CN203794824U - Production system capable of continuously producing copolymerized antistatic cationic polyester - Google Patents
Production system capable of continuously producing copolymerized antistatic cationic polyester Download PDFInfo
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- CN203794824U CN203794824U CN201420056096.9U CN201420056096U CN203794824U CN 203794824 U CN203794824 U CN 203794824U CN 201420056096 U CN201420056096 U CN 201420056096U CN 203794824 U CN203794824 U CN 203794824U
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- monomer
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- static inhibitor
- charging tank
- esterifier
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- 229920000728 polyester Polymers 0.000 title claims abstract description 34
- 125000002091 cationic group Chemical group 0.000 title claims abstract description 27
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 25
- 239000000178 monomer Substances 0.000 claims abstract description 128
- 239000006185 dispersion Substances 0.000 claims abstract description 42
- 230000032050 esterification Effects 0.000 claims abstract description 42
- 238000005886 esterification reaction Methods 0.000 claims abstract description 42
- 238000000227 grinding Methods 0.000 claims abstract description 37
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 230000003068 static effect Effects 0.000 claims description 106
- 239000003112 inhibitor Substances 0.000 claims description 103
- 238000009826 distribution Methods 0.000 claims description 20
- 238000010438 heat treatment Methods 0.000 claims description 16
- 238000002360 preparation method Methods 0.000 claims description 16
- 150000002148 esters Chemical class 0.000 claims description 15
- 238000010790 dilution Methods 0.000 claims description 11
- 239000012895 dilution Substances 0.000 claims description 11
- 239000003795 chemical substances by application Substances 0.000 claims description 10
- 239000002002 slurry Substances 0.000 claims description 8
- 238000009987 spinning Methods 0.000 claims description 7
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 238000013329 compounding Methods 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 4
- 125000004185 ester group Chemical group 0.000 claims 6
- 238000010924 continuous production Methods 0.000 abstract description 6
- 239000000835 fiber Substances 0.000 abstract description 5
- 239000002216 antistatic agent Substances 0.000 abstract 4
- 238000005809 transesterification reaction Methods 0.000 abstract 2
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 27
- 239000000203 mixture Substances 0.000 description 14
- 238000000034 method Methods 0.000 description 12
- XOLBLPGZBRYERU-UHFFFAOYSA-N tin dioxide Chemical compound O=[Sn]=O XOLBLPGZBRYERU-UHFFFAOYSA-N 0.000 description 8
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 6
- -1 polyoxyethylene Polymers 0.000 description 6
- 229920003171 Poly (ethylene oxide) Polymers 0.000 description 5
- 229910044991 metal oxide Inorganic materials 0.000 description 5
- 238000000498 ball milling Methods 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 238000006068 polycondensation reaction Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- QPKOBORKPHRBPS-UHFFFAOYSA-N bis(2-hydroxyethyl) terephthalate Chemical compound OCCOC(=O)C1=CC=C(C(=O)OCCO)C=C1 QPKOBORKPHRBPS-UHFFFAOYSA-N 0.000 description 2
- 238000007334 copolymerization reaction Methods 0.000 description 2
- 239000003085 diluting agent Substances 0.000 description 2
- 238000010036 direct spinning Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 230000002045 lasting effect Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 229910001887 tin oxide Inorganic materials 0.000 description 2
- 208000033999 Device damage Diseases 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- QQVIHTHCMHWDBS-UHFFFAOYSA-N isophthalic acid Chemical compound OC(=O)C1=CC=CC(C(O)=O)=C1 QQVIHTHCMHWDBS-UHFFFAOYSA-N 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- 239000003607 modifier Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- LIGAHKBUWHFCIT-UHFFFAOYSA-M sodium benzenesulfonate dimethyl benzene-1,3-dicarboxylate Chemical compound [Na+].[O-]S(=O)(=O)c1ccccc1.COC(=O)c1cccc(c1)C(=O)OC LIGAHKBUWHFCIT-UHFFFAOYSA-M 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000004381 surface treatment Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Landscapes
- Polyesters Or Polycarbonates (AREA)
Abstract
The utility model relates to a production system capable of continuously producing copolymerized antistatic cationic polyester. The production system comprises an esterification system, wherein the esterification system at least comprises a first esterification reactor and a second esterification reactor which are connected sequentially, the esterification system further comprises an antistatic agent grinding and dispersing system, a third monomer transesterification system and a fourth monomer configuration system, an antistatic agent dispersion liquid outlet of the antistatic agent grinding and dispersing system is connected with an antistatic agent dispersion liquid inlet of the second esterification reactor, a third monomer outlet of the third monomer transesterification system is connected with a third monomer inlet of the second esterification reactor, and a fourth monomer outlet of the fourth monomer configuration system is connected with a fourth monomer inlet of the second esterification reactor. The production system has the advantages that the continuous production of the copolymerized antistatic cationic polyester is realized, and fibers can be spun directly.
Description
Technical field
The utility model relates to a kind of production system of polyester, relates in particular to a kind of production system that can produce continuously the antistatic cationic polyester of copoly type.
Background technology
Antistatic cationic polyester is important functional polyester, and along with the static hazards such as static discharge sets off an explosion, electron device damage are increasing, the demand of antistatic polyester will sharply increase.The preparation method of antistatic polyester mainly contains blend, copolymerization and surface treatment etc., surface preparation low production cost, but antistatic effect is difficult to permanent preservation, and washing resistance performance is poor, and in low-humidity environment, does not show antistatic property; The antistatic fibre static resistance that blending method is produced is relatively lasting, and selectable have the inorganic of conductivity or organic materials kind is more, but compare the large usage quantity of static inhibitor with copolymerization method, also can affect material body and surface property.
There is no now the antistatic cationic polyester of continuous industrial production both at home and abroad; Continuous industrial production antistatic polyester be take blending method extrusion molten continuous processing or surface preparation technical process substantially as main, and the former static inhibitor large usage quantity, antistatic fibre spinning properties are poor, and product cost is high, unstable product quality; And the latter's antistatic property is not lasting, wash resistant not.
Utility model content
The problem existing in order to solve prior art, the purpose of this utility model is to provide a kind of production system that can produce continuously the antistatic cationic polyester of copoly type, can realize the antistatic cationic polyester of copoly type continuous production and can Direct Spinning fiber.
The technical solution of the utility model:
A kind of production system that can produce continuously the antistatic cationic polyester of copoly type, comprise esterification system, described esterification system at least comprises the first esterifier and the second esterifier connecting successively, also comprise static inhibitor grinding distribution system, the 3rd monomeric ester exchange system and the 4th monomer configuration-system, the static inhibitor dispersion liquid outlet of described static inhibitor grinding distribution system is connected with the static inhibitor dispersion liquid entrance of described the second esterifier, the 3rd monomer outlet of described the 3rd monomeric ester exchange system is connected with the 3rd monomer entrance of described the second esterifier, the 4th monomer outlet of described the 4th monomer configuration-system is connected with the 4th monomer entrance of described the second esterifier.
Preferably, described static inhibitor grinding distribution system comprises static inhibitor dispersion slot, grinding system, static inhibitor dilution trap, whizzer and the static inhibitor dispersion liquid charging tank connecting successively, described static inhibitor dispersion slot is provided with feed(raw material)inlet, described static inhibitor dispersion liquid charging tank is provided with the outlet of static inhibitor dispersion liquid, its outlet of static inhibitor dispersion liquid as described static inhibitor grinding distribution system.
Further, described grinding system can comprise shredder and static inhibitor circulation groove, the loop exit of described shredder can be connected with the loop head of described static inhibitor circulation groove, and the loop exit of described static inhibitor circulation groove can be connected with the loop head of described shredder.
Preferably, described the 3rd monomeric ester exchange system comprises the 3rd monomeric ester exchange reactor and the 3rd monomer charging tank, the outlet of described the 3rd monomeric ester exchange reactor is connected with the entrance of described the 3rd monomer charging tank, and the outlet of described the 3rd monomer charging tank is as the 3rd monomer outlet of described the 3rd monomeric ester permutoid reaction system.
Preferably, described the 4th monomer compounding system comprises the 4th molten monomer groove and the 4th monomer charging tank, described the 4th molten monomer groove outlet is connected with described the 4th monomer charging tank entrance, outlet on described the 4th monomer charging tank is as the 4th monomer outlet of described the 4th monomer configuration-system, and the outlet of described the 4th monomer charging tank is also connected with described the 4th molten monomer groove entrance.
Conventionally, a part for pipeline between described the 4th monomer charging tank outlet and the 4th monomer entrance of described the second esterifier and a part for the pipeline between described the 4th monomer charging tank outlet and described the 4th molten monomer groove entrance can share same segment pipe, on this section of described pipeline, charging pump are installed;
Further, pipeline between described the 4th monomer charging tank and described the 4th molten monomer groove and the pipeline between the 4th monomer charging tank and described the second esterifier all can be furnished with hot steam pipeline, described the 4th molten monomer groove inside can be provided with heating medium for heating coil pipe, its outside can be provided with heating agent chuck, and the outside of described the 4th monomer charging tank can be provided with heating agent chuck.
Preferably, described the second esterifier is horizontal esterifier, its inner chamber is divided into the first chamber, the second chamber and the 3rd chamber from left to right, in each chamber, be equipped with whipping appts, the static inhibitor dispersion liquid outlet of described static inhibitor grinding distribution system connects described the first chamber, the 3rd monomer outlet of described the 3rd monomeric ester exchange system connects described the first chamber, and the 4th monomer outlet of described the 4th monomer configuration-system connects described the second chamber.
Conventionally, the utility model can also comprise and connects successively Prepolycondensating reactor and finishing reactor, the esterification outlet of described the second esterification device can connect the esterification entrance of described Prepolycondensating reactor, and described Prepolycondensating reactor and described finishing reactor all can dispose corresponding vacuum system and temperature controlling system.
Conventionally, the utility model can also comprise slurry preparation groove, and the esterification outlet of described slurry preparation groove can connect the esterification entrance of described the first esterifier.
Conventionally, the esterification of described finishing reactor outlet can connect slice systems and/or spinning system by pipeline.
The beneficial effects of the utility model:
The 4th monomer prepared by the 3rd monomer that the utility model is prepared the static inhibitor dispersion liquid of being prepared by static inhibitor grinding distribution system, the 3rd monomeric ester exchange system, the 4th monomer compounding system is introduced the second esterifier, again in conjunction with continuous normal polyester production technology and continous way direct spinning technology, the antistatic cationic polyester melt/section of continuous production copoly type and fused mass directly spinning have been realized, in the time of process simplification, production efficiency and benefit have been improved, reduce production cost, stablized quality product.
Accompanying drawing explanation
Fig. 1 is schema of the present utility model;
Fig. 2 is the schema of static inhibitor grinding distribution system;
Fig. 3 is the structural representation of a kind of embodiment of the present utility model.
Embodiment
Referring to Fig. 1 and Fig. 3, the utility model relates to a kind of production system that can produce continuously the antistatic cationic polyester of copoly type, comprise the slurry preparation groove 1, esterification system, Prepolycondensating reactor 4 and the finishing reactor 5 that connect successively, the esterification outlet of described finishing reactor can connect slice systems 6 and/or spinning system 7 by pipeline.
Described esterification system comprises the first esterifier 2 and the second esterifier 3 connecting successively, the esterification outlet of described slurry preparation groove is connected with the esterification entrance of described the first esterification system, and the esterification outlet of described the second esterifier is connected with the esterification entrance of described Prepolycondensating reactor.In practical application, described esterification system can also add other esterifier to realize more multistep esterification as required.
The static inhibitor dispersion liquid entrance of described the second esterifier is connected with static inhibitor grinding distribution system 8, the 3rd monomer entrance of described the second esterifier is connected with the 3rd monomeric ester exchange system, and the 4th monomer entrance of described the second esterifier is connected with the 4th monomer preparation system.
Described the second esterifier is horizontal esterifier, its inner chamber can be divided into the first chamber 31, the second chamber 32 and the 3rd chamber 33 from left to right, in each chamber, be equipped with whipping appts, the static inhibitor dispersion liquid outlet of described static inhibitor grinding distribution system connects described the first chamber, the 3rd monomer outlet of described the 3rd monomeric ester exchange system connects described the first chamber, the 4th monomer outlet of described the 4th monomer configuration-system connects described the second chamber, can also be provided with catalyzer and add entrance on described the second chamber.
Raw material PTA and EG are mixed and made into suspension by process ratio metering, the polycondensation catalyst ethylene glycol solution preparing is metered into described slurry preparation groove from catalyzer charging tank simultaneously, through well-mixed mixture paste, by spiral pump, quantitatively send into esterification system, in addition, can add by needs of production the additive of other purposes; The slurry of sending into the first esterifier fully reacts to esterification yield and reaches more than 90% under certain temperature, pressure, liquid level, is then sent to the second esterifier reaction.
Described static inhibitor dispersion liquid and the 3rd monomer are added to the first chamber of described the second esterifier, the additives such as the 4th monomer and titanium dioxide 9 inject the second chamber of described the second esterifier, and control cooperatively interacting of described the second esterifier three chamber temps, the product being conducive to after the first esterification refines and is decomposed into BHET monomer in the first chamber of described the second esterifier, make static inhibitor (nanometer antimony-doped stannic oxide ATO), thereby cation-modified the 3rd monomer and polyester monocase BHET can full and uniform mixing reach static inhibitor and cation modifier is uniformly distributed in product.Material in three chambers of described the second esterifier under different temperature and liquid level condition fully after stirring reaction (esterification yield is not less than 96.5%) be sent to polycondensation system (Prepolycondensating reactor and finishing reactor), under certain temperature and vacuum condition, there is polycondensation.
Wherein, the working pressure scope in described the second esterifier can be for 0-20kPa (G), as 0 kPa(G), 5 kPa(G), 10 kPa(G), 15 kPa(G) or 20 kPa(G); Operating temperature range in described the first chamber can be 240-250 ℃, and as 240 ℃, 245 ℃ or 250 ℃, reaction time can be 15-30min, as 15min, 25min or 30min; Operating temperature range in described the second chamber can be 230-245 ℃, and as 230 ℃, 235 ℃, 240 ℃ or 245 ℃, reaction time can be 20-40min, as 20min, 25min, 30min, 35min or 40min; Operating temperature range in the 3rd chamber can be 250-265 ℃, and as 250 ℃, 255 ℃ or 265 ℃, institute's reaction time can be 30-50min, as 30min, 35min, 40min, 45min or 50min.
The preparation of static inhibitor dispersion liquid:
Referring to Fig. 2, described static inhibitor grinding distribution system at least comprises shredder and whizzer.Nano-metal-oxide static inhibitor (nano stibium doped tin oxide ATO), dispersion agent polyoxyethylene glycol and ethylene glycol mix and blend directly can be sent into shredder and carry out ball milling, send into whizzer separation, the less static inhibitor of particle diameter that separation is obtained is sent into the second esterifier again.
In addition, described static inhibitor grinding distribution system also can comprise static inhibitor dispersion slot, grinding system, static inhibitor dilution trap, whizzer and the static inhibitor dispersion liquid charging tank connecting successively, described static inhibitor dispersion slot is provided with feed(raw material)inlet, described static inhibitor dispersion liquid charging tank is provided with static inhibitor outlet, its outlet of static inhibitor dispersion liquid as described static inhibitor grinding distribution system.By nano-metal-oxide static inhibitor (nano stibium doped tin oxide ATO), dispersion agent polyoxyethylene glycol and ethylene glycol mix and blend in static inhibitor dispersion slot, static inhibitor mixture after stirring is sent into grinding system and is carried out ball milling, dilutes the static inhibitor mixture after ball milling is sent into static inhibitor dilution trap, again the mixture after dilution is sent into whizzer centrifugation, filtration, the static inhibitor dispersion liquid with the less static inhibitor of particle diameter that separation obtains, and sent into the second esterifier.
Described grinding system comprises shredder and static inhibitor circulation groove, and the loop exit of described shredder can be connected with the loop head of described static inhibitor circulation groove, and the loop exit of described static inhibitor circulation groove can be connected with the loop head of described shredder.The number of times that static inhibitor mixture carries out ball milling at grinding system is preferably 1-2 time, when grinding number of times is 2 times, static inhibitor mixture enters shredder and grinds for the first time, after completing, send into static inhibitor circulation groove, through static inhibitor circulation groove, again enter in shredder and grind for the second time.The number of times of described grinding can be adjusted according to practical situation.
In the preparation process of above-mentioned static inhibitor dispersion liquid, flow and flow velocity that the static inhibitor mixture after wherein stirring in static inhibitor dispersion slot is sent into grinding system can artificially regulate; Flow and flow velocity that static inhibitor mixture after grinding enters in the process of static inhibitor dilution trap also can artificially regulate; Described static inhibitor dilution trap is also furnished with flow and counts its supplementary diluent, the preferred ethylene glycol of diluent.
Described shredder can be selected projection formula sand mill, and the particle diameter after projection formula sand mill grinds is less, and effect is better, and working efficiency is high.
Can grind the single time and number of times is controlled the degree of scatter of static inhibitor in static inhibitor dispersion liquid by adjusting, nano-metal-oxide static inhibitor in static inhibitor dispersion liquid (nanometer antimony-doped stannic oxide ATO) can be 1:2-1:10 with quality of glycol than span of control, nano-metal-oxide static inhibitor can be 1:0.5-1:3 with the quality of dispersion agent polyoxyethylene glycol than span of control, in antistatic dispersion liquid, the concentration of nanometer antimony-doped stannic oxide ATO can be 5-20%, working pressure scope is 0-10kPa (G), operating temperature range can be 10-100 ℃.Under this reaction conditions, static inhibitor stability is higher, nano-metal-oxide disperses comparatively even, and particle diameter is less, be conducive to further esterification and polycondensation and produce antistatic cationic polyester product, combine with follow-up esterification technique condition, realize the optimization of each composition and each reactions steps in esterification technique, thus not only for the continuous production of antistatic cationic polyester with the condition that provides is directly provided, but also be conducive to improve antistatic property and the dyeing behavior of product.
Described shredder and/or described static inhibitor circulation groove can be provided with grinding system entrance, and described static inhibitor dispersion slot can be provided with static inhibitor and disperse outlet, and described static inhibitor disperses outlet to be connected with described grinding system entrance.Static inhibitor dispersion slot can be connected with static inhibitor circulation groove with shredder simultaneously, therein connecting passage stop up or the situation of damage under, still can guarantee the normal work of static inhibitor grinding distribution system.
Described shredder and/or described static inhibitor circulation groove can be provided with grinding system outlet, and described static inhibitor dilution trap can be provided with static inhibitor dilution entrance, and described grinding system outlet can be connected with described static inhibitor dilution entrance.Static inhibitor dilution trap can be connected with static inhibitor circulation groove with shredder simultaneously, therein connecting passage stop up or the situation of damage under, still can guarantee the normal work of static inhibitor grinding distribution system.
The preparation of the 3rd monomer:
Described the 3rd monomeric ester exchange system comprises the 3rd monomeric ester exchange reactor 21 and the 3rd monomer charging tank 22, the outlet of described the 3rd monomeric ester exchange reactor is connected with the entrance of described the 3rd monomer charging tank, and the outlet of described the 3rd monomer charging tank is as the 3rd monomer outlet of described the 3rd monomeric ester exchange system.Described the 3rd monomer preparation system employing dimethyl isophthalate-5-benzene sulfonic acid sodium salt (SIPM) carries out transesterify with ethylene glycol by semi-continuous process and prepares the two hydroxyl ethyl ester-5-benzene sulfonic acid sodium salts (described the 3rd monomer SIPE) of m-phthalic acid, and be stored in described the 3rd monomer charging tank, then by the 3rd monomer after accurate measurement, inject described the second esterifier.On pipeline between described the 3rd monomer charging tank and described the second esterifier, charging pump can be installed.
The preparation of the 4th monomer:
Described the 4th monomer compounding system comprises the 4th molten monomer groove 41 and the 4th monomer charging tank 42, described the 4th molten monomer groove outlet is connected with described the 4th monomer charging tank entrance, outlet on described the 4th monomer charging tank is as the 4th monomer outlet of described the 4th monomer configuration-system, and the outlet of described the 4th monomer charging tank is also connected with described the 4th molten monomer groove entrance.
Conventionally, a part for pipeline between described the 4th monomer charging tank outlet and the 4th monomer entrance of described the second esterifier and a part for the pipeline between described the 4th monomer charging tank outlet and described the 4th molten monomer groove entrance can share same segment pipe, on this section of described pipeline, charging pump are installed;
Further, pipeline between described the 4th monomer charging tank and described the 4th molten monomer groove and the pipeline between the 4th monomer charging tank and described the second esterifier all can be furnished with hot steam pipeline, described the 4th molten monomer groove inside can be provided with heating medium for heating coil pipe, its outside can be provided with heating agent chuck, and the outside of described the 4th monomer charging tank can be provided with heating agent chuck.
Load weighted the 4th monomer polyoxyethylene glycol is added in described the 4th molten monomer groove, the 4th monomer solution that draws again one heat from the 4th monomer charging pump enters in the 4th molten monomer groove, by heating medium for heating coil pipe, accelerate the melting of polyoxyethylene glycol, through stirring the 4th monomer solution that is mixed with 100% concentration.After being filtered, send in the 4th monomer charging tank.Again the 4th monomer being stored in described the 4th monomer charging tank is passed through to accurate-metering by injecting continuously described the second esterifier by charging pump.In this process, the outside of the 4th molten monomer groove and the 4th monomer charging tank is equipped with heating agent chuck, connecting tube between them is furnished with hot steam pipeline needs coil pipe heating and vapour line, reduce the loss of heat in the 4th periods of monomer flow process and storage process, guarantee that the 4th monomer remains the state of melting.
Conventionally, on described Prepolycondensating reactor, can be provided with precondensation vacuum system 10 and the precondensation temperature controlling system of controlling described Prepolycondensating reactor internal vacuum and temperature.Its service temperature is controlled at 260-280 ℃ conventionally, and as 260 ℃, 265 ℃, 270 ℃, 275 ℃ or 280 ℃, definitely working pressure is controlled at 5-25mbar, as 5mbar, 10mbar, 15mbar, 20mbar or 25mbar.
Conventionally, on described finishing reactor, can be provided with aftercondensated vacuum system 11 and the aftercondensated temperature controlling system of controlling described finishing reactor internal vacuum and temperature.Its temperature is controlled at 265-285 ℃ conventionally, as 265 ℃, 270 ℃, 275 ℃, 280 ℃ or 285 ℃, regulates the absolute pressure after vacuum system to be not more than 3mbar, as 3mbar, 2mbar or 1mbar.
The esterification outlet of described finishing reactor can connect slice systems and/or spinning system by pipeline, on described pipeline, can be provided with toothed gear pump and strainer, make the melt that reaches desired viscosity after described toothed gear pump supercharging and strainer filtration, by distribution valve, switch and to distribute, deliver to slice systems and/or spinning system.
The utility model is under the processing parameter and specific device structure condition of above-mentioned uniqueness, realized the continuous production of the antistatic cationic polyester of copoly type, in the antistatic cationic polyester of producing static inhibitor granularity little, be evenly distributed, associativity is good, antistatic cationic polyester static inhibitor mass content scope is 0.3-1.5%, fiber volume fraction resistance≤10
8Ω cm, fusing point>=250 ℃, can be controlled in ± 0.01dl/g of viscosity fluctuation scope product performance are stable, and antistatic property is excellent, wash resistant, dyeability under ordinary pressure is excellent, and painted rear color is beautiful.
Claims (10)
1. the production system that can produce continuously the antistatic cationic polyester of copoly type, comprise esterification system, described esterification system at least comprises the first esterifier and the second esterifier connecting successively, characterized by further comprising static inhibitor grinding distribution system, the 3rd monomeric ester exchange system and the 4th monomer configuration-system, the static inhibitor dispersion liquid outlet of described static inhibitor grinding distribution system is connected with the static inhibitor dispersion liquid entrance of described the second esterifier, the 3rd monomer outlet of described the 3rd monomeric ester exchange system is connected with the 3rd monomer entrance of described the second esterifier, the 4th monomer outlet of described the 4th monomer configuration-system is connected with the 4th monomer entrance of described the second esterifier.
2. the production system that can produce continuously the antistatic cationic polyester of copoly type according to claim 1, it is characterized in that described static inhibitor grinding distribution system comprises static inhibitor dispersion slot, grinding system, static inhibitor dilution trap, whizzer and the static inhibitor dispersion liquid charging tank connecting successively, described static inhibitor dispersion slot is provided with feed(raw material)inlet, described static inhibitor dispersion liquid charging tank is provided with the outlet of static inhibitor dispersion liquid, its outlet of static inhibitor dispersion liquid as described static inhibitor grinding distribution system.
3. the production system that can produce continuously the antistatic cationic polyester of copoly type according to claim 2, it is characterized in that described grinding system comprises shredder and static inhibitor circulation groove, the loop exit of described shredder is connected with the loop head of described static inhibitor circulation groove, and the loop exit of described static inhibitor circulation groove is connected with the loop head of described shredder.
4. the production system that can produce continuously the antistatic cationic polyester of copoly type according to claim 1, it is characterized in that described the 3rd monomeric ester exchange system comprises the 3rd monomeric ester exchange reactor and the 3rd monomer charging tank, the outlet of described the 3rd monomeric ester exchange reactor is connected with the entrance of described the 3rd monomer charging tank, and the outlet of described the 3rd monomer charging tank is as the 3rd monomer outlet of described the 3rd monomeric ester permutoid reaction system.
5. the production system that can produce continuously the antistatic cationic polyester of copoly type according to claim 1, it is characterized in that described the 4th monomer compounding system comprises the 4th molten monomer groove and the 4th monomer charging tank, described the 4th molten monomer groove outlet is connected with described the 4th monomer charging tank entrance, outlet on described the 4th monomer charging tank is as the 4th monomer outlet of described the 4th monomer configuration-system, and the outlet of described the 4th monomer charging tank is also connected with described the 4th molten monomer groove entrance.
6. the production system that can produce continuously the antistatic cationic polyester of copoly type according to claim 5, it is characterized in that a part for the pipeline between described the 4th monomer charging tank outlet and the 4th monomer entrance of described the second esterifier and a part for the pipeline between described the 4th monomer charging tank outlet and described the 4th molten monomer groove entrance share same segment pipe, are provided with charging pump on this section of described pipeline;
Pipeline between described the 4th monomer charging tank and described the 4th molten monomer groove and the pipeline between the 4th monomer charging tank and described the second esterifier are all furnished with hot steam pipeline, described the 4th molten monomer groove inside is provided with heating medium for heating coil pipe, its outside is provided with heating agent chuck, and the outside of described the 4th monomer charging tank is provided with heating agent chuck.
7. according to the production system that can produce continuously the antistatic cationic polyester of copoly type described in claim 1-6 any one, it is characterized in that described the second esterifier is horizontal esterifier, its inner chamber is divided into the first chamber from left to right, the second chamber and the 3rd chamber, in each chamber, be equipped with whipping appts, the static inhibitor dispersion liquid outlet of described static inhibitor grinding distribution system connects described the first chamber, the 3rd monomer outlet of described the 3rd monomeric ester exchange system connects described the first chamber, the 4th monomer outlet of described the 4th monomer configuration-system connects described the second chamber.
8. the production system that can produce continuously the antistatic cationic polyester of copoly type according to claim 7, characterized by further comprising and connect successively Prepolycondensating reactor and finishing reactor, the esterification outlet of described the second esterification device connects the esterification entrance of described Prepolycondensating reactor, and described Prepolycondensating reactor and described finishing reactor all dispose corresponding vacuum system and temperature controlling system.
9. the production system that can produce continuously the antistatic cationic polyester of copoly type according to claim 7, characterized by further comprising slurry preparation groove, and the esterification outlet of described slurry preparation groove connects the esterification entrance of described the first esterifier.
10. the production system that can produce continuously the antistatic cationic polyester of copoly type according to claim 8, is characterized in that the esterification outlet of described finishing reactor connects slice systems and/or spinning system by pipeline.
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| CN201420056096.9U CN203794824U (en) | 2014-01-29 | 2014-01-29 | Production system capable of continuously producing copolymerized antistatic cationic polyester |
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| CN201420056096.9U CN203794824U (en) | 2014-01-29 | 2014-01-29 | Production system capable of continuously producing copolymerized antistatic cationic polyester |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2020133961A1 (en) * | 2018-12-29 | 2020-07-02 | 中国纺织科学研究院有限公司 | Functional polyester production method and production system, and functional polyester fiber |
| CN112844280A (en) * | 2020-12-23 | 2021-05-28 | 中国纺织科学研究院有限公司 | Horizontal reaction kettle, functional polyester production system applying same and production method |
-
2014
- 2014-01-29 CN CN201420056096.9U patent/CN203794824U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2020133961A1 (en) * | 2018-12-29 | 2020-07-02 | 中国纺织科学研究院有限公司 | Functional polyester production method and production system, and functional polyester fiber |
| CN112844280A (en) * | 2020-12-23 | 2021-05-28 | 中国纺织科学研究院有限公司 | Horizontal reaction kettle, functional polyester production system applying same and production method |
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