=NC=C(C=N1)C1CCN(CC1)C(CCC1=CC2=C(NC(O2)=O)C=C1)=O DEXFNLNNUZKHNO-UHFFFAOYSA-N 0.000 description 1
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- AFCARXCZXQIEQB-UHFFFAOYSA-N N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]-2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidine-5-carboxamide Chemical compound O=C(CCNC(=O)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)N1CC2=C(CC1)NN=N2 AFCARXCZXQIEQB-UHFFFAOYSA-N 0.000 description 1
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- DQWPFSLDHJDLRL-UHFFFAOYSA-N triethyl phosphate Chemical compound CCOP(=O)(OCC)OCC DQWPFSLDHJDLRL-UHFFFAOYSA-N 0.000 description 1
- 239000006097 ultraviolet radiation absorber Substances 0.000 description 1
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J3/00—Processes of treating or compounding macromolecular substances
- C08J3/20—Compounding polymers with additives, e.g. colouring
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/74—Mixing; Kneading using other mixers or combinations of mixers, e.g. of dissimilar mixers ; Plant
- B29B7/7461—Combinations of dissimilar mixers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/002—Methods
- B29B7/007—Methods for continuous mixing
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
- B29B7/32—Mixing; Kneading continuous, with mechanical mixing or kneading devices with non-movable mixing or kneading devices
- B29B7/325—Static mixers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
- B29B7/34—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices
- B29B7/38—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary
- B29B7/40—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
- B29B7/34—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices
- B29B7/38—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary
- B29B7/40—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft
- B29B7/401—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft having a casing closely surrounding the rotor, e.g. with a plunger for feeding the material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
- B29B7/34—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices
- B29B7/38—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary
- B29B7/40—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with single shaft
- B29B7/405—Mixing heads
- B29B7/407—Mixing heads with a casing closely surrounding the rotor, e.g. with conical rotor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/74—Mixing; Kneading using other mixers or combinations of mixers, e.g. of dissimilar mixers ; Plant
- B29B7/7476—Systems, i.e. flow charts or diagrams; Plants
- B29B7/748—Plants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B7/00—Mixing; Kneading
- B29B7/74—Mixing; Kneading using other mixers or combinations of mixers, e.g. of dissimilar mixers ; Plant
- B29B7/7476—Systems, i.e. flow charts or diagrams; Plants
- B29B7/7485—Systems, i.e. flow charts or diagrams; Plants with consecutive mixers, e.g. with premixing some of the components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/362—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die using static mixing devices
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/395—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die using screws surrounded by a cooperating barrel, e.g. single screw extruders
- B29C48/40—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die using screws surrounded by a cooperating barrel, e.g. single screw extruders using two or more parallel screws or at least two parallel non-intermeshing screws, e.g. twin screw extruders
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J3/00—Processes of treating or compounding macromolecular substances
- C08J3/20—Compounding polymers with additives, e.g. colouring
- C08J3/203—Solid polymers with solid and/or liquid additives
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J3/00—Processes of treating or compounding macromolecular substances
- C08J3/20—Compounding polymers with additives, e.g. colouring
- C08J3/22—Compounding polymers with additives, e.g. colouring using masterbatch techniques
- C08J3/226—Compounding polymers with additives, e.g. colouring using masterbatch techniques using a polymer as a carrier
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B9/00—Making granules
- B29B9/02—Making granules by dividing preformed material
- B29B9/06—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
- B29K2067/00—Use of polyesters or derivatives thereof, as moulding material
Definitions
- thermoplastic resin composition and method for producing the same-Technical field.
- the present invention relates to a modified thermoplastic resin and a method for producing the same. More specifically, the present invention relates to a highly modified thermoplastic resin containing and / or copolymerized with a modifier useful for fiber applications, film applications and other molded article applications. The present invention relates to a method of continuously producing a resin while imparting uniformity and dispersibility, and a thermoplastic resin composition obtained by the method. Background art
- Thermoplastic resin represented by polyester, polyamide, polyolefin, etc. (Hereinafter, in this specification, the term “resin” simply refers to the "thermoplastic resin.") Because of its excellent physical and chemical properties, it is widely used in fibres, films and other molded articles. However, despite its excellent properties, there were problems with workability in the molding process of these resins, poor workability due to poor slipperiness when handling the molded products themselves, and a decrease in product value. It is also known that undesirable problems occur.
- thermoplastic resin has properties that cannot be obtained by the resin alone as long as the original excellent performance of the resin is not lost, such as flame retardancy, antistatic property, easy dyeing property, clear dyeing property, and heat resistance.
- a modified resin imparted with various properties it is used in a wider range of industrial fields.
- As a technology for manufacturing resins that meet the demand for use in such a wide range of applications in addition to the aforementioned method of adding particles, blending various functional substances into resins according to their purposes And copolymerization methods. Many of these methods have been successful in achieving higher performance and higher functionality of the final product.
- thermoplastic resin examples include, for example, providing a mixing device on a transport passage of a polymer in a molding process such as a yarn forming process or a film forming process, whereby various additives are added. Attempts have been made to uniformly add and mix the resin. However, in general, even if a powdery, liquid or paste-like additive is directly added to and mixed with the resin, the thermoplastic resin in the molten state has a high viscosity, so the additive in the resin is The dispersibility of the fiber is poor, and the quality is insufficient for use in fiber and film.
- a so-called “master batch” containing the additives in a high concentration is prepared in advance, and the A method of improving the dispersibility of additives in a resin by kneading the resin into a molten resin has been used.
- the viscosity of the master batch is reduced when one master batch is kneaded with resin.
- the surface tension can be made close to that of the resin to be kneaded, and the state of mixing can be enhanced.
- a static mixing device is used as a device for mixing in the middle of a flow path for transferring a resin to a molding process.
- this static mixing device two types of chips consisting of a resin and a master batch are blended and charged before a kneading extruder that melts the resin into chips and melted. After that, a method is known in which the mixture is passed through a static mixing device and sent to a yarn-making machine (see Japanese Patent Application Laid-Open No. 59-1256457).
- a continuous polymerization method is being replaced with a conventional batch method.
- the continuous polymerization method has less variation in product quality than the batch polymerization method, and can produce a large number of specific brands over a long period of time, which is overwhelmingly advantageous in terms of cost.
- the intrinsic viscosity decreases over time during product discharge, the color deteriorates, and the quality changes between different batches, the raw material charge fluctuation, or the reaction condition fluctuations cause batch-to-batch deterioration. Quality fluctuations.
- the continuous polymerization method controls the process conditions appropriately so as to cancel such external disturbances, so that the resulting products can change over time in the polymerization process. Is relatively easy to minimize. Furthermore, while it is difficult to increase the capacity of existing equipment per batch in the batch method, the continuous polymerization method is becoming larger and larger due to the progress of technological innovation in recent years. It is growing more and more.
- the continuous polymerization method has the drawback that small turns are not effective in producing many kinds and small quantities.
- the drawbacks of the continuous polymerization method have become more serious.
- the continuous polymerization direct membrane method or the direct spinning method is a method in which a polymer after completion of polymerization is chipped once, stored in a silo, dried, and then formed into a film. Attempts have been made to omit steps that are essential in batch systems when transporting to the spinning process. Such attempts have led to more sophisticated processes. Are being pursued.
- the rotation generated in response to the rotation cycle of the pump used to feed the modifier-containing thermoplastic resin that is, the unevenness in the concentration and quality of the masterbatch, and the base polymer and the polymer containing the modifier.
- the problem that periodic mottling of the polymer due to periodical mottling, etc. cannot be avoided is being closed up.
- the continuous polymerization method has the disadvantage that the production is not easily turned around.However, in the continuous polymerization method, the need for higher functionality and diversification of the resin by the modifier is increasing more and more. That is the current situation. Under such circumstances, as an attempt to perform production in response to diversification of brands, there is a technique proposed in, for example, Japanese Patent Publication No. 46-37767. In this technique, in a continuous polymerization apparatus composed of multistage polymerization cans, a plurality of molten polymers having different polymerization stages are appropriately removed from the polymerization cans and blended or combined.
- polyesters having different degrees of polymerization are obtained, or these polyesters are appropriately combined.
- a multi-brand technology has been proposed in which a composite fiber having a potential crimping performance is efficiently produced by adding such operations in a variety of combinations.
- this technology uses only a combination of multiple polymers with different polymerization stages in a method for producing a single polymer that is produced consistently by continuous polymerization.
- the present inventors have sought to improve the above-mentioned drawbacks of the conventional method and to uniformly disperse and mix various modifiers in a thermoplastic resin having high dispersibility without causing unevenness with time. Therefore, provide a modified thermoplastic resin composition and a process for its production, which is a mixing method that can withstand straight film or straight spinning and that can flexibly respond to diversification of production and multi-brand production. It is assumed that
- the present invention has excellent dispersibility of the modifying agent in the thermoplastic resin, and therefore has molding processability or various functions for forming fibers, films, and resin molded products, and has a high degree of dispersibility.
- An object of the present invention is to provide a thermoplastic resin composition that does not cause aging spots and a method for producing the same.
- the modified thermoplastic resin in which the variation with time has been eliminated can be obtained. This enables continuous production of resin. Disclosure of the invention
- an object of the present invention is to uniformly add a modifier to a continuously polymerized thermoplastic resin in a molten state, and as a result, to obtain a uniform dispersibility and a modification without aging.
- At least one type of thermoplastic resin containing a modifier is added and mixed to the flow path for transferring the thermoplastic resin, and the above-mentioned process is performed when the thermoplastic resin composition containing the modifier is continuously produced. This involves performing static mixing and dynamic mixing on these in the transfer channel.
- the dynamic mixing is performed by passing through a dynamic mixing device having a stirring blade and power for driving the stirring blade.
- the dynamic mixing device used in the present invention is a complete mixing tank or a kneading extruder.
- the stirring blade is selected from the group consisting of double helical ribbon wing, anchor wing, double motion paddle wing, helical screw wing, MIG wing and rim cone wing.
- the use of any one of the stirring blades can be preferably used to eliminate the unevenness of the thermoplastic resin that has been continuously polymerized over time.
- the modified thermoplastic resin composition of the present invention is obtained by the above-described method of the present invention, and comprises a modifier containing a modifier in a flow path for transferring a thermoplastic resin in a molten state. At least one kind of the contained thermoplastic resin is added and mixed, and the continuous production of the modified thermoplastic resin composition results in a 240 mm inner diameter mesh wire mesh fin. 33.3 minutes at a temperature of 20 ° C. or more and 100 ° C. or less of the melting point of the modified thermoplastic resin or the plasticization point. The rate of increase in filtration pressure when filtering at a filtration rate is 10 kg / cm 2 / h or less.
- FIGS. 1 and 2 are front sectional views respectively showing an embodiment of a dynamic mixing apparatus for mixing a modified thermoplastic resin by an external power to carry out the method of the present invention.
- FIGS. 3 to 13 and FIG. 17 show the respective embodiments of the present invention.
- FIGS. 3A and 3B are schematic process diagrams schematically illustrating the state, in which these figures are for dynamic mixing using the dynamic mixing apparatus illustrated in FIGS. 1 and Z or FIG.
- FIGS. 14 to 16 show examples of respective embodiments when a kneading extruder is used as a dynamic mixing device other than the dynamic mixing device illustrated in FIG. 1 and / or FIG.
- FIGS. 18 to 20 are schematic process diagrams schematically illustrating a conventional method for producing a modified thermoplastic resin, respectively. It is. BEST MODE FOR CARRYING OUT THE INVENTION
- thermoplastic resin “modifier-containing thermoplastic resin”, and “modified thermoplastic resin” are clearly distinguished from each other as “resins having different properties”. Keep it.
- thermoplastic resin is a crystalline or amorphous resin exhibiting thermoplasticity, for example, a polycondensation polymer such as a polyester or a polyamide, or a polycondensation polymer.
- Addition-condensation polymers such as urethane, and vinyl polymers such as methacrylic resins such as polyethylene, polypropylene, polystyrene, polychlorinated vinyl, and polymethylmethacrylate.
- Various thermoplastic resins may contain particles or additives in advance or may be copolymerized in advance as long as its properties are not lost.
- the “thermoplastic resin” is sometimes referred to as a base polymer or a straight polymer.
- the “modifier-containing thermoplastic resin” in the present invention refers to the resin itself or a resin polymerized by a polymerization apparatus different from the resin itself as described above.
- the resin component of the thermoplastic resin containing the modifier is preferably compatible with the thermoplastic resin, and more preferably the same. This is because the compatibility with the thermoplastic resin improves the mixing property of the two and makes the dispersibility more highly uniform.
- modified “modifier” in the present invention examples include inorganic oxides such as titanium oxide, silicon oxide, calcium carbonate, kaolinite, talc, alumina, zeolite, graphite, and barium sulfate. Particles, polystyrene, polymethyl methacrylate, methyl methacrylate copolymer, methyl methacrylate crosslinked copolymer, polytetrafluoroethylene, polyvinylidene fluoride And organic particles such as polyacrylonitrile, benzoguanamine resin, and cross-linked silicone resin. Further, these particles are described in, for example, Japanese Patent Application Laid-Open No.
- the silane coupling agent and / or the titanium coupling agent It does not matter even if it is processed in such as.
- particles of silicon oxide, titanium oxide, alumina, polystyrene, cross-linked silicone resin, or particles in which the surface of these particles is coated with another compound are suitably used industrially.
- the organic and Z or inorganic particles are preferably of an average particle size
- the non-copolymerized functional modifier is not particularly limited since it should be contained by appropriately selecting the type of thermoplastic resin and the modifier according to the purpose of modification. .
- non-copolymerized functional modifier used as a modifier
- a flame retardant an antistatic agent, an easy dye, a heat-resistant agent , An antioxidant, a deepening agent, a crystallinity modifier, an ultraviolet absorber, an ultraviolet stabilizer, and the like.
- flame retardants include phosphorus compounds such as triethyl phosphate, tris (/ S-chloroethyl) phosphate, xylenyldiphenylphosphonate, and antimony trioxide.
- phosphorus compounds such as triethyl phosphate, tris (/ S-chloroethyl) phosphate, xylenyldiphenylphosphonate, and antimony trioxide.
- Nitimon compounds zirconium hydroxide, and the like.
- antistatic agent examples include fatty acid ester metal salts, alkyl sulfonates, and alkylbenzene sulfonic acids.
- alkyl benzene sulfonic acid is widely used in various resins, and is commercially available as a mixture of various molecular weight agents for the purpose of sufficiently exhibiting antistatic performance. A value of 30 or less is desirable from the viewpoint of antistatic performance and thermal stability of the agent.
- Examples of easy dyes include polyethylene glycol and other polyalkylene glycols.
- Polyethylene glycol has various molecular weights, but in the case of this application, it is preferable that the molecular weight is large because the amorphous portion is formed to be large. Is preferably 40000 or more.
- Examples of the deepening agent include calcium trimethylphosphate and quaternary phosphonium magnesium isophthalate.
- heat-resistant agent examples include normal phosphoric acid and phosphorous acid.
- crystallinity modifier examples include benzoic acid, p-oxybenzoic acid, ⁇ -decanoic acid, and the like.
- antioxidants include phenol-based antioxidants such as 2,6-di-t-butyl-P-cresole, and 2,2′-methylenebis (4-ethyl-6 Bisphenolic antioxidants such as —t-butylphenol) and tetraxone (methylen-3— (3,, 5′-di-t-butyl-1-4′-hydroxyphenyl) propione
- Polyphenolic compounds such as methane, sulfur-based antioxidants such as di-stearyl-1,3,3'-thiodiprobionate, and phosphorus such as triphenylphosphite Based antioxidants.
- UV absorbent examples include salicylic acid-based absorbents such as p-t-butyldizarite sylate, benzophenone-based absorbents such as 2,4-dihydroxybenzobenzophenone, and 2 — (2 '— Hydroxy-1 5' — Triazole compounds such as t-butylphenyl and benzotriazole.
- ultraviolet stabilizer examples include hindered amide compounds such as bis (2,2,6,6—tetramethyl-14-piperidyl) sebacate).
- the modifier-containing thermoplastic resin obtained by copolymerizing the third component for example, if a vinyl polymer resin is used, it is widely practiced to randomly copolymerize another vinyl polymer.
- examples of the moldability improver include polyethylene and 11-butene.
- a polyester as an example of the polycondensation polymer resin, as a clear dye, 5-sulfur sodium sulfophthalic acid or an ester-forming derivative thereof, or a quaternary phosphonium thereof.
- Substituent salts are mentioned, and as the formability improver, there are isophthalic acid, adipic acid, sebacic acid or ester-forming derivatives thereof.
- the physical property modifiers for the diol component include diethylene glycol, triethylene glycol, polyethylene glycol, and bisphenol A And thilenoxide adducts.
- polyethylene glycol is widely used because it is inexpensive and easily exhibits a reforming function.However, when it is used for this purpose, it must be copolymerized with a resin, and a preferable molecular weight is used. Is not more than 400.
- the modifier contained in the modifier-containing thermoplastic resin may be one type or a plurality of types. In addition, it does not matter if particles, non-copolymerizing modifiers and copolymerizing modifiers are mixed.
- the weight ratio of the modifier in preparing the modifier-containing thermoplastic resin can be appropriately selected according to the content in the finally obtained modified thermoplastic resin.
- a thermoplastic resin is thickened by incorporating a modifier, it is considered that the higher the concentration of the modifier to be added, the higher the shearing force and the better the dispersion.
- the thermoplastic resin containing filler is added into the base polymer, the relative amount of the modifier-containing thermoplastic resin to be added becomes smaller, so that a larger amount of distributive mixing is required. Therefore, there is an optimum value for the concentration of the modifier in the thermoplastic resin containing the modifier. It should be noted that there is an optimum value when the viscosity decreases, as in the case where the viscosity increases.
- the appropriate range of the modifier content in the modifier-containing thermoplastic resin varies depending on the combination of the thermoplastic resin and the modifying agent, but is preferably the entirety of the modified thermoplastic resin. It is in the range of 0.01 to 70% by weight based on the weight, and the concentration may be appropriately designed appropriately in accordance with the modifier within the range. If the content is less than 0.01% by weight, the production of the modified thermoplastic resin composition has too little dilution factor to limit the quantitative performance. In addition, it has no cost advantage and loses its business significance. On the other hand, when the concentration is higher than 70% by weight, the quality of the modifier is deteriorated due to the thermal degradation of the modifier or the decomposition of the resin due to the resolution of the modifier.
- the mixing of the modifier-containing thermoplastic resin with the thermoplastic resin obtained by continuous polymerization without the addition of the modifier is performed by using a transfer channel (“transfer line”) of the thermoplastic resin.
- transfer line a transfer channel of the thermoplastic resin. It is preferable to carry out the above, but as a method of supplying the thermoplastic resin in a molten state to the transfer line, the thermoplastic resin is temporarily chipped, dried, and then melt-mixed by a kneading extruder again. Alternatively, a sidestream may be taken from the thermoplastic resin transfer line, mixed with the modifier above a given concentration to form an intermediate preparation, and then based again. It may be returned to the thermoplastic resin transfer line. Which method to use may be selected as appropriate in accordance with the operating conditions, and may vary depending on, for example, the design of the intrinsic viscosity of the thermoplastic resin, the frequency of brand switching, and the ease of cleaning the manufacturing equipment. .
- the modifier in order to prepare the modifier-containing thermoplastic resin, the modifier may be directly added to the thermoplastic resin that has been continuously polymerized and dispensed, or the thermoplastic resin that has been continuously polymerized may be used.
- a modifier may be added to the thermoplastic resin obtained through another process such as once forming a chip.
- the thermoplastic resin as the base polymer before the addition of the modifier is modified with the thermoplastic resin.
- the mixing operation to obtain the modified thermoplastic resin by mixing with the thermoplastic resin containing the additive, the static mixing operation without external power and the forced dynamic mixing operation with external power are combined. It is essential to do it.
- the “static mixing” in the present invention means that a flow composed of a modified thermoplastic resin is repeatedly divided in a cross section perpendicular to the flow direction, It is a mixture that is dispersed and distributed.
- This static mixing for example, when the modifier is already dispersed to some extent in the modified thermoplastic resin, must be mixed by applying external power to forcibly apply a large shear force. However, it is useful because mixing can be performed to a certain extent relatively smoothly.
- a static mixing device capable of performing such static mixing conventionally known devices can be used. For example, a Kenics-type static mixer, a sluser, first manufactured by Kenics Co., Ltd.
- a commercially available static mixing device such as a through mixer type static mixing element first manufactured by one company or a high mixer (trade name) manufactured by Toray Industries, Inc. can be preferably used.
- a Kenics-type static Taking a mixer as an example, it is desirable to install a mixer in which the number of divided elements per static mixer is 10 elements or more. This is self-evident in view of the fact that the object of the present invention is to obtain a highly uniformly dispersed modified thermoplastic resin. Also, for other static mixing devices having different polymer division types, the details of the number of division elements and the like need not be described here, and modifications required by those skilled in the art are required. It is only a matter of condition selection that only needs to select and use the number of divided elements according to the quality of the high-quality thermoplastic resin, and will not be described any further.
- thermo mixing refers to “a stirring blade driven by external power”.
- the modified thermoplastic resin is passed through a dynamic mixing device and / or a kneading extruder, and mixed within a certain residence time.
- the “perfect mixing tank” refers to a “can-shaped mixing tank having stirring blades driven by external power”.
- the tank shape, tank dimensions, The optimum liquid depth and the like may be used according to the production conditions, and the optimal conditions may be appropriately selected and used according to the production conditions of the modified thermoplastic resin.
- the shape of the stirring blade a well-known blade shape used for high-viscosity mixing / dispensing can be used, thereby realizing various different mixing types.
- double-helical ribbon wings, anchor wings, double-moment paddle wings, helical screw wings, MIG wings and helicone wings are particularly preferably used because of their excellent mixing properties.
- the clearance between the blade walls, the blade pitch, the blade width, and the number of blades may be appropriately selected and used according to production conditions.
- the stirring method is either the up-pulling method or the down-pulling method. Good.
- a high rotation speed is desirable for the stirring rotation speed in order to promote mixing, but if the polymer has a high viscosity, if the rotation speed is too high, the strength of the blade material may be insufficient. It is not preferable because the required stirring power becomes too large. For this reason, a preferred stirring speed is 1 to 30 rpm.
- the modified thermoplastic resin when performing dynamic mixing, it is necessary to allow the modified thermoplastic resin to stay in the dynamic mixing device for a certain period of time in order to eliminate unevenness over time.
- the number is more preferably more than 150.
- the residence time in the dynamic mixing device is preferably less than 20 minutes, and more preferably. It should be less than 15 minutes.
- the “complete mixing tank” may be provided with a vent line.
- the vent line can be used to maintain a vacuum in the complete mixing tank, and the modified thermoplastic resin in the tank can be maintained. This can suppress a decrease in the intrinsic viscosity of the resin.
- a screw provided with a disk segment for resin extrusion and / or kneading is provided.
- An extruder is preferred.
- the number of screws may be one, two or more, but a single-shaft and Z- or twin-screw extruder is preferred in terms of equipment cost and maintainability.
- the reason for using a kneading extruder to perform dynamic mixing is that the kneading extruder has a function of kneading while retaining the resin for a certain period of time. This is because it is possible to eliminate aging spots of the resin.
- an appropriate screw configuration according to the purpose may be used.
- a reverse feed segment at least at one or more locations on the screw. This is because, by providing such a reverse feeding means in the kneading extruder, a part of the modified thermoplastic resin moving in the kneading extruder can be reversely fed in the moving direction. This is because mixed plaques over time can be eliminated.
- the rotation speed of the screw only needs to be within a range in which the resin is fed normally and the resin is not excessively heated by the shearing stress, for example, 100 to 500. A range of rpm is preferably used.
- the residence time of the modified thermoplastic resin in the extruder is preferably within 15 minutes.
- a non-vented kneading extruder may be used, but it is preferable to use a vented one.
- the static mixing device when at least one static mixing device and one dynamic mixing device are respectively installed, the static mixing device may be arranged first and the dynamic mixing device may be arranged later. Conversely, the dynamic mixing device may be arranged first, and the static mixing device may be arranged later. Such an arrangement may be appropriately selected in consideration of the type of the modifier, the viscosity of the polymer, the installation location of the apparatus, and the ease of cleaning.
- better mixing characteristics are improved by installing at least one of two types of mixing devices having greatly different mixing modes such as a static mixing device and a dynamic mixing device.
- a static mixing device and a dynamic mixing device.
- High quality thermoplastic resin In this case, two or more static mixing devices may be installed in series or in parallel to perform static mixing, and then a dynamic mixing device may be installed to perform dynamic mixing, or after dynamic mixing.
- Static mixing equipment Static mixing may be performed by installing two or more units in series or in parallel. Also
- the dynamic mixing may be performed by installing two or more dynamic mixing devices in series or in parallel.
- the static mixing operation and the dynamic mixing operation are performed a plurality of times as described above, they may be the same type of mixing, but in order to obtain better mixing characteristics, different types of mixing are required. Is preferred.
- the size of the mixing tank, the shape of the stirring blade and the stirring speed are changed, or if a kneading extruder is used.
- the composition of the screw segment By changing the rotation speed of the screw, various “mixing types” in which the residence time of the polymer and the number of agitation are changed can be adopted. Lima's first class can be mixed in more complicated ways. Further, a complete mixing tank and a kneading extruder may be used in combination.
- the arrangement of the mixing devices is such that static mixing devices and dynamic mixing devices are provided alternately, and static mixing and dynamic mixing operations are performed.
- the mixing efficiency is excellent.
- the number of times of the alternating mixing operation is counted as having received the mixing operation once after going through either the static mixing operation or the dynamic mixing operation. It is preferable to perform the mixing operation twice or more. In this case, it does not matter whether the mixing operation of the static mixing operation or the dynamic mixing operation is performed first.
- the static mixing operation may be performed before the dynamic mixing operation, or the dynamic mixing operation may be performed.
- the mixing operation may be performed before the static mixing operation.
- such a mixture In the mixing operation, the polymer is subjected to static mixing, dynamic mixing, and static mixing, followed by three mixing operations in this order, or two mixing operations in which static mixing is performed after dynamic mixing.
- the reason why the former mixing example is preferable is that mixing unevenness in a plane perpendicular to the flow direction of the polymer is again caused by the flow characteristics of the polymer in the dynamic mixing device for dynamic mixing. What can happen? In other words, even if the polymer is mixed in a plane perpendicular to the flow direction of the polymer by static mixing, it is then mixed in the flow direction of the polymer (that is, the aging direction) by dynamic mixing.
- thermoplastic resin containing the modifier is added to the base thermoplastic resin, dynamic mixing is first performed to make uniform over time, and then static mixing is performed. Distributive mixing between the resins proceeds extremely smoothly, and dynamic mixing is further performed thereafter, so that unevenness in resin quality over time due to the influence of drift and the like generated during dynamic mixing can be completely eliminated.
- the number of dynamic mixers and static mixers is increased more than necessary, the effect of improving the kneading degree (uniform dispersity) of the modifier at a certain level will level off, while on the other hand the equipment installation costs It is not preferable because various drawbacks such as rise in the temperature, complexity of maintenance, and deterioration of the quality due to the long-term retention of the polymer in the mixing device become apparent. But Although it depends on the production conditions of the modified thermoplastic resin, it is usually preferable that the number of the mixing devices to be installed is 5 or less in total, including the static mixing device and the dynamic mixing device.
- a plurality of transfer channels such as a payout line for a thermoplastic resin serving as a base are branched into a plurality of portions, and a thermoplastic resin containing a modifier is added and mixed to each branch line.
- the modified thermoplastic resin composition can be produced at the same time.
- This method has very high industrial utility because it can easily cope with diversification of brands.
- it is preferable to adopt a configuration in which a base straight polymer is produced by a continuous polymerization method, and the polymer is branched into a plurality of lines at the outlet of the polymer.
- a straight polymer, a bright polymer, a semi-polymer, and a full-polymer can be simultaneously produced.
- it is easy to flexibly change the amount of additive-containing thermoplastic resin added to the base polymer in response to fluctuations in demand and inventory, diversifying brands and adjusting production volumes flexibly. It is very effective.
- thermoplastic resin composition containing a modifier are added to a transfer line such as a base polymer payout line.
- a transfer line such as a base polymer payout line.
- a plurality of thermoplastic resin compositions containing a modifier are pelletized, and the pellets are blended and injected into an extruder to be melted, followed by melting of a base polymer. It can also be added to the payout line.
- a plurality of modifier-containing thermoplastic resin compositions are added to the base polymer payout line via kneading extruders provided corresponding to each of the plurality of modifier-containing thermoplastic resin compositions. Each of the plastic resin compositions may be charged.
- the method of the present invention is capable of uniformly dispersing various particles and modifiers at an extremely high level due to its high uniform dispersibility.
- a plurality of master batches are kneaded and a plurality of reformers are kneaded. It is also possible to have a quality function.
- a masterbatch of titanium oxide and a masterbatch of 5-sodium sodium sulfophthalic acid copolymer are blended and added simultaneously to improve opacity and cationic dyeing. The effect can be provided simultaneously.
- the modifier content of the modified thermoplastic resin composition in the present invention can be appropriately selected depending on the type of resin, the type of modifier, and the target quality of the resin composition.
- the preferred range of modifier content is from 0.001 to 50% by weight, based on the total weight of the modified thermoplastic resin composition. If the amount is less than 0.001% by weight, the function of the modifier will not be exhibited, which is not preferable. On the other hand, if it exceeds 50% by weight, the quality of the resin composition is significantly degraded by the modifier, and even if it is formed into a film, resin or fiber, its physical properties are inferior and cannot be used.
- the modifier content of the modifier-containing thermoplastic resin used in the present invention can be appropriately selected according to the type of the resin, the type of the modifier, and the target quality of the resin composition.
- the preferred range is from 0.01 to 70% by weight based on the total weight of the thermoplastic resin containing the modifier.
- a particularly high degree of partitioning / mixing effect is observed in a polyester resin which is known to cause a chemical redistribution reaction between the molecular chains of a thermoplastic resin.
- copolymerized polyester is suitably used for randomizing the modifier by a redistribution reaction.
- thermoplastic resin composition in the method of the present invention, as described above, it is possible to produce a modified thermoplastic resin composition while maintaining extremely high dispersibility of various modifiers, and it is possible to prevent aging spots. And the resulting reforming heat Plastic resin compositions also have high uniform dispersibility, which has not been seen before. As a result, a modified thermoplastic resin composition having no large aggregated particles or foreign matter due to thermal decomposition can be obtained.
- the modified thermoplastic resin composition thus obtained is obtained by laminating two 240 mesh mesh screen filters having an inner diameter of 64 mm ⁇ , and melting the thermoplastic resin or the melting point of the modified thermoplastic resin.
- the filtration pressure rise rate is 10 kg / cm 2 / h or less when filtering at a filtration rate of 33.3 g Z at any temperature between 20 ° C and 100 ° C, which is the melting point. And exhibit extremely high uniform dispersibility.
- the modified polyester resin is filtered at a temperature of 290 ° C, the filtration pressure rise rate is 10 kg / cm 2 / h or less, particularly preferably less than 5 kg / cm 2 Zh. It shows excellent and high uniform dispersibility.
- the modified thermoplastic resin composition of the present invention exerts its effect particularly in the case of a polyester resin capable of obtaining a high dispersion effect by a redistribution reaction.
- the polyester composition obtained by the method of the present invention which contains particles and a non-copolymerizing modifier in the base polyester polymer line, and the polyester in which the modifier is copolymerized, are the modifier. Since the resin is highly dispersed in the resin, a composition having less resin pressure fluctuation and quality unevenness in the process when molded into a fiber or a film can be obtained.
- FIGS. 1 and 2 illustrate a dynamic mixing apparatus used in the present invention.
- 1 is a polymer inlet
- 2 is a polymer outlet
- 3 is a double helical ribbon blade
- 4 is a double-moment paddle blade.
- the stirring method for the double-ribbon ribbon blade 3 any of a lifting method and a lifting method can be used.
- 5 Is a drive shaft for driving the stirring blade by external power.
- reference numeral 6 denotes an extruder for melting the thermoplastic resin
- reference numeral 7 denotes a line for dispensing the molten thermoplastic resin.
- a thermoplastic resin containing a modifying agent is introduced from the inlet 9 of the kneading extruder 8 and added to the delivery line 7.
- the base thermoplastic resin and the added thermoplastic resin containing the modifier are sent to the Static Mixer 10, where the polymer flux is repeatedly divided and mixed in a direction perpendicular to the resin flow. .
- the polymer mixture that has passed through the static mixer 10 in this way is then sent to the dynamic mixing device 11.
- stirring is performed by a stirring blade provided to be connected to the stirring drive shaft 5 shown in FIG. 1, and the film forming process and the Z or direct spinning process 12 and the chip forming process 13 are performed.
- Sent Sent.
- FIG. 4 shows another embodiment of the present invention, in which 14 is the last tank of the continuous polymerization, 15 is the entrance to the polymerization tank, and 16 is the discharge line of the polymer after polymerization. 17 is a vacuum system.
- the modifying agent-containing thermoplastic resin is charged into the kneading extruder shown in 8 from the inlet 9 of the kneading extruder, and the polymer is discharged to the line 16.
- the base thermoplastic resin and the added thermoplastic resin containing the modifier are sent to the Static Mixer 10, where the polymer flux is divided repeatedly in a plane perpendicular to the flow direction. And uniformly mixed.
- the reformed polymer that has passed through the static mixer 10 is sent to the dynamic mixing device 11.
- stirring is performed by a stirring blade provided in connection with the stirring drive unit 5 shown in FIG. 1, and a direct film forming and / or direct spinning process 12 and a chip forming process are performed. Sent to 1 3 etc.
- FIG. 5 is an example of an embodiment of the present invention, and is an example in which the example of FIG. 4 is more labor-saving.
- 14 is the final tank for continuous polymerization
- 15 is the polymerization
- the entrance to the tank, 16 is a line for discharging the polymer after polymerization.
- a part of the base polymer discharged from the discharge line 16 is sent to the kneading extruder 18 as part of a side stream 20.
- the modifier-containing polyester is charged into the kneading extruder 18 through the inlet 19 or the additive is added to prepare the additive-containing polyester in the kneading extruder 18. .
- the modifier-containing polyester prepared in the kneading extruder 18 is added again to the base polymer line 16 and subjected to the same distribution mixing as shown in FIG. Alternatively, it is sent directly to the spinning process 12 and chipping process 13.
- 6 to 13 are explanatory views of still another embodiment of the method of the present invention.
- 21 is a static mixer, which is different from the static mixer 10 provided in that the number of resin divisions and / or the type of division is different in the plane perpendicular to the polymer flow direction. It is a quick mixer.
- the dynamic mixing device 22 is a dynamic mixing device having a different agitation type, a tank shape, or a liquid depth from the separately provided dynamic mixing device 11.
- FIGS. 14 to 16 show another embodiment of the present invention, in which 14 is the last tank of continuous polymerization, 15 is the entrance to the polymerization tank, and 16 is the polymer that has been polymerized. This is the payout line. 17 is a vacuum system.
- the modifying agent-containing thermoplastic resin is introduced into the kneading extruder indicated by 8 from the inlet 9 of the kneading extruder and added to the polymer dispensing line 16.
- the kneading extruder 23 may be used in combination.
- the base thermoplastic resin and the modifier-containing thermoplastic resin are sent to the static mixer 10 and distributed and mixed by repeating division in a plane perpendicular to the polymer flow direction. Are combined. Then, the modified polymer having passed through the static mixer 10 is sent to a twin-screw kneading extruder 25 having a vent 26. Then, after kneading with the vented twin-screw kneading extruder 25, it is sent to a direct film forming and Z or direct spinning step 12, a chip forming step 13 and the like.
- FIG. 17 shows still another embodiment of the present invention.
- 14 is the last tank of the continuous polymerization
- 15 is the entrance to the polymerization tank
- 16 is the discharge line of the polymer whose polymerization has been completed.
- 17 is a vacuum system.
- the payout line 16 is further divided into four rows of lines indicated by 27, 29, 31 and 37, respectively. In each of the four rows, the payout lines 27, 29 and 31 are provided with kneading extruders 8, 23 and 32 on each line. Further, the dispensing line 37 is provided with two kneading extruders 38 and 40.
- the thermoplastic resin containing the modifier is dispensed from the kneading extruders 8, 23, 32, 38 and 40 to the respective payout lines 27, 29, 31 and 3 to 7 respectively.
- Each payout line 27, 29, 31 and 37 is provided with a static mixer 10, 21, 34 and 42 respectively, and a complete mixing tank 11, 22, 3 5 and 4 3 units are provided.
- the static mixers Kenics type static mixers (the number of divided elements is 20 elements) were used for those indicated by 10, 34 and 42.
- a through-type static mixer (having 18 divided elements) was used.
- a refining agent having an intrinsic viscosity (Intrinsic Viscosity) of 0.65 obtained through an esterification reaction and a predetermined polycondensation reaction using terephthalic acid and ethylene glycol as raw materials.
- Polyethylene terephthalate, which was not included, was supplied as a base polymer to four rows of payout lines 2722931 and 37 at a rate of 150811. At that time, the temperature of each base polymer was kept at 285 ° C.
- a base chip and titanium oxide are supplied to a twin-screw kneading extruder, and a master tube of polyethylene terephthalate containing 50% of titanium oxide having an average particle diameter of 0.35 im (specifically) A viscosity of 0 • 49) was prepared.
- a masterbatch prepared by copolymerizing 8 mol% of 5-sodium sulfonic acid in a separate batch reactor was prepared.
- the masterbatch was not added to the payout line 27, and a straight polymer was obtained as it was.
- a titanium oxide-containing master coat was added at 0.91 kg Zh.
- a master batch containing titanium oxide was added at 7.9 kg / h.
- Discharge line 37 contains extruders 38 and 40 containing 7.1 kg / h of titanium oxide containing master and 21.4 kg / h of masterbatch containing 5% sodium sulfoisophtalic acid. Respectively.
- Grade 1 The number of particles exceeding 5.0 m is less than 5 particles / mm 2
- Grade 2 The number of particles exceeding 5.0 ⁇ m is 5 to 10 particles / mm 2
- Grade 3 The number of particles exceeding 5.0 m exceeds 10 Zmm 2 Note that only special grade and grade 1 are available for practical use.
- a polymer fixed-quantity feeder is attached to the exit side of the molten polymer of the small single-screw screw-type kneading extruder of the direct spinning device, and a 240 mm mesh wire mesh filter with an inner diameter of 64 mm0 is attached to the exit side.
- the polymer is controlled to a constant temperature of either the melting temperature or the plasticization temperature of 20 ° C or more and 100 ° C or less,
- the polymer is continuously filtered at a rate of 33.3 g per minute for 10 hours.
- the average value of the pressure rise value on the filter inlet side at this time is defined as the filtration pressure rise speed.
- the amount of particles added to the polymer to be filtered should be 0.3% by weight.
- Filtration pressure rise rate is 5 kg / cm 2 or less per hour
- Grade 1 Filtration pressure rise rate is 5 to 1 O kg gcm per hour
- Grade 2 Filtration pressure rise rate is 120 kg / cm 2 per hour.
- Grade 3 Filtration pressure rise rate is 20 kg / cm 2 or more per hour.
- polyester (A) dilute with polyester (A) so that the amount of particles in the polyester becomes 0.3% by weight, and then embed the polyester extruded with a small-shaft screw-type extruder in epoxy resin. Then, the section is cut with a microtome, and the cut surface is observed with a scanning electron microscope (magnification: 50,000 to 10,000). At that time, the linear distance between the particles of 30 sets of two adjacent particles is measured, and the average value, standard deviation, and coefficient of variation are determined, and the following judgment is made.
- the coefficient of variation is less than 0.05.
- Grade 1 The coefficient of variation is 0.05 to 0.1.
- Class 2 The coefficient of variation is from 0.1 to 0.2.
- Class 3 The coefficient of variation is 0.2 or more.
- the polymer discharged as a product is chip-sampled to measure the content of the modifier, and the average value of the 50 measured values, standard Determine the deviation and coefficient of variation and make the following judgment.
- the coefficient of variation is less than 0.05.
- Grade 1 The coefficient of variation is from 0.05 to 0.1.
- Grade 2 The coefficient of variation is from 0.1 to 0.2.
- Class 3 The coefficient of variation is 0 2 or more. Only the special grade and the first grade are put to practical use.
- a polyethylene terephthalate chip having an intrinsic viscosity of 0.65 which has undergone an esterification reaction and a predetermined polycondensation reaction using terephthalic acid and ethylene glycol as raw materials, is produced in a conventional manner. After drying, it was supplied to a kneading extruder 6 at a rate of 900 kg Zh. At this time, the temperature of the base polymer was kept at 285 ° C. Separately, a base chip and titanium oxide having an average particle diameter of 0.35 am are supplied to a twin-screw kneading extruder (not shown), and a polyethylene terephthalate containing titanium oxide at 25% by weight is supplied.
- a master stick (intrinsic viscosity: 0.54) was prepared and added to the transfer line 7 through the kneading extruder 8 at a rate of 10 Okg / h. Thereafter, the mixture is distributed and mixed through a Kenics-type static mixer 10 having 20 elements, and a complete mixing tank 1 equipped with a double-ribbon ribbon blade 3 shown in FIG. Sent to 1 At that time, the stirring was performed in the upward direction, and the rotation speed was set to 15 rpm. The residence time of the resin was set to 12 minutes. In the modified poly (ethylene terephthalate) resin thus obtained, 100 kg / h was directly supplied to the spinning step 12 and the remainder was supplied to the chipping step 13 o
- terephthalic acid and ethyl alcohol are used as raw materials to undergo an esterification reaction and a predetermined polycondensation reaction.
- a base chip and titanium oxide are supplied to the twin-screw kneading extruder 8 from the inlet 9, and a polyethylene terephthalate containing 25% of titanium oxide having an average particle size of 0.35 m is supplied from the inlet 9.
- a single master batch (having a specific viscosity of 0.554) was prepared and discharged through the twin-screw kneading extruder 8 at a rate of 10 O kg / h and added to the line 16. Thereafter, the reformed polymer was distributed and mixed through a Kenics-type static mixer 10 (the number of splitting elements was 20 elements), and further, the double-helical ribbon shown in FIG. It was sent to the complete mixing tank 11 equipped with the wing 3.
- Table 1 shows the evaluation results obtained in this way.
- the same base polymer as in Example 2 was dispensed at a rate of 975 kg / h and dispensed to line 16, of which the size was reduced by the dispensing line 16.
- the base polymer is extracted at a rate of 75 kg / h as a stream 20 and ventilated at a rate of 25 kg / h with titanium oxide powder having an average particle diameter of 0.362 m.
- titanium oxide powder having an average particle diameter of 0.362 m.
- the twin-screw kneading extruder 18 needs The disk was mounted and the screw rotation speed was set to 400 rpm.
- a modifier-containing thermoplastic resin composition containing 25% by weight of a titanium oxide pigment was prepared, and while maintaining the temperature at 285 ° C., the above-described twin-screw kneading and extrusion with a vent was performed. Dispensed through machine 18 and added to line 16 base polymer. The other conditions were the same as in Example 2.
- Table 1 shows the evaluation results obtained at this time.
- the base polymer is withdrawn at a rate of 25 kg / h from the dispensing line 16 and supplied to a twin-screw kneading extruder 18 with a vent 18 where the average particle size 0.34 zm of titanium oxide powder was supplied at a rate of 25 kg Zh to perform kneading, and the obtained composition was added to the base polymer of the dispensing line 16.
- the other conditions were the same as in Example 2.
- Table 1 shows the evaluation results obtained at this time.
- Example 2 was carried out under the same conditions as in Example 2 except that the addition amount of the titanium oxide-containing master batch was 11 kg / h.
- Table 1 shows the evaluation results obtained at this time.
- Example 3 a base polymer was withdrawn at a rate of 12 kgZh as a side stream, and 3 kg Zh of titanium oxide powder was fed to a twin-screw kneading extruder 18 with a vent. The procedure was performed under the same conditions as in Example 3 except that they were added in a ratio.
- Table 1 shows the evaluation results obtained at this time.
- Example 3 the base polymer was extracted at a rate of 3 kgh. Then, the mixture is supplied to a twin-screw kneading extruder 18 with a vent, where titanium oxide powder is supplied at a rate of 3 kg Zh for kneading, and this composition is discharged through a nozzle. The procedure was carried out under the same conditions as in Example 3 except that it was added to the base polymer of No. 16.
- Table 1 shows the evaluation results obtained at this time.
- Table 1 shows the evaluation results obtained at this time.
- the rotation was performed under the same conditions as in Example 2 except that the rotation speed of the stirring blade of the dynamic kneading device 11 was set to 9 rpm and the residence time was set to 16 minutes.
- Table 1 shows the evaluation results obtained at this time.
- the payout line 16 was discharged at a rate of 675 kg Zh. Then, a master batch containing titanium oxide was added to the discharge line 16 at a rate of 75 kg / h, and then passed through a dynamic mixing device 11. At that time, the same operation as in Example 2 was performed except that the rotation speed of the stirring blade of the dynamic mixing device 11 was set at 10 rpm and the residence time was set at 16 minutes.
- Table 1 shows the evaluation results obtained at this time.
- Example 2 the same procedure as in Example 2 was carried out except that the stirring blade of the dynamic mixing device 11 was replaced with the double motion paddle blade 4 shown in FIG.
- the rotation speed of the stirring blade was set at 15 rpm, and the average residence time of the polymer in the dynamic mixer 11 was set at 10 minutes.
- Table 1 shows the evaluation results obtained at this time.
- the masterbatch was added to the base polymer discharge line 16, passed through the dynamic mixing device 11 first, and then passed through the static mixing device 10. Other than that, the same conditions as in Example 2 were used.
- Table 1 shows the evaluation results obtained at this time.
- Example 1 is the same as Example 1 except that 1 and a Kenics type static mixer 10 having 20 elements were connected in series and then passed through the dynamic mixer 11. Performed under the same conditions as in 2.
- Table 1 shows the evaluation results obtained at this time.
- the masterbatch was added to the base polymer withdrawal line 16 and the dynamic mixing devices 11 and 2 were set with an average residence time of 9 minutes and 12 minutes, respectively. After passing through 1, the test was carried out under the same conditions as in Example 2 except that it passed through a Kenics-type static mixer 10 having 20 elements.
- Table 1 shows the evaluation results obtained at this time.
- a Kenics-type static mixer 10 having 20 elements is divided. After passing through, the same as in Example 2 except that they were connected in series and passed through dynamic mixing devices 11 and 22 each having an average residence time of 9 minutes and 12 minutes. The test was performed under the same conditions.
- Table 1 shows the evaluation results obtained at this time.
- a Kenics-type static mixer 10 with 20 elements is used. Same as Example 1 except that the dynamic mixing device 11 and the mixing device connected in series with the static mixer 22 manufactured by Sulzer, Inc. having 18 elements were used. It carried out on condition of.
- Table 1 shows the evaluation results obtained at this time.
- the residence time was set to 9 minutes.
- a dynamic mixing device 11 a kinetic-type static mixer 10 with 20 elements, and a dynamic mixing device 22 with a residence time of 12 minutes are connected in series. The procedure was performed under the same conditions as in Example 2 except that the connection was made and the reforming polymer was passed through each apparatus.
- Table 1 shows the evaluation results obtained at this time.
- a Kenics static mixer 10 with 20 elements divided in parallel and a through-sizer with 18 elements divided into 18 elements are arranged in parallel. Same as Example 14 except that the reforming polymer was passed through the static mixer 21 and then passed through the same complete mixing tank 11 as in Example 14 as a dynamic mixing device. It was performed under the conditions.
- Table 1 shows the evaluation results obtained at this time.
- a twin-screw kneading extruder 25 with a bent was used as a dynamic mixing device instead of the complete mixing tank 11 in Example 2.
- the screw of the twin-screw kneading extruder 25 with a vent was equipped with a reverse feed segment at two locations to provide a retaining portion.
- the resin temperature in the twin-screw kneading extruder 25 was maintained at 285 ° C., and the screw rotation speed was set at 400 rpm.
- the vent 26 of the twin-screw kneading extruder 25 was connected to a vacuum pump (not shown) and kept at lTorr.
- Table 1 shows the evaluation results obtained at this time.
- the conditions were the same as those in Example 18 except that a twin-screw kneading extruder 25 with a bent was used instead of the complete mixing tank 11.
- a twin-screw kneading extruder with a vent 25 The screen was equipped with reverse feed segments at two locations to provide stagnant sections.
- the resin temperature in the twin-screw kneading extruder 25 was kept at 285 ° C., and the screw rotation speed was set at 400 rpm.
- the vent 26 of the twin-screw kneading extruder 25 was connected to a vacuum pump (not shown) and kept at 1 Torr.
- Table 1 shows the evaluation results obtained at this time.
- polyethylene terephthalate was flowed at a rate of 75 O kg / h into the base polymer payout line 16 to remove the modifier-containing thermoplastic resin provided at two locations.
- 50 kg of titanium oxide containing 50% by weight of titanium oxide was added at a rate of 50 kg Zh, and 5-sodium sulfisophthalic acid was added.
- Evaluation was carried out under the same conditions as in Example 22 except that the masterbatch copolymerized at 8 mol% was added at a rate of 200 kg Zh.
- Table 1 shows the evaluation results obtained. Note that “IPS” used in Table 1 indicates “5-sodium sulfeusophthalic acid”.
- the esterification reaction is completed using terephthalic acid and ethylene glycol as raw materials, and then at the end of the polycondensation reaction, polyethylene glycol having a molecular weight of 20000 is used as an antistatic agent. 0.5% based on the acid component and 0.5% dodecylbenzenesulfonic acid based on the acid component.After that, polycondensation is continued and a modifying agent with an intrinsic viscosity of 0.60 is included. A thermoplastic resin composition was obtained.
- the esterification reaction was completed using terephthalic acid and ethylene glycol as raw materials by a continuous polymerization method.
- 90 O kg was dispensed to line 16 using polyethylene terephthalate, which does not contain a modifier with an intrinsic viscosity of 0.65, as a base polymer.
- Zh was dispensed, and the above-mentioned thermoplastic resin composition containing a modifying agent was added to the dispensing line 16 at a rate of 100 kg Zh.
- the temperature of the base polymer was kept at 285 ° C.
- the mixture was distributed and mixed by passing through a static mixer 10 manufactured by Noritake Co., Ltd.
- Table 1 shows the evaluation results obtained at this time.
- the esterification reaction is completed using terephthalic acid and ethylene glycol as raw materials, and then, at the beginning of the polycondensation reaction, trimethyl phosphate and calcium acetate are used as a body-forming agent.
- trimethyl phosphate and calcium acetate are used as a body-forming agent.
- the intrinsic viscosity of 0.65 which has undergone a predetermined polycondensation reaction is determined.
- Polyethylene terephthalate containing no modifier was obtained. And this is the base
- supply 90 O kg Zh to the payout line 16 at a rate of 90 O kg Zh, and pay out the above-mentioned modifier-containing polyethylene terephthalate at a rate of 10 Okg / h. was added to the solution.
- the temperature of the base polymer was kept at 285 ° C.
- the mixture was passed through a Noritake-made sticky mixer 10 having 20 elements and further mixed by a dynamic mixing device 11.
- the rotation speed of the dynamic mixing device 11 was set to 15 rpm, and the residence time was set to 12 minutes.
- the obtained modified polymer was directly supplied to a spinning step 12 at a rate of 500 kg Zh, and the remainder was supplied to a chip forming step 13.
- the chips were subjected to a reflex treatment with a 20% aqueous sodium hydroxide solution for 1 hour to obtain chips in the spinning step.
- the voids formed on the surface of the obtained fiber were evaluated in the same manner as the above-described coarse particles and dispersion of particles in the polyester.
- Table 1 shows the evaluation results obtained at this time.
- TMP-Ca used in Table 1 indicates “composite particles composed of trimethyl phosphate and calcium acetate”.
- the esterification reaction is completed using terephthalic acid and 15 mol% of isophthalic acid and ethylene glycol based on terephthalic acid as raw materials, and then a polycondensation reaction is performed to obtain an intrinsic viscosity of 0.6.
- a thermoplastic resin containing isophthalic acid was obtained.
- the intrinsic viscosity of the mixture obtained through a predetermined polycondensation reaction is 0.6.
- Polyethylene terephthalate containing no modifier was obtained as a base polymer.
- the polymer was supplied to payout line 16 at a rate of 25 O kg Zh.
- the temperature of the base polymer was kept at 285 ° C. So Then, the above-mentioned resin was added to the base polymer at a rate of 25 O kg / h through a kneading extruder 8 to obtain a modified polymer.
- the mixture was passed through the dynamic mixing devices 11 and 22 and further distributed and mixed through a Noritake Static Mixer 10 having 20 elements.
- the modified polymer thus obtained was directly supplied to the spinning step 12 at a rate of 250 kg / h, and the remainder was supplied to the chip forming step 13.
- the dispersibility simultaneously spun fibers were randomly sampled in 0.1 g increments, their melting points were measured, and the dispersion was evaluated based on this variation.
- Table 1 shows the evaluation results obtained at this time.
- IA used in Table 1 indicates “isophthalic acid”.
- a polyester containing 5% by weight of silica particles having an average particle size of 1 Zm was used as a master batch, and the concentration of silica in the final product was 500,000.
- the preparation was carried out under the same conditions as in Example 2 except that it was adjusted to be ppm and added to the dispensing line 16 of the base polymer.
- Table 1 shows the evaluation results obtained at this time.
- nylon 6 after the completion of the polymerization reaction was supplied as a base polymer to the delivery line 16 at a rate of 90 O kg / h. At this time, the temperature of the base polymer was kept at 265 ° C.
- a base chip made of nylon 6 and titanium oxide are supplied to a twin-screw kneading extruder 8, and a master batch made of nylon 6 containing 25% by weight of titanium oxide is prepared. This was discharged through a twin screw extruder 8 at a rate of 10 O kg / h and added to the line 16.
- a Kenic-type static mixer with 20 elements The mixture was distributed and mixed through the mixer 10 and then sent to the complete mixing tank 11 equipped with double helical ribbon blades shown in FIG. At that time, stirring was performed in the upward direction, and the rotation speed was set to 15 rpm. At this time, the residence time of the polymer in the complete mixing tank was 12 minutes.
- the modified polymer thus obtained was directly supplied to the spinning step 12 at a rate of 500 kg / h, and the remainder was subjected to the chip forming step 13.
- Table 1 shows the evaluation results obtained at this time.
- a polypropylene chip is melted at a rate of 90 kg / h and supplied to the base polymer payout line 7, and then a polypropylene containing 5% by weight of talc is used.
- Master-batch was discharged from kneading extruder 8 at a rate of 10 kg Zh and supplied to line 7. At that time, the polymer temperature was kept at 230 ° C.
- the resulting modified polymer was sent directly to the spinning step 12 and the chipping step 13 at a rate of 50 k / h.
- Table 1 shows the evaluation results obtained at this time.
- reference numeral 14 denotes a final tank of continuous polymerization
- 15 denotes an entrance to the polymerization tank
- 16 denotes a line for discharging the polymer after polymerization.
- 17 is a vacuum system.
- the payout line 16 is divided into four parallel lines indicated by 27, 29, 31 and 37, respectively.
- each of the three payout lines 27, 29, and 31 is provided with the extruder containing the thermoplastic resin containing the modifying agent introduced from the respective populations 9, 24, and 33. Supplied by 8, 23 and 32 respectively.
- another extruder line 37 is supplied with a thermoplastic resin containing a modifier from two extruders 38 and 40 through inlets 39 and 41, respectively. .
- the payout lines 27, 29, 31 and 37 are provided with static mixers 10, 21, 34 and 42, respectively.
- complete mixing tanks 11, 22, 35, and 43 are provided in series with the static mixers 10, 21, 34, and 42 respectively.
- the static mixers 10, 34, and 42 use a Kenics type static mixer having 20 elements, and the static mixer 21 has the number of divided elements. Used an 18-element static through-type static mixer.
- the complete mixing tanks 11, 35 and 43 used lift-up double-helical ribbon blades, and the complete mixing tank 22 used double-motion paddle blades. At that time, the rotation speed of each of these stirring blades was maintained at 12 rpm, and the residence time was set at 12 minutes.
- a poly (ethylene terephthalate) containing no modifier having a specific viscosity of 0.65 is obtained through an esterification reaction and a predetermined polycondensation reaction using terephthalic acid and ethylene glycol as raw materials.
- the rate was supplied as base polymer to four rows of payout lines 27, 29, 31 and 37 at a rate of 150 kg Zh each. At that time, the temperature of each of the polymers was kept at 285 ° C.
- the base chip and titanium oxide are supplied to a twin-screw kneading extruder, and a master batch of polyethylene terephthalate containing 50% by weight of titanium oxide having an average particle diameter of 0.35 ⁇ m ( An intrinsic viscosity of 0.49) was prepared.
- a master batch was prepared by copolymerizing 8-mol% sodium sulfoisphthalic acid with 8 mol% in another batch reactor.
- the first row, line 27, obtained a straight polymer without adding a masterbatch.
- Master oxide titanium oxide was added to line 29 in the second row at a rate of 0.91 kg / h.
- a master batch of titanium oxide was added in order of 7.9 kg Zh from the additive nozzle provided.
- Line 4 37 in the fourth column contains a master of titanium oxide at a rate of 7.1 kg Zh and a master of 5— sodium sulfoisphthalic acid at 21.4. kZh was added at the rate.
- the modified thermoplastic resin composition obtained in lines 27, 29, 31 and 37 in each row is directly spun into a spinning step 12 or a chipping step 28. 30, 36 and 45. Then, the coarse particles, dispersibility, change in kneading degree over time, and the degree of increase in filtration pressure during spinning were determined for each of the chips.
- Table 1 shows the evaluation results obtained at this time. Note that “IPS” used in Table 1 indicates “5-sodium sulfeusophthalic acid”.
- Example 2 The same conditions as in Example 2 except that the mixing operation was performed only with the static mixing device 10 in the process illustrated in FIG. 18 in which the dynamic mixing device was omitted from the process illustrated in FIG. 4 I went in.
- Table 1 shows the evaluation results obtained at this time.
- Example 25 Same as Example 25 except that the mixing operation was performed only with the static mixing device 10 in the process illustrated in FIG. 18 in which the dynamic mixing device 11 was omitted from the process illustrated in FIG. I went under the conditions.
- Table 1 shows the evaluation results obtained at this time.
- TMP—Ca used in Table 1 indicates “composite particles composed of trimethylphosphoric acid and calcium acetate”.
- Table 1 shows the obtained evaluation results.
- Comparative Examples 1 to 4 were evaluated in the evaluation items such as the dispersibility of the modifier, the change over time in the degree of mixing, and the rate of increase in the filtration pressure. All were inferior to 0. table 1
- thermoplastic resin containing a modifier is added to a discharge line of a base polymer obtained by continuous polymerization of a thermoplastic resin
- a dynamic mixer having a static mixing device and a stirring blade is provided.
- a method for continuously producing a thermoplastic resin through a mechanical mixing device is provided.
- the resin composition thus obtained has excellent moldability when molding into fibers, films, and resin molded products, and the product quality as fibers, films, and resin molded products. It has an extremely remarkable effect of being excellent. According to the present invention, such good processes and quality can be easily performed in a continuous polymerization dispensing line, and it is possible to dramatically promote the production of a wide variety of thermoplastic resins.
- a thermoplastic resin composition in which the agent is highly dispersed can be obtained.
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Processes Of Treating Macromolecular Substances (AREA)
- Compositions Of Macromolecular Compounds (AREA)
- Extrusion Moulding Of Plastics Or The Like (AREA)
- Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR1019997006186A KR100602816B1 (ko) | 1997-11-10 | 1998-11-09 | 개질 열가소성 수지 조성물 및 그 제조 방법 |
CA002277129A CA2277129C (en) | 1997-11-10 | 1998-11-09 | Modified thermoplastic resin composition and method of producing the same |
US09/331,883 US6281278B1 (en) | 1997-11-10 | 1998-11-09 | Modified thermoplastic resin composition and method of producing the same |
EP98951742A EP0952173B1 (en) | 1997-11-10 | 1998-11-09 | Process for producing a modified thermoplastic resin composition |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP9/307362 | 1997-11-10 | ||
JP9307362A JPH11172082A (ja) | 1997-11-10 | 1997-11-10 | 改質ポリエステルの連続製造方法 |
Publications (1)
Publication Number | Publication Date |
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WO1999024495A1 true WO1999024495A1 (en) | 1999-05-20 |
Family
ID=17968180
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1998/005035 WO1999024495A1 (en) | 1997-11-10 | 1998-11-09 | Modified thermoplastic resin composition and method of producing the same |
Country Status (9)
Country | Link |
---|---|
US (1) | US6281278B1 (ja) |
EP (1) | EP0952173B1 (ja) |
JP (1) | JPH11172082A (ja) |
KR (1) | KR100602816B1 (ja) |
CN (1) | CN1178975C (ja) |
CA (1) | CA2277129C (ja) |
ID (1) | ID21931A (ja) |
TW (1) | TW400346B (ja) |
WO (1) | WO1999024495A1 (ja) |
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JP2007512982A (ja) * | 2003-12-06 | 2007-05-24 | バイエル・マテリアルサイエンス・アクチェンゲゼルシャフト | ポリマーメルトに添加剤を導入する方法 |
WO2010097873A1 (ja) * | 2009-02-27 | 2010-09-02 | 三菱重工業株式会社 | 混合装置及びシーラント |
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- 1998-11-09 ID IDW990658A patent/ID21931A/id unknown
- 1998-11-09 CN CNB98803218XA patent/CN1178975C/zh not_active Expired - Fee Related
- 1998-11-09 US US09/331,883 patent/US6281278B1/en not_active Expired - Lifetime
- 1998-11-09 TW TW087118623A patent/TW400346B/zh not_active IP Right Cessation
- 1998-11-09 EP EP98951742A patent/EP0952173B1/en not_active Expired - Lifetime
- 1998-11-09 CA CA002277129A patent/CA2277129C/en not_active Expired - Fee Related
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JP2007512982A (ja) * | 2003-12-06 | 2007-05-24 | バイエル・マテリアルサイエンス・アクチェンゲゼルシャフト | ポリマーメルトに添加剤を導入する方法 |
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Also Published As
Publication number | Publication date |
---|---|
KR20000069971A (ko) | 2000-11-25 |
CN1250455A (zh) | 2000-04-12 |
US6281278B1 (en) | 2001-08-28 |
CA2277129C (en) | 2008-01-22 |
EP0952173B1 (en) | 2012-03-14 |
CN1178975C (zh) | 2004-12-08 |
CA2277129A1 (en) | 1999-05-20 |
KR100602816B1 (ko) | 2006-07-19 |
EP0952173A1 (en) | 1999-10-27 |
JPH11172082A (ja) | 1999-06-29 |
ID21931A (id) | 1999-08-12 |
TW400346B (en) | 2000-08-01 |
EP0952173A4 (en) | 2003-09-03 |
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