CN217516872U - Continuous production system for preparing regenerated polyester from waste polyester - Google Patents
Continuous production system for preparing regenerated polyester from waste polyester Download PDFInfo
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- CN217516872U CN217516872U CN202221360487.0U CN202221360487U CN217516872U CN 217516872 U CN217516872 U CN 217516872U CN 202221360487 U CN202221360487 U CN 202221360487U CN 217516872 U CN217516872 U CN 217516872U
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Abstract
The utility model discloses a serialization production system by old and useless polyester preparation regeneration polyester, include screw extruder, first alcoholysis cauldron, second alcoholysis cauldron, active carbon adsorption device, first film evaporator, second film evaporator, molecular distillation ware, first polycondensation reaction cauldron in advance, second polycondensation reaction cauldron in advance and final polycondensation reaction cauldron through pipeline series connection in proper order, wherein: and a light component discharge port of the molecular distiller is connected with a feed inlet of the first pre-polycondensation reaction kettle, and a heavy component discharge port of the molecular distiller is connected with a feed back port of the first alcoholysis kettle. Serialization production system, not only can realize serialization production, practice thrift the energy consumption moreover to simplified the preparation technology of regeneration polyester and obviously shortened regeneration polyester's preparation cycle, realized the complete closed loop recycle of old and useless PET polyester, to realizing that old and useless PET polyester is the most meaningful regeneration cyclic utilization has important and practical value.
Description
Technical Field
The utility model relates to a by waste polyester preparation regeneration polyester's serialization production system belongs to waste polyester recycle technical field.
Background
Polyesters (i.e., polyethylene terephthalate) have been widely used in the fields of food packaging, film sheets, electronic devices, mechanical equipment, etc., because of their excellent physicochemical properties. According to statistics, in 2008, China becomes the first major country for producing and consuming polyester in the world, the yield accounts for more than half of the world, in 2015, the yield of polyester in China reaches 3530 ten thousand tons, in 2019, the yield of polyester in China reaches 5006 ten thousand tons, and the amplification reaches 41.8%. Most of polyester products become waste products after one-time use, so that the yield of waste polyester is increased along with the rapid development of the polyester industry. However, polyester has strong chemical inertness, is difficult to degrade after being naturally stored or is decomposed by microorganisms, not only causes huge resource waste, but also generates serious environmental pollution, so how to realize the virtuous cycle of recycling and reusing waste polyester becomes an important subject which cannot be avoided and needs to be solved urgently in the development of the current polyester industry.
Theoretically, BHET (i.e. ethylene terephthalate with CAS number of 959-26-2) can be directly subjected to polycondensation reaction to obtain polyethylene terephthalate (i.e. PET), so that if high-purity BHET monomer prepared from waste polyester can be obtained, regenerated polyester can be prepared through further polycondensation reaction, and the recycling of waste PET polyester is really realized. However, the waste PET polyester has a complex source, and the colored PET polyester raw material can cause the color of the depolymerization product BHET to be dark, so that the reapplication grade of the regenerated polyester is limited, and the colored PET polyester raw material becomes a bottleneck problem for recycling the PET polyester through glycolysis; further, since BHET has a high boiling point (432.1 ℃) and an active group (hydroxyl group), when ethylene glycol is used to depolymerize waste polyester, a by-product of diethylene glycol (hereinafter abbreviated as DEG) produced by self-condensation of ethylene glycol and a by-product of 2-hydroxyethyl terephthalate (hereinafter abbreviated as DEG ester) produced by transesterification of DEG with BHET are likely to occur, and DEG or DEG ester has characteristics similar to those of EG or BHET and is extremely difficult to be separated from BHET, so that high purity BHET monomer cannot be produced. Although the patent number 200510097626.X discloses that high-purity BHET can be obtained by performing molecular distillation treatment on an ethylene glycol solution containing crude BHET after 2 times of evaporation treatment, the patent needs a plurality of treatment procedures such as pre-depolymerization, removal of solid foreign matters, decolorization of activated carbon, deionization by using ion exchange resin, crystallization, solid-liquid separation and the like from waste polyester to the ethylene glycol solution containing crude BHET, and not only has complex process and large energy consumption (for example, the process needs to use ethylene glycol with the mass at least 5 times as much as that of the waste polyester, otherwise, the whole system is in a hard block shape or a hard paste shape, and subsequent crystallization and solid-liquid separation cannot be performed, but also needs to heat up to 250 ℃ from normal temperature to the crystallization procedure, and needs to cool down to 5 ℃, then needs to heat up to 150 ℃ for evaporation, and needs to heat up to and back again between 5 ℃ and 250 ℃ during the depolymerization procedure, Temperature reduction and temperature rise treatment, so that energy consumption is high), and the key is that the process cannot realize continuous production, such as: the BHET obtained by crystallization is in a sludge state, so that a filter press is required to perform filter pressing during solid-liquid separation treatment, the situation that the filter screen is blocked and the filter cloth needs to be frequently replaced is easy to occur, and continuous production cannot be realized.
SUMMERY OF THE UTILITY MODEL
To the above problems in the prior art, the present invention provides a continuous production system for preparing recycled polyester from waste polyester, so as to meet the requirement of large-scale recycling of waste polyester.
In order to achieve the above object, the utility model adopts the following technical scheme:
a continuous production system for preparing regenerated polyester from waste polyester comprises a screw extruder, a first alcoholysis kettle, a second alcoholysis kettle, an activated carbon adsorption device, a first film evaporator, a second film evaporator, a molecular distiller, a first pre-polycondensation reaction kettle, a second pre-polycondensation reaction kettle and a final polycondensation reaction kettle which are sequentially connected in series through pipelines, wherein: and a light component discharge port of the molecular distiller is connected with a feed port of the first pre-polycondensation reaction kettle, and a heavy component discharge port of the molecular distiller is connected with a feed back port of the first alcoholysis kettle.
In one embodiment, the continuous production system further comprises a waste polyester feeding bin, and a discharge port of the waste polyester feeding bin is connected with a feed port of the screw extruder through a pipeline.
In one embodiment, a first melt filter and a first delivery pump are connected in series on a pipeline connecting a screw extruder and a first alcoholysis kettle.
In one embodiment, a second delivery pump is connected in series with the pipeline connecting the first alcoholysis kettle and the second alcoholysis kettle.
In one embodiment, a third delivery pump, a second melt filter, an alcoholysis product transfer tank and a fourth delivery pump are sequentially connected in series on a pipeline connecting the second glycolysis kettle and the activated carbon adsorption device.
In one embodiment, a first thin film evaporation product transfer tank and a fifth delivery pump are connected in series on a pipeline connecting the first thin film evaporator and the second thin film evaporator.
In one embodiment, a second film evaporation product transfer tank and a sixth delivery pump are connected in series on a pipeline connecting the second film evaporator and the molecular still in sequence.
In one embodiment, a pipeline connecting a light component discharge port of the molecular distiller and the first pre-polycondensation reaction kettle is sequentially connected in series with a BHET monomer melt collecting and heat preserving tank and a BHET monomer melt delivery pump.
In one embodiment, a seventh delivery pump is connected in series on a pipeline between a heavy component discharge port of the molecular distiller and a return port of the first alcoholysis kettle.
In one embodiment, a pre-shrinking melt conveying pump and a pre-shrinking melt filter are connected in series on a pipeline connecting the second pre-polycondensation reaction kettle and the final polycondensation reaction kettle in sequence.
In one embodiment, a final-shrinkage melt conveying pump and a final-shrinkage melt filter are connected in series at a discharge port of a final-shrinkage polymerization reaction kettle in sequence.
Compared with the prior art, the utility model discloses following beneficial effect has:
the continuous production system of the utility model, through setting up the screw extruder at the alcoholysis front end, make old and useless polyester material extrude melting and alcoholysis in advance in the screw extruder in advance to reduce the intrinsic viscosity of waiting to alcoholysis material, thereby not only realized the continuous feeding of alcoholysis reaction, realized moreover that the alcoholysis reaction can go on in the homogeneous system, and then accelerated the alcoholysis rate and shortened the alcoholysis reaction time, can effectively reduce the production of accessory substance, be favorable to obtaining high-purity BHET monomer; additionally, the utility model discloses an organic combination film evaporator and molecular still's purification treatment can realize making high-purity BHET monomer fuse-element by old and useless polyester high yield, and then can directly carry out the polycondensation reaction in advance, so not only practiced thrift the energy consumption, realized the complete serialization production of regeneration polyester, simplified the preparation technology of regeneration polyester and obviously shortened the preparation cycle of regeneration polyester moreover, realized old and useless PET polyester complete closed loop recycle, it has important meaning and practical value to realizing old and useless PET polyester regeneration cyclic utilization in the true sense.
Drawings
Fig. 1 is a schematic structural diagram of a continuous production system for preparing recycled polyester from waste polyester provided in embodiment 1 of the present invention.
The numbers in the figures are as follows:
01. a screw extruder; 02. a first alcoholysis kettle; 02-1, a feed back port; 03. a second glycolysis kettle; 04. an activated carbon adsorption unit; 05. a first thin film evaporator; 06. a second thin film evaporator; 07. a molecular still; 07-1, and a heavy component discharge port; 07-2 parts of a light component discharge port; 08. a first pre-polycondensation reaction kettle; 09. a second pre-polycondensation reaction kettle; 10. a final polycondensation reaction kettle; 11. feeding waste polyester into a bin; 12. a first melt filter; 13. a first delivery pump; 14. a second delivery pump; 15. a third delivery pump; 16. a second melt filter; 17. alcoholysis products are transferred to a tank; 18. a fourth delivery pump; 19. a first thin film evaporation product transfer tank; 20. a fifth delivery pump; 21. a second thin film evaporation product transfer tank; 22. a sixth delivery pump; 23. a BHET monomer melt collection and heat preservation tank; 24. a delivery pump for BHET monomer melt; 25. a seventh delivery pump; 26. a pre-shrinking melt delivery pump; 27. a pre-shrinking melt filter; 28. a final-shrinkage melt delivery pump; 29. a final shrinkage melt filter; 30. casting a belt head; 31. a granulator; 32. a dryer; 33. vibrating screen; 34. a slicing bin.
Detailed Description
The technical solution of the present invention will be described in detail and fully with reference to the following embodiments and accompanying drawings. It should be understood that the following examples are illustrative of the present invention only and are not intended to limit the scope of the present invention.
It is to be understood that, in the description of the present invention:
the terms "first," "second," "third," …, and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implying any number of technical features indicated.
The waste polyester of the utility model includes but not limited to polyester production waste and waste polyester product, the polyester product includes but not limited to PET bottle, PET packing sheet, PET fibre, PET fabrics and PET papaw material.
Examples
Referring to fig. 1, the continuous production system for preparing recycled polyester from waste polyester provided in this embodiment includes a screw extruder 01, a first alcoholysis kettle 02, a second glycolysis kettle 03, an activated carbon adsorption device 04, a first film evaporator 05, a second film evaporator 06, a molecular still 07, a first pre-polycondensation reaction kettle 08, a second pre-polycondensation reaction kettle 09, and a final polycondensation reaction kettle 10, which are sequentially connected in series through a pipeline, specifically: a discharge hole of the screw extruder 01 is connected with a feed hole of the first alcoholysis kettle 02 through a pipeline, a discharge hole of the first alcoholysis kettle 02 is connected with a feed hole of the second alcoholysis kettle 03 through a pipeline, a discharge hole of the second alcoholysis kettle 03 is connected with a feed hole of the activated carbon adsorption device 04 through a pipeline, a discharge hole of the activated carbon adsorption device 04 is connected with a feed hole of the first film evaporator 05 through a pipeline, a discharge hole of the first film evaporator 05 is connected with a feed hole of the second film evaporator 06 through a pipeline, a discharge hole of the second film evaporator 06 is connected with a feed hole of the molecular distiller 07 through a pipeline, and a heavy component discharge hole 07-1 of the molecular distiller 07 is connected with a return hole 02-1 of the first alcoholysis kettle 02 through a pipeline; the light component discharge port 07-2 of the molecular still 07 is connected with the feed port of the first pre-polycondensation reaction kettle 08 through a pipeline, the discharge port of the first pre-polycondensation reaction kettle 08 is connected with the feed port of the second pre-polycondensation reaction kettle 09 through a pipeline, and the discharge port of the second pre-polycondensation reaction kettle 09 is connected with the feed port of the final polycondensation reaction kettle 10 through a pipeline.
In addition, in the present embodiment:
the continuous production system further comprises a waste polyester feeding bin 11, a discharge hole of the waste polyester feeding bin 11 is connected with a feed inlet of the screw extruder 01 through a pipeline, and continuous feeding of the screw extruder 01 can be guaranteed by arranging the waste polyester feeding bin 11.
A first melt filter 12 and a first delivery pump 13 are connected in series on a pipeline connecting the screw extruder 01 and the first alcoholysis kettle 02 in sequence, specifically: the feeding hole of the first melt filter 12 is connected with the discharging hole of the screw extruder 01 through a pipeline, the discharging hole of the first melt filter 12 is connected with the feeding hole of the first conveying pump 13 through a pipeline, and the discharging hole of the first conveying pump 13 is connected with the feeding hole of the first alcoholysis kettle 02 through a pipeline. The first melt filter 12 is connected in series between the screw extruder 01 and the first alcoholysis kettle 02 to filter solids in the pre-alcoholysis melt output by the screw extruder, so that the pre-alcoholysis melt can better form a homogeneous system with an alcoholysis solvent in the first alcoholysis kettle, and further the speed of the alcoholysis reaction can be further improved and the time of the alcoholysis reaction can be shortened.
A second delivery pump 14 is connected in series on a pipeline connecting the first alcoholysis kettle 02 and the second alcoholysis kettle 03, specifically: the feed inlet of the second delivery pump 14 is connected with the discharge outlet of the first alcoholysis kettle 02 through a pipeline, and the discharge outlet of the second delivery pump 14 is connected with the feed inlet of the second alcoholysis kettle 03 through a pipeline.
A third delivery pump 15, a second melt filter 16, an alcoholysis product transfer tank 17 and a fourth delivery pump 18 are sequentially connected in series on a pipeline connecting the second alcoholysis kettle 03 and the activated carbon adsorption device 04, specifically: the feed inlet of third delivery pump 15 passes through the pipeline and links to each other with the discharge gate of second glycolysis cauldron 03, the discharge gate of third delivery pump 15 passes through the pipeline and links to each other with the feed inlet of second fuse-element filter 16, the discharge gate of second fuse-element filter 16 passes through the pipeline and links to each other with the feed inlet of alcoholysis product transfer tank 17, the discharge gate of alcoholysis product transfer tank 17 passes through the pipeline and links to each other with the feed inlet of fourth delivery pump 18, the discharge gate of fourth delivery pump 18 passes through the pipeline and links to each other with the feed inlet of active carbon adsorption device 04. The second melt filter 16 is arranged between the second glycolysis kettle 03 and the activated carbon adsorption device 04, so that solid particles in a secondary alcoholysis product can be filtered, the adverse effect on subsequent decolorization and film evaporation is avoided, and the continuous operation of subsequent processes and the inhibition of side reactions are further guaranteed; in addition, an alcoholysis product transfer tank 17 is arranged between the second alcoholysis kettle 03 and the activated carbon adsorption device 04, so that on one hand, stable guarantee can be provided for continuous feeding of the activated carbon adsorption device 04, and on the other hand, the temperature of the alcoholysis product in the alcoholysis product transfer tank 17 can be adjusted from the alcoholysis reaction to the temperature suitable for thin film evaporation, and the influence on the operating efficiency of subsequent processes is avoided.
A first film evaporation product transfer tank 19 and a fifth delivery pump 20 are connected in series on a pipeline connecting the first film evaporator 05 and the second film evaporator 06, specifically: the feed inlet of the first film evaporation product transfer tank 19 is connected with the discharge outlet of the first film evaporator 05 through a pipeline, the discharge outlet of the first film evaporation product transfer tank 19 is connected with the feed inlet of the fifth delivery pump 20 through a pipeline, and the discharge outlet of the fifth delivery pump 20 is connected with the feed inlet of the second film evaporator 06 through a pipeline. By providing the first thin film evaporation product relay-tank 19 between the first thin film evaporator 05 and the second thin film evaporator 06, a stable guarantee can be provided for the continuous supply of the second thin film evaporator 06.
A second film evaporation product transfer tank 21 and a sixth delivery pump 22 are connected in series on a pipeline connecting the second film evaporator 06 and the molecular distiller 07, specifically: the feed inlet of the second film evaporation product transfer tank 21 is connected with the discharge outlet of the second film evaporator 06 through a pipeline, the discharge outlet of the second film evaporation product transfer tank 21 is connected with the feed inlet of a sixth delivery pump 22 through a pipeline, and the discharge outlet of the sixth delivery pump 22 is connected with the feed inlet of the molecular still 07 through a pipeline. By providing the second thin film evaporation product relay-tank 21 between the second thin film evaporator 06 and the molecular still 07, a stable guarantee can be provided for the continuous feeding of the molecular still 07.
A collecting and heat-preserving tank 23 for BHET monomer melt and a delivery pump 24 for BHET monomer melt are sequentially connected in series on a pipeline connecting a light component discharge port 07-2 of the molecular distiller 07 with the first pre-polycondensation reaction kettle 08, specifically: the feeding hole of the collecting and heat-insulating tank 23 of the BHET monomer melt is connected with the light component discharging hole 07-2 of the molecular distiller 07 through a pipeline, the discharging hole of the collecting and heat-insulating tank 23 of the BHET monomer melt is connected with the feeding hole of the conveying pump 24 of the BHET monomer melt through a pipeline, and the discharging hole of the conveying pump 24 of the BHET monomer melt is connected with the feeding hole of the first pre-polycondensation reaction kettle 08 through a pipeline. By arranging the collecting and heat-preserving tank 23 for the BHET monomer melt between the light component discharge port 07-2 of the molecular distiller 07 and the first pre-polycondensation reaction kettle 08, on one hand, stability guarantee can be provided for continuous feeding of the first pre-polycondensation reaction kettle 08, and on the other hand, heat-preserving storage is performed in the form of the BHET monomer melt, so that the BHET monomer melt can directly participate in subsequent pre-polycondensation reaction, heating energy consumption of the pre-polycondensation reaction can be obviously saved, the continuous production period can be shortened, and continuous feeding can be realized.
A seventh delivery pump 25 is connected in series on a pipeline between a heavy component discharge port 07-1 of the molecular distiller 07 and a return port 02-1 of the first alcoholysis kettle 02, and specifically: and a feed inlet of the seventh delivery pump 25 is connected with a heavy component discharge port 07-1 of the molecular still 07 through a pipeline, and a discharge port of the seventh delivery pump 25 is connected with a feed back port 02-1 of the first alcoholysis kettle 02 through a pipeline.
A pre-shrinking melt conveying pump 26 and a pre-shrinking melt filter 27 are connected in series on a pipeline connecting the second pre-polycondensation reaction kettle 09 and the final polycondensation reaction kettle 10 in sequence, specifically: the feeding hole of the pre-shrinking melt conveying pump 26 is connected with the discharging hole of the second pre-polycondensation reaction kettle 09 through a pipeline, the discharging hole of the pre-shrinking melt conveying pump 26 is connected with the feeding hole of the pre-shrinking melt filter 27 through a pipeline, and the discharging hole of the pre-shrinking melt filter 27 is connected with the feeding hole of the final polycondensation reaction kettle 10 through a pipeline. By arranging the pre-polycondensation melt filter 27 between the second pre-polycondensation reaction kettle 09 and the final polycondensation reaction kettle 10, solid particles in the pre-polycondensation product can be filtered out, so that adverse effects on the subsequent final polycondensation reaction can be avoided, and further guarantee effects on the continuous proceeding and side reaction inhibition of the subsequent process can be achieved.
A final-shrinkage melt conveying pump 28 and a final-shrinkage melt filter 29 are sequentially connected in series at a discharge port of the final-polycondensation reaction kettle 10, specifically: the feed inlet of the final-shrinkage melt conveying pump 28 is connected with the discharge outlet of the final-shrinkage polymerization reaction kettle 10 through a pipeline, and the discharge outlet of the final-shrinkage melt conveying pump 28 is connected with the feed inlet of the final-shrinkage melt filter 29 through a pipeline. The final polycondensation reaction kettle 10 is connected with the final polycondensation melt filter 29 in series at the discharge port, so that solid particles in the final polycondensation product can be filtered, the adverse effect on subsequent recycled polyester granulation is avoided, and the continuous feeding of the subsequent process is better ensured.
In addition, the discharge port of the final-shrinkage melt filter 29 may be connected to a subsequent polyester pelletizing system through a pipeline, and the polyester pelletizing system adopts the prior art, specifically: the polyester granulating system comprises a casting belt head 30, a granulator 31, a dryer 32, a vibrating screen 33 and a slicing bin 34; wherein, the discharge gate of final-shrinkage melt filter 29 links to each other with the feed inlet of casting belt head 30, the discharge gate of casting belt head 30 links to each other with the feed inlet of pelleter 31, the discharge gate of pelleter 31 links to each other with the feed inlet of desicator 32, the discharge gate of desicator 32 links to each other with the feed inlet of shale shaker 33, the discharge gate of shale shaker 33 links to each other with the feed inlet of section feed bin 34.
Adopt the utility model discloses foretell serialization production system is as follows by the production flow of old and useless polyester preparation regeneration polyester:
A) injecting the pretreated waste polyester into a screw extruder 01 from a waste polyester feeding bin 11, simultaneously injecting ethylene glycol which is 0.1-5% of the mass of the waste polyester into the screw extruder 01, and performing screw extrusion melting and pre-alcoholysis at 220-280 ℃;
B) filtering solids of the pre-alcoholysis solution output by the screw extruder 01 through a first melt filter 12, inputting the pre-alcoholysis solution into a first alcoholysis kettle 02 through a first conveying pump 13, simultaneously adding ethylene glycol 1-3 times of the mass of the waste polyester and an alcoholysis catalyst 0.1-1 per mill of the mass of the waste polyester into the first alcoholysis kettle 02, carrying out a primary alcoholysis reaction for 5-30 min at 220-260 ℃ and under the pressure of 0.1-0.5 MPa in the kettle, inputting the mixture into a second alcoholysis kettle 03 through a second conveying pump 14, and continuously carrying out a secondary alcoholysis reaction for 5-30 min at 220-260 ℃ and under the pressure of 0.1-0.5 MPa in the kettle;
C) sending the alcoholysis product subjected to secondary alcoholysis to a second melt filter 16 through a third conveying pump 15, filtering solids of the alcoholysis product through the second melt filter 16, sending the alcoholysis product to an alcoholysis product transfer tank 17, cooling the alcoholysis product in the alcoholysis product transfer tank 17 to 140-180 ℃, and sending the alcoholysis product to an activated carbon adsorption device 04 through a fourth conveying pump 18 for decolorization;
D) inputting the alcoholysis product subjected to the decoloring treatment into a first film evaporator 05, and performing film evaporation treatment at 140-180 ℃ and under the pressure of 100-1000 Pa for one time to remove most of ethylene glycol and low-boiling-point substances in the alcoholysis product, wherein the ethylene glycol and the low-boiling-point substances can be collected and condensed by a condenser and then recycled;
E) collecting the residual alcoholysis product subjected to the primary thin film evaporation treatment in a first thin film evaporation product transfer tank 19, inputting the product into a second thin film evaporator 06 through a fifth delivery pump 20, and performing secondary thin film evaporation treatment at 140-180 ℃ and under the pressure of 10-100 Pa to further remove glycol and low-boiling-point substances in the residual alcoholysis product subjected to the primary thin film evaporation treatment, wherein the glycol and the low-boiling-point substances can be collected and condensed by a condenser and recycled;
F) collecting the melt obtained by the secondary film evaporation treatment in a second film evaporation product transfer tank 21, inputting the melt into a molecular distiller 07 by a sixth delivery pump 22, and performing molecular distillation treatment at 190-250 ℃ and under the pressure of 1-100 Pa;
G) in the molecular distiller 07, the purified high-purity BHET monomer is gasified from an evaporation surface and condensed into liquid on a condenser arranged in the molecular distiller through a short stroke, enters a collecting and heat-preserving tank 23 of BHET monomer melt from a light component discharge port 07-2 of the molecular distiller 07 for storage, and is further conveyed into a first pre-polycondensation reaction kettle 08 by a conveying pump 24 of the BHET monomer melt; the remaining distillation residue flows along the evaporation surface into the heavy component outlet port 07-1 of the molecular still 07 and is conveyed by the seventh conveying pump 25 back to the first alcoholysis kettle 02 for cyclic alcoholysis;
H) carrying out primary pre-polycondensation reaction on the BHET monomer melt in a first pre-polycondensation reaction kettle 08 at 265-270 ℃ under the condition that the pressure in the kettle is 8-12 KPa to generate a first pre-polycondensation melt; the first pre-condensed melt continuously flows into a second pre-condensation polymerization reaction kettle 09 under the pressure transmission in a pipeline, and a secondary pre-condensation polymerization reaction is carried out at 272-275 ℃ and under the pressure of 1 KPa-1.5 KPa to generate a second pre-condensed melt; the second pre-condensed melt enters a final polycondensation reaction kettle 10 through a pre-condensed melt delivery pump 26 and a pre-condensed melt filter 27, and is subjected to final polycondensation reaction at 278-282 ℃ and under the pressure of 100-400 Pa to generate a final condensed melt; the final-shrinkage melt enters a casting head 30 through a final-shrinkage melt conveying pump 28 and a final-shrinkage melt filter 29;
I) the final-shrinkage melt becomes a plurality of polyester melt sample strips after flowing through the casting belt head 30, becomes a solid state after being cooled by a guide plate of the granulator 31, and is cut into chemically recycled polyester chips in a cutting chamber of the granulator 31; the chemical regeneration polyester chip enters a dryer 32 through a conveying pipeline, after moisture is removed in the dryer 32, the chemical regeneration polyester chip enters a vibrating screen 33 to remove abnormal chips, and finally the chemical regeneration polyester chip enters a chip storage bin 34.
From the above, it can be seen that: the continuous production system of the utility model, through setting up the screw extruder at the alcoholysis front end, make old and useless polyester material extrude melting and alcoholysis in advance in the screw extruder in advance to reduce the intrinsic viscosity of waiting to alcoholysis material, thereby not only realized the continuous feeding of alcoholysis reaction, realized moreover that the alcoholysis reaction can go on in the homogeneous system, and then accelerated the alcoholysis rate and shortened the alcoholysis reaction time, can effectively reduce the production of accessory substance, be favorable to obtaining high-purity BHET monomer; additionally, the utility model discloses a purification treatment of organic combination film evaporator and molecular still can realize making high-purity BHET monomer fuse-element by old and useless polyester high yield, and then can directly carry out the condensation polymerization reaction in advance, so not only practiced thrift the energy consumption, the complete serialization production of regeneration polyester has been realized, and simplified the preparation technology of regeneration polyester and obviously shortened the preparation cycle of regeneration polyester, the complete closed loop recycle of old and useless PET polyester has been realized, it has significant and practical value to realize the regeneration cyclic utilization of old and useless PET polyester in the true meaning.
Finally, it should be pointed out here that: the above is only a part of the preferred embodiments of the present invention, and it should not be understood as limiting the scope of the present invention, and the modifications and adjustments made by those skilled in the art according to the above-mentioned contents of the present invention are all included in the scope of the present invention.
Claims (10)
1. A continuous production system for preparing regenerated polyester from waste polyester is characterized in that: comprises a screw extruder, a first alcoholysis kettle, a second alcoholysis kettle, an activated carbon adsorption device, a first film evaporator, a second film evaporator, a molecular distiller, a first pre-polycondensation reaction kettle, a second pre-polycondensation reaction kettle and a final polycondensation reaction kettle which are sequentially connected in series through pipelines, wherein: and a light component discharge port of the molecular distiller is connected with a feed inlet of the first pre-polycondensation reaction kettle, and a heavy component discharge port of the molecular distiller is connected with a feed back port of the first alcoholysis kettle.
2. The continuous production system according to claim 1, wherein: the continuous production system further comprises a waste polyester feeding bin, and a discharge port of the waste polyester feeding bin is connected with a feed port of the screw extruder through a pipeline.
3. The continuous production system according to claim 1, wherein: the pipeline connecting the screw extruder and the first alcoholysis kettle is sequentially connected with a first melt filter and a first delivery pump in series, and the pipeline connecting the first alcoholysis kettle and the second alcoholysis kettle is connected with a second delivery pump in series.
4. The continuous production system according to claim 1, wherein: a third delivery pump, a second melt filter, an alcoholysis product transfer tank and a fourth delivery pump are sequentially connected in series on a pipeline connecting the second glycolysis kettle and the activated carbon adsorption device.
5. The continuous production system according to claim 1, wherein: a first film evaporation product transfer tank and a fifth delivery pump are connected in series on a pipeline connecting the first film evaporator and the second film evaporator in sequence.
6. The continuous production system according to claim 1, wherein: a second film evaporation product transfer tank and a sixth delivery pump are connected in series on a pipeline connecting the second film evaporator and the molecular distiller in sequence.
7. The continuous production system according to claim 1, wherein: a pipeline connecting a light component discharge port of the molecular distiller and the first pre-polycondensation reaction kettle is sequentially connected in series with a BHET monomer melt collecting and heat preserving tank and a BHET monomer melt delivery pump.
8. The continuous production system according to claim 1, wherein: a seventh delivery pump is connected in series on a pipeline between a heavy component discharge port of the molecular distiller and a feed back port of the first alcoholysis kettle.
9. The continuous production system according to claim 1, wherein: a pre-shrinking melt conveying pump and a pre-shrinking melt filter are sequentially connected in series on a pipeline connecting the second pre-polycondensation reaction kettle and the final polycondensation reaction kettle.
10. The continuous production system according to claim 1, wherein: a final-shrinkage melt conveying pump and a final-shrinkage melt filter are sequentially connected in series at a discharge port of the final-shrinkage polymerization reaction kettle.
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| CN202221360487.0U CN217516872U (en) | 2022-05-31 | 2022-05-31 | Continuous production system for preparing regenerated polyester from waste polyester |
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| CN202221360487.0U CN217516872U (en) | 2022-05-31 | 2022-05-31 | Continuous production system for preparing regenerated polyester from waste polyester |
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