CN201485548U - System for continuously producing cation modified polyester melts and directly spinning polyester fibers - Google Patents
System for continuously producing cation modified polyester melts and directly spinning polyester fibers Download PDFInfo
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- CN201485548U CN201485548U CN 200920173003 CN200920173003U CN201485548U CN 201485548 U CN201485548 U CN 201485548U CN 200920173003 CN200920173003 CN 200920173003 CN 200920173003 U CN200920173003 U CN 200920173003U CN 201485548 U CN201485548 U CN 201485548U
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Abstract
The utility model relates to a system for continuously producing cation modified polyester melts and directly spinning polyester fibers. The system comprises a feed system, an esterification reaction system, a polycondensation reaction system and a spinning system which are sequentially connected, wherein the polycondensation reaction system and the spinning system have a connecting mode that a melt outlet of the polycondensation reaction system is connected with a melt inlet of the spinning system; the feed system comprises a slurry preparation tank respectively connected with a PTA metering system, an ethylene glycol metering system and a catalyst metering system through pipelines; the esterification reaction system at least comprises a first esterification reactor and a second esterification reactor; and the second esterification reactor is a horizontal chambered reactor specially designed aiming at cation polyester production. The system can realize the continuous production of cation modified polyester and the direct spinning of the melts, improves the production efficiency of the cation modified polyester melts and fibers, is beneficial to reducing the production cost and has stable product quality.
Description
Technical field
The utility model relates to the system of cation-modified polyester fondant of a kind of continuous production and Direct Spinning polyester fiber.
Background technology
Existing terylene direct fabrics technology is had relatively high expectations to technological parameters such as temperature, pressure, drawing-off degree, and certain variation has all taken place through polyester physical and chemical performance, spinning properties and the serviceability after cation-modified, bring bigger difficulty to direct fabrics, therefore, general employing discontinuous polycondensation and slice spinning when spinning cationic polyester fiber both at home and abroad at present.But the slice spinning technological process is long, the capital expenditure expense is big, energy consumption is big, production cost is high, and deviation all can appear in each batch of batch production temperature, pressure, proportioning raw materials, controlled condition etc., is difficult to reach consistent, causes unstable product quality.
Summary of the invention
For overcoming the defective of prior art, the utility model provides the system of cation-modified polyester fondant of a kind of continuous production and Direct Spinning polyester fiber, this system can comprise the feeding system that links to each other successively, the esterification system, polycondensation system and spinning system, described polycondensation system and the connected mode of described spinning system can be connected the melt inlet of described spinning system for the melt outlet of described polycondensation system, described feeding system can comprise the slurry make-up tank, described slurry make-up tank can by pipeline respectively with the PTA metering system, the ethylene glycol metering system links to each other with the catalyst metering system.
Described esterification system generally includes first esterifier and second esterifier that connects successively, described second esterifier can be one and be different from the horizontal reactor that normal polyester is produced three chambers of used vertical reactor, adjacent chamber in three chambers of described horizontal reactor generally adopts dividing plate to separate, be typically provided with plurality of holes on the described dividing plate, be used for melt and can flow into two Room from a Room, and then flow into three Room from two Room, can have some other monomer input ports on the end face of described three chambers, described three chambers generally are respectively equipped with heating agent heat(ing) coil separately, are used for controlling respectively the temperature of corresponding chambers.
Described three chambers of described second esterifier can also be respectively equipped with agitator separately, and the top of described agitator can be equipped with paddle, and the bottom can be equipped with shearing wheel and stable bearing; Described heating agent heat(ing) coil adopts the screw type coil pipe usually, can use the heating of liquid phase heating agent.
Described second esterifier is furnished with ethylene glycol Gas Recovery refrigerated separation equipment usually, described recovery refrigerated separation equipment can be provided with ethylene glycol import, light component outlet and heavy ends outlet, and described heavy ends outlet connects the ethylene glycol import of described second esterifier usually by pipeline.
Described polycondensation reaction equipment can comprise prepolymerization reaction equipment and the poly-consersion unit of final minification that connects successively at least, the poly-consersion unit of described prepolymerization reaction equipment and/or final minification can be provided with the scraper plate condenser, and the ethylene glycol import of described recovery refrigerated separation equipment connects the ethylene glycol outlet of described scraper plate condenser usually by pipeline.
Described prepolymerization reaction equipment adopts vertical perfectly mixed reactor usually, and described vertical perfectly mixed reactor is generally a still two cell structures, divides chamber up and down, and is provided with the control valve that chamber and following chamber are gone up in connection, and following chamber is provided with mechanical agitation.
Described Prepolycondensating reactor and final polycondensation reactor all are furnished with vacuum equipment usually, and described vacuum equipment can be made up of the ethylene glycol steam jet pump and the liquid-ring vacuum pump that complement one another.
Described spinning system be typically provided with connect successively leave standstill blender and spinning manifold.
Be typically provided with booster pump on the pipeline of described final polycondensation reactor melt outlet and spinning manifold melt inlet.Can also be provided with distributing valve on the pipeline of described final polycondensation reactor melt outlet and spinning manifold melt inlet, described distributing valve can connect bypass duct, and described bypass duct connects the section production system usually.
The beneficial effects of the utility model are that the fused mass directly spinning continuously synthetic and cation-modified polyester fiber with cation-modified polyester is incorporated on the production line, required the 3rd monomer of cation-modified polyester adds in the second step esterification, and introduce the refining recovery refrigerated separation Tower System that condensation ethylene glycol is carried out refining and edulcoration by unique design that second esterifier is carried out and novelty, make the continous mode melt reach the spinning requirement degree of polymerization, thereby solved the difficulty that the continous mode Direct Spinning is difficult to be applied to the cationic polyester fiber production smoothly, make polyester under melt state, enter the spinning system and directly carry out spinning, simplified whole technical process thus significantly, improve the production efficiency of cation-modified polyester fiber, also stablized product quality when reducing production costs; By distributing valve is set the melt of spinning unit redundancy is introduced slice systems, adopt existing microtomy to make section, can mate the production capacity of each system effectively, and can under situations such as spinning system maintenance, melt be made section.
Description of drawings
Fig. 1 is a schematic flow sheet of the present utility model.
Fig. 2 is the second esterifier schematic diagram in the utility model.
Fig. 3 is the schematic diagram of flow process of the present utility model and system embodiment I.
Fig. 4 is the schematic diagram of flow process of the present utility model and system embodiment II.
The specific embodiment
Referring to Fig. 1-4, the utility model provides the system of cation-modified polyester fondant of a kind of continuous production and Direct Spinning polyester fiber, solved the difficulty of cation-modified polyester continous mode melt Direct Spinning fiber smoothly, improve the production efficiency of cation-modified polyester fondant and fiber, also stablized product quality when reducing production costs.
The bin and the slurry make-up tank of the various materials supporting with it are set as last in the esterification system.PTA can pass through the continuous discharging of revolving valve from bin, and material enters vibrating screen usually after the discharging, and the different shape foreign material of sieve deentrainment enter mass flowmenter subsequently, are sent into the slurry make-up tank continuously through the PTA that measures; Raw material ethylene glycol (MEG) is sent into the slurry make-up tank from head tank in proportion continuously after delivery pump, mass flowmenter metering; Simultaneously, adopt the polycondensation reaction of intermittently dispensing mode allotment after the liquid mass flow meter metering, also to send into the slurry make-up tank continuously from feeder channel by polymerization ratio with antimony triacetate or glycol antimony catalyst solution.According to actual production batching standard, can adjust and change catalyst and follow-up various other monomers, these adjustment can not hinder enforcement of the present utility model according to prior art and other correlation techniques.
Be typically provided with agitator in the slurry configured slot, raw material PTA, MEG and antimony triacetate or glycol antimony catalyst fully mix under the effect of agitator usually, be mixed with the slurry of the needed constant mol ratio of polyester synthetic reaction (MEG/PTA), subsequently, slurry is sent into the esterification system continuously by the slurry delivery pump.
The esterification system comprises first esterifier and second esterifier that links to each other successively at least, at least two step esterifications before and after can realizing, between first esterifier and second esterifier, also can add other esterifier as required, to realize the more esterification of multistep.Described first esterifier and second esterifier are equipped with corresponding Temperature-controlled appliance usually respectively and are used for the recovery refrigerated separation equipment that ethylene glycol waste gas is recycled.Regulate described Temperature-controlled appliance, temperature required to reach the polyester esterification; The described recovery refrigerated separation equipment of described second esterifier is generally refining separation equipment, described refining separation equipment can be provided with the ethylene glycol import that is used to introduce described prepolymerization reaction and/or the poly-reaction of described final minification scraper plate condenser condenses ethylene glycol, realizes that the refining and edulcoration of ethylene glycol lime set separates.Described refining separation equipment can adopt the knockout tower under the prior art.
The slurry of sending into first esterifier is under the effect of agitator, and fully reaction is also sent into second esterifier continuously, adds synthetic required other monomers of cation-modified polyester and proceed synthetic reaction after melt enters second esterifier.Can control the esterification yield of reaction by temperature, pressure and the liquid level of regulating first esterifier and second esterifier, the esterification yield of first step esterification can reach the esterification yield of 91%, the second step esterification more than 96%.Simultaneously the first esterifier ethylene glycol gas is reclaimed, cools off and separates at separation equipment, heavy ends ethylene glycol after the separation is back to first esterifier, it is interior as phegma to stay separation equipment after the light component condensation, and all the other send into treatment system as esterification waste water.
Second esterifier generally is the horizontal reactor of one three Room, three chambers link to each other usually successively, can separate with dividing plate between adjacent chamber, have some semicircle holes on the dividing plate usually, melt can flow into two Room from a Room by hole, and then flows into three Room; Three chamber roof all have the input port of several other monomers; Other monomers can add the different phase of the second different step esterifications according to the needs of producing to from the input port, each chamber generally is provided with the independently interior heat(ing) coil of heating agent, interior heat(ing) coil adopts the screw type coil pipe usually, and material can be OCr18Ni9, can adopt the heating of liquid phase heating agent; Each chamber also is provided with independently agitator usually, and top, shearing wheel and the stable bearing that paddle can be installed in agitator is installed in the bottom of agitator, and mixing speed is adjustable.
Polycondensation reaction equipment generally includes Prepolycondensating reactor and the final polycondensation reactor that links to each other successively, described Prepolycondensating reactor and final polycondensation reactor all are furnished with corresponding vacuum equipment, Temperature-controlled appliance, scraper plate condenser and liquid seal trough usually, vacuum equipment can comprise ethylene glycol jet pump and vavuum pump, usually be connected with the scraper plate condenser between the vacuum equipment of described Prepolycondensating reactor, final polycondensation reactor and correspondence, the described cooler of scraping can link to each other with liquid seal trough by pipeline.
Described prepolymerization reaction can adopt vertical perfectly mixed reactor, described vertical perfectly mixed reactor is generally a still two Room reactors that comprise chamber and following chamber, the described chamber of going up is typically provided with the esterification material inlet, described chamber down is typically provided with agitating device, the junction of chamber and following chamber is typically provided with the Flow of Goods and Materials control valve on described, open described control valve, the reaction mass of last chamber can flow into down the chamber, described chamber down is provided with agitating device, agitating device is not established in last chamber, utilize air-flow to stir, the agitating device of following chamber can be mechanical agitation.
The melt that reaches certain esterification yield is sent into Prepolycondensating reactor continuously after the second esterifier discharging, regulate that Prepolycondensating reactor is equipped with Temperature-controlled appliance, it is temperature required to make temperature reach the polyester prepolymerization reaction, send into melt fully reaction under the effect of vacuum condition and agitator of Prepolycondensating reactor, absolute operating pressure generally is controlled at about 8-20mbar, simultaneously, can adopt ethylene glycol and entrainment in the ethylene glycol spray capture vapour phase, with recirculated cooling water as cooling medium, the ethylene glycol gas of collecting leaves in the liquid seal trough after the scraper plate condenser condenses, usually the refining separation equipment of second esterification is sent in extraction, carries out impurity removal and purification and separates.
The chuck valve generally is equipped with in the Prepolycondensating reactor bottom, and melt can pass through the gear pump discharging, sends in the final polycondensation reactor.Can regulate the Temperature-controlled appliance that final polycondensation reactor is equipped with, temperature required to reach the PET final polycondensation reaction, send into melt fully reaction under the effect of vacuum condition and agitator of final polycondensation reactor, absolute operating pressure is controlled at about 3mbar usually; Final polycondensation reactor can be created vacuum environment by the ethylene glycol steam jet, with the exhaust stage of liquid rotary pump as it, the jet pump that sprays ethylene glycol steam is connected with the ethylene glycol evaporimeter, for jet pump provides power steam, be the poly-system vacuum degree of control final minification, adopt the cooling medium of chilled water, regulate vacuum and make the degree of polymerization of melt reach spinning requirement as the ethylene glycol spray liquid.
The melt that possesses the required degree of polymerization of spinning is the effect by gear pump usually, from final polycondensation reactor, flow out, under certain pressure after the poly-fondant filter of final minification filters, enter the melt jacket pipe and be delivered to distributing valve, the static mixer that melt by distributing valve is equipped with by uniform distribution to each bar spinning manifold is to reach identical spinning temperature and viscosity, enter spinning manifold then and carry out spinning, finish drawing-off, packing, storage and the transportation of strand subsequently.
In order to satisfy the needed melt pressure of spinning, in the melt Conveying pipeline, be provided with booster pump usually, simultaneously,, guarantee the quality of melt in order to overcome the temperature rise of melt through being produced behind the booster pump, can also be provided with melt cooler behind the booster pump.
The cationic polyester esterification system of this device, the used thermal source of polycondensation system and cationic polyester fibre spinning system provide by the heating agent station, heat medium circulation pump is delivered to cationic polyester esterification system, polycondensation system and cationic polyester fibre spinning system with the heating agent (about 320 ℃) of steady temperature, the heating agent that uses the back temperature to reduce is got back to the heating agent station by circulation line, promptly finishes the primary fluid closed-loop system.On the other hand, the volumetric expansion that raises and to produce for the balance heat medium temperature, the highest point of the synthesizer of forming at cationic polyester esterification system and polycondensation system is provided with the heating agent expansion slot with the balance volume change, simultaneously the heating agent feeder is set at the heating agent station, when stopping or running into other emergencies, receive the heating agent of polyester device discharging, the heating agent of delivering to each heat supplying loop circulation in the synthesizer is the secondary heating agent.By the primary fluid amount that adjusting enters each secondary circuit, can control the temperature of secondary heating agent, realize on the technology requirement to each equipment different temperatures.
The outlet of the melt of described final polycondensation reactor connects the melt Conveying pipeline usually, and the melt Conveying pipeline also can be connected with bypass duct by distributing valve, and described bypass duct connects the section production system.
When device for spinning quits work, changes product variety or reduce load, finish the melt of final minification after poly-and can send into the section production system and carry out Cast Strip pelletizing, packing, storage.Therefore, offered a pelletizing production line behind final polycondensation reactor, be furnished with the heat exchanger cooling recirculation system, cooling medium adopts demineralized water.
Claims (10)
1. system that produces continuously cation-modified polyester fondant and Direct Spinning polyester fiber, it is characterized in that comprising the feeding system, esterification system, polycondensation system and the spinning system that link to each other successively, described polycondensation system and the connected mode of described spinning system are the melt inlet that the melt outlet of described polycondensation system is connected described spinning system, described feeding system comprises the slurry make-up tank, and described slurry make-up tank links to each other with PTA metering system, ethylene glycol metering system and catalyst metering system respectively by pipeline.
2. according to the system of claim 1 cation-modified polyester fondant of described continuous production and Direct Spinning polyester fiber, it is characterized in that described esterification system comprises first esterifier and second esterifier that connects successively, described second esterifier is one and is different from the horizontal reactor that normal polyester is produced three chambers of used vertical reactor, adjacent chamber in three chambers of described horizontal reactor adopts dividing plate to separate, described dividing plate is provided with plurality of holes, be used for melt and flow into two Room from a Room, and then flow into three Room from two Room, have some other monomer input ports on the end face of described three chambers, described three chambers are respectively equipped with heating agent heat(ing) coil separately, are used for controlling respectively the temperature of corresponding chambers.
3. according to the system of claim 1 or 2 cation-modified polyester fondants of described continuous production and Direct Spinning polyester fiber, described three chambers that it is characterized in that described second esterifier also are respectively equipped with agitator separately, the top of described agitator is equipped with paddle, and the bottom is equipped with shearing wheel and stable bearing; Described heating agent heat(ing) coil adopts the screw type coil pipe, uses the heating of liquid phase heating agent.
4. according to the system of claim 3 cation-modified polyester fondant of described continuous production and Direct Spinning polyester fiber, it is characterized in that described second esterifier is furnished with ethylene glycol Gas Recovery refrigerated separation equipment, described recovery refrigerated separation equipment is provided with ethylene glycol import, light component outlet and heavy ends outlet, and described heavy ends outlet connects the ethylene glycol import of described second esterifier by pipeline.
5. according to the system of claim 4 cation-modified polyester fondant of described continuous production and Direct Spinning polyester fiber, it is characterized in that described polycondensation reaction equipment comprises prepolymerization reaction equipment and the poly-consersion unit of final minification that connects successively at least, the poly-consersion unit of described prepolymerization reaction equipment and/or final minification is provided with the scraper plate condenser, and the ethylene glycol import of described recovery refrigerated separation equipment connects the ethylene glycol outlet of described scraper plate condenser by pipeline.
6. according to the system of claim 5 cation-modified polyester fondant of described continuous production and Direct Spinning polyester fiber, it is characterized in that described prepolymerization reaction equipment adopts vertical perfectly mixed reactor, described vertical perfectly mixed reactor, be a still two cell structures, divide chamber up and down, and being provided with the control valve that chamber and following chamber are gone up in connection, following chamber is provided with mechanical agitation.
7. according to the system of claim 3,4, the 5 or 6 cation-modified polyester fondants of described continuous production and Direct Spinning polyester fiber, it is characterized in that described Prepolycondensating reactor and final polycondensation reactor all be furnished with vacuum equipment, described vacuum equipment is made up of the ethylene glycol steam jet pump and the liquid-ring vacuum pump that complement one another.
8. according to the system of claim 7 cation-modified polyester fondant of described continuous production and Direct Spinning polyester fiber, it is characterized in that described spinning system be provided with connect successively leave standstill blender and spinning manifold.
9. the system of cation-modified polyester fondant of described according to Claim 8 continuous production and Direct Spinning polyester fiber is characterized in that the described final polycondensation reactor melt outlet and the pipeline of spinning manifold melt inlet are provided with booster pump.
10. according to the system of claim 9 cation-modified polyester fondant of described continuous production and Direct Spinning polyester fiber, it is characterized in that also being provided with distributing valve on the pipeline of the outlet of described final polycondensation reactor melt and spinning manifold melt inlet, and by described distributing valve connection bypass duct, described bypass duct connects the section production system.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200920173003 CN201485548U (en) | 2009-08-13 | 2009-08-13 | System for continuously producing cation modified polyester melts and directly spinning polyester fibers |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 200920173003 CN201485548U (en) | 2009-08-13 | 2009-08-13 | System for continuously producing cation modified polyester melts and directly spinning polyester fibers |
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| CN201485548U true CN201485548U (en) | 2010-05-26 |
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| CN 200920173003 Expired - Lifetime CN201485548U (en) | 2009-08-13 | 2009-08-13 | System for continuously producing cation modified polyester melts and directly spinning polyester fibers |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109321989A (en) * | 2018-11-10 | 2019-02-12 | 宁波华星科技有限公司 | A kind of polymer melt and the polymer melt conveying technique |
| CN110724253A (en) * | 2019-11-14 | 2020-01-24 | 扬州普立特科技发展有限公司 | Full-continuous PBAT production equipment and process flow |
-
2009
- 2009-08-13 CN CN 200920173003 patent/CN201485548U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109321989A (en) * | 2018-11-10 | 2019-02-12 | 宁波华星科技有限公司 | A kind of polymer melt and the polymer melt conveying technique |
| CN110724253A (en) * | 2019-11-14 | 2020-01-24 | 扬州普立特科技发展有限公司 | Full-continuous PBAT production equipment and process flow |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170214 Address after: 100007 Beijing, Dongzhimen, North Street, No. 9, No. Patentee after: China National Petroleum Corporation Patentee after: China Kunlun Engineering Co., Ltd. Address before: 100007 Beijing, Dongzhimen, North Street, No. 9, No. Patentee before: China National Petroleum Corporation Patentee before: China Textile Industrial Engineering Institute |
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| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20100526 |