CN113583227B - Production system of full-continuous degradable polyester - Google Patents
Production system of full-continuous degradable polyester Download PDFInfo
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- CN113583227B CN113583227B CN202110802677.7A CN202110802677A CN113583227B CN 113583227 B CN113583227 B CN 113583227B CN 202110802677 A CN202110802677 A CN 202110802677A CN 113583227 B CN113583227 B CN 113583227B
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- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
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- C08G63/785—Preparation processes characterised by the apparatus used
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention relates to a production system of fully continuous degradable polyester, which comprises a batching and pulping kettle, a multifunctional tower reactor, a final polycondensation reactor and a granulating system. The material mixing and pulping kettle is connected with an aromatic dibasic acid and/or aliphatic dibasic acid bin, the bottom of the material mixing and pulping kettle is connected with the bottom of a heat exchanger through a slurry conveying pump, the heat exchanger is communicated with a multifunctional tower reactor through a pipeline, the upper part of the multifunctional tower reactor is connected with a process tower, the lower part of the multifunctional tower reactor is connected with a final polycondensation reactor through a pipeline, the final polycondensation reactor is connected with a final polymer filter through a melt conveying pump, and the final polymer filter is connected with a granulating system. The invention is applicable to degradable aromatic-aliphatic polyesters and degradable aliphatic polyesters. The invention has the advantages of reasonable process, high efficiency, energy saving, high continuous automation degree, small equipment investment and occupied area, stable product quality and high uniformity.
Description
Technical Field
The invention relates to a production system of full-continuous degradable polyester, and belongs to the technical field of production of full-continuous degradable polyester.
Background
In recent years, with the improvement of environmental awareness of people, related regulations are continuously formulated and brought out worldwide, and the use of non-degradable plastics is limited by means of local forbidden, limited, forced collection, collection of pollution tax collection and other measures, so that new degradable materials are greatly developed to protect the environment. The traditional polyester is undegradable, so that serious white pollution is caused in the nature, and the degradable polyester gradually becomes a hot spot in the chemical fiber industry. The degradable polyester not only has good thermal stability and mechanical properties, but also has good extensibility and tensile properties. The benzene ring of rigid group is reduced/eliminated in the molecular chain of degradable polyester, the fatty carbon chain and ester bond which is easier to hydrolyze are added, the flexibility of the molecular chain is enhanced, and the degradable polyester can be degraded into carbon dioxide, water and some small molecular compounds under the action of microorganisms under the aerobic or anaerobic condition.
At present, the production process method for preparing the degradable polyester is known and is basically realized through a 3-5 kettle process flow, wherein the esterification reaction and the pre-polycondensation reaction are all carried out in a single reactor, the material residence time is long, the inevitable side reaction is aggravated, the energy consumption is high, and the equipment investment and the maintenance cost are high.
Disclosure of Invention
The invention aims to solve the existing problems and provides a production system of fully-continuous degradable polyester.
The technical scheme of the invention is as follows: a production system of fully continuous degradable polyester comprises a batching and pulping system, an esterification reaction system, a pre-polycondensation reaction system, a final polycondensation reaction system and a granulating system, wherein the batching and pulping system is used for pulping aromatic dibasic acid and/or aliphatic dibasic acid raw materials; the method is characterized in that:
the batching and pulping system comprises an aliphatic dibasic acid bin, an aromatic dibasic acid bin, an aliphatic dibasic acid metering device, an aromatic dibasic acid metering device and a pulping kettle; the aliphatic dibasic acid bin and the aromatic dibasic acid bin are arranged in left-right alignment; the aliphatic dibasic acid metering device is arranged at the outlet of the aliphatic dibasic acid bin, and the aromatic dibasic acid metering device is arranged at the outlet of the aromatic dibasic acid bin; the top of the beating kettle is respectively communicated with the aliphatic dibasic acid metering device and the aromatic dibasic acid metering device through pipelines;
the esterification reaction system comprises a multifunctional tower reactor esterification chamber, a process tower, a recycling aliphatic diol pump and a heat exchanger; the heat exchanger is positioned on the right side of the beating kettle, and the beating kettle is communicated with the left side of the heat exchanger through a slurry conveying pump; the multifunctional tower reactor esterification chamber is positioned at the upper part of the multifunctional tower reactor, the bottom of the heat exchanger is communicated with the lower part of the multifunctional tower reactor esterification chamber through a pipeline, and the right side of the heat exchanger is communicated with the upper part of the multifunctional tower reactor esterification chamber; the process tower is arranged on the right side of the multifunctional tower reactor, and the top of the esterification chamber of the multifunctional tower reactor is communicated with the middle part of the process tower through a pipeline; the recycling aliphatic diol pump is arranged under the process tower and is communicated with the esterification chamber of the multifunctional tower reactor through the recycling aliphatic diol pump;
the pre-polycondensation reaction system comprises a multi-functional tower reactor pre-polycondensation chamber, a flow regulating valve, a pre-polycondensation condenser and a di-polycondensation condenser; the multifunctional tower reactor pre-condensation chamber is positioned at the middle lower part of the multifunctional tower reactor and is communicated with the multifunctional tower reactor esterification chamber at the upper part of the multifunctional tower reactor through an external esterification flow regulating valve of the multifunctional tower reactor; the pre-polycondensation condenser and the secondary polycondensation condenser are arranged on the right side of the multifunctional tower reactor and are communicated with a pre-polycondensation chamber of the multifunctional tower reactor;
the final polycondensation reaction system comprises a final polycondensation reactor, a final polycondensation condenser, a melt conveying pump and a melt filter; the final polycondensation reactor is arranged on the right side of the multifunctional tower reactor, and a prepolymer outlet at the bottom of the multifunctional tower reactor is communicated with a prepolymer inlet at the bottom of the front end of the final polycondensation reactor; the final polycondensation condenser is arranged above the final polycondensation reactor and is communicated with a gas phase outlet at the upper part of the rear end of the final polycondensation reactor; the melt conveying pump is arranged right below the rear end of the final polycondensation reactor, and a melt outlet at the lower part of the rear end of the final polycondensation reactor is communicated with the melt filter through the melt conveying pump and a pipeline;
the melt filter is connected to the pelletizing system via a pipe.
The esterification chamber and the precondensation chamber of the multifunctional tower reactor are arranged from bottom to top or from top to bottom;
when the multifunctional tower reactor esterification chamber and the multifunctional tower reactor pre-polycondensation chamber are arranged from top to bottom, the multifunctional tower reactor esterification chamber and the multifunctional tower reactor pre-polycondensation chamber are respectively arranged in the multifunctional tower reactor, the multifunctional tower reactor esterification chamber and the multifunctional tower reactor pre-polycondensation chamber are arranged from top to bottom, the temperature of the multifunctional tower reactor is gradually increased from top to bottom, and the absolute pressure is gradually reduced.
When the device is used, the aliphatic dibasic acid and the aromatic dibasic acid are respectively added into the beating kettle after passing through the aliphatic dibasic acid metering device and the aromatic dibasic acid metering device according to the set required proportion, so that the mixing and beating are realized.
The multifunctional tower reactor esterification chamber is not limited to one reaction chamber, and a plurality of multifunctional tower reactor esterification reaction chambers can be sequentially arranged from top to bottom; the esterification catalyst and the heat stabilizer adding port are arranged on a pipeline, the bottom of the heat exchanger is communicated with the lower part of the esterification chamber of the multifunctional tower reactor, so that the catalyst is uniformly dispersed, and the hydrolysis failure of the esterification catalyst is avoided;
the process tower is communicated with the vacuum system through an esterification gas phase pipeline and is used for separating water vapor, micromolecular esterification byproducts and aliphatic dihydric alcohol generated by the esterification reaction, and the water vapor and the micromolecular esterification byproducts are discharged from the top of the process tower and are sent to a byproduct recovery system;
the heat exchanger is a tube type heat exchanger.
The pre-polycondensation chamber of the multifunctional tower reactor is sequentially provided with an overflow type tray reaction zone, a depressurization reaction zone, a prepolymer heating reaction zone and a prepolymer baffling reaction zone from top to bottom, and the overflow type tray reaction zone is communicated with the depressurization reaction zone through an external flow regulating valve of the multifunctional tower reactor; a polycondensation catalyst is arranged on a pipeline communicated with the overflow type tray reaction zone and the depressurization reaction zone; the pre-condensation condenser is communicated with a vacuum system through a pre-condensation vacuum pipeline; the connecting port of the precondensation condenser and the multifunctional tower reactor is positioned between the overflow type tray reaction zone and the prepolymer baffling reaction zone; the second polycondensation condenser is communicated with the vacuum system through a second polycondensation gas phase pipeline, and a connecting port of the second polycondensation condenser and the multifunctional tower reactor is positioned between the prepolymer heating reaction zone and the prepolymer baffling reaction zone.
The final polycondensation reactor is a horizontal double-shaft stirring vacuum reactor; the final polycondensation condenser is communicated with a vacuum system through a final polycondensation gas phase pipeline.
The overflow type tray reaction zone is provided with a plurality of reaction trays, and each reaction tray is communicated with each other through a material pipeline perpendicular to the reaction tray; each reaction tray is provided with a first overflow weir and a gas phase pipe, the gas phase pipe is vertically arranged inside the first overflow weir, the top of the gas phase pipe is lower than a connecting port of the multifunctional tower reactor and the precondensation condenser and higher than a first overflow weir plate, and the bottom of the gas phase pipe is kept at a distance from the bottom of the first overflow weir;
the depressurization reaction zone is provided with a baffle plate, and a plurality of annular guide plates are arranged on the baffle plate;
the prepolymer heating reaction zone is provided with a plurality of tubes, the tops of the tubes are all at the same horizontal plane, and each tube is provided with a second overflow weir;
the prepolymer baffling reaction zone is provided with a plurality of groups of symmetrical baffle plates, a third overflow weir is arranged at the top end of each baffle plate, annular baffle plates are arranged between each layer of baffle plates, and a precondensation condenser and a multifunctional tower reactor connecting port are arranged between the bottommost baffle plate and the annular baffle plates below the baffle plates.
The aromatic dibasic acid bin is communicated with the pulping kettle through an aromatic dibasic acid feeding pipeline;
the aliphatic dibasic acid bin is communicated with the pulping kettle through an aliphatic dibasic acid feeding pipeline;
the beating kettle is also connected with an aliphatic dihydric alcohol feeding pipeline;
the esterification catalyst and heat stabilizer adding port is connected with an esterification catalyst adding pipeline and a heat stabilizer adding pipeline;
and a polycondensation catalyst adding pipeline is arranged on a pipeline communicated with the overflow type tray reaction zone and the depressurization reaction zone.
The granulating system comprises a reversing valve, a cutting chamber, a template, a granulator with a driving system, a cooling pipeline, a dryer and a vibrating screen.
The invention has reasonable combination and convenient use, and the full-continuous degradable polyester production system provided by the invention has the following advantages:
1. the two-kettle mode is adopted, the esterification reaction and the pre-polycondensation reaction are carried out in a multifunctional tower reactor, the occupied area of equipment is small, the equipment investment is small, and the later maintenance is convenient;
2. the two-kettle mode is adopted, the material residence time is short, and the side reaction degree is small;
3. realizes continuous production of the degradable polyester, and has simple and convenient method, high efficiency, energy conservation and controllability.
In summary, the invention provides a production system of fully continuous degradable polyester, which comprises a batching and pulping kettle, a multifunctional tower reactor, a final polycondensation reactor and a granulating system. The material mixing and pulping kettle is connected with an aromatic dibasic acid and/or aliphatic dibasic acid bin, the bottom of the material mixing and pulping kettle is connected with the bottom of a heat exchanger through a slurry conveying pump, the heat exchanger is communicated with a multifunctional tower reactor through a pipeline, the upper part of the multifunctional tower reactor is connected with a process tower, the lower part of the multifunctional tower reactor is connected with a final polycondensation reactor through a pipeline, the final polycondensation reactor is connected with a final polymer filter through a melt conveying pump, and the final polymer filter is connected with a granulating system. The invention is applicable to degradable aromatic-aliphatic polyesters and degradable aliphatic polyesters. The invention has the advantages of reasonable process, high efficiency, energy saving, high continuous automation degree, small equipment investment and occupied area, stable product quality and high uniformity.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention;
wherein, 1 beating kettle, 2 heat exchanger, 3-1 multifunctional tower reactor esterifying chamber, 3-2 overflow tray reaction zone, 3-3 depressurization reaction zone, 3-4 prepolymer heating reaction zone, 3-5 prepolymer baffling reaction zone, 4 process tower, 5 pre-polycondensation condenser, 6 di-polycondensation condenser, 7 final polycondensation condenser, 8 final polycondensation reactor, 9 melt transfer pump, 10 melt filter, 11 particle cutting system, a aromatic diacid feed line, b aliphatic diacid feed line, c aliphatic diol feed line, d esterification catalyst addition line, e heat stabilizer addition line, f polymerization catalyst addition line, g1 esterification gas phase line, g2 pre-polycondensation vacuum line, g3 di-polycondensation gas phase line, g4 final polycondensation gas phase line.
Detailed description of the preferred embodiments
The invention is further described below in connection with specific embodiments. The scope of the invention is not limited in this regard:
a production system of fully continuous degradable polyester comprises a batching and pulping system, an esterification reaction system, a pre-polycondensation reaction system, a final polycondensation reaction system and a granulating system 11, wherein the batching and pulping system is used for pulping aromatic dibasic acid and/or aliphatic dibasic acid raw materials; the batching and pulping system comprises an aliphatic dibasic acid bin, an aromatic dibasic acid bin, an aliphatic dibasic acid metering device, an aromatic dibasic acid metering device and a pulping kettle 1; the aliphatic dibasic acid bin and the aromatic dibasic acid bin are arranged in left-right alignment; the aliphatic dibasic acid metering device is arranged at the outlet of the aliphatic dibasic acid bin, and the aromatic dibasic acid metering device is arranged at the outlet of the aromatic dibasic acid bin; the top of the beating kettle 1 is respectively communicated with an aliphatic dibasic acid metering device and an aromatic dibasic acid metering device through pipelines.
The esterification reaction system comprises a multifunctional tower reactor esterification chamber 3-1, a process tower 4, a recycling aliphatic diol pump and a heat exchanger 2; the heat exchanger 2 is positioned on the right side of the beating kettle 1, and the beating kettle 1 is communicated with the left side of the heat exchanger 2 through a slurry conveying pump; the multifunctional tower reactor esterification chamber 3-1 is positioned at the upper part of the multifunctional tower reactor, the bottom of the heat exchanger 2 is communicated with the lower part of the multifunctional tower reactor esterification chamber 3-1 through a pipeline, and the right side of the heat exchanger 2 is communicated with the upper part of the multifunctional tower reactor esterification chamber 3-1; the process tower 4 is arranged on the right side of the multifunctional tower reactor, and the top of the esterification chamber 3-1 of the multifunctional tower reactor is communicated with the middle part of the process tower 4 through a pipeline; the recycling aliphatic diol pump is arranged under the process tower 4 and is communicated with the esterification chamber 3-1 of the multifunctional tower reactor through the recycling aliphatic diol pump.
The pre-polycondensation reaction system comprises a multi-functional tower reactor pre-polycondensation chamber, a flow regulating valve, a pre-polycondensation condenser 5 and a di-polycondensation condenser 6; the pre-condensing chamber of the multifunctional tower reactor is positioned at the middle lower part of the multifunctional tower reactor and is communicated with the esterification chamber 3-1 of the multifunctional tower reactor at the upper part of the multifunctional tower reactor through an external esterification flow regulating valve of the multifunctional tower reactor; the prepolycondensation condenser 5 and the two-condensation condenser 6 are arranged on the right side of the multifunctional tower reactor, and the prepolycondensation condenser 5 and the two-condensation condenser 6 are communicated with a prepolycondensation chamber of the multifunctional tower reactor;
the final polycondensation reaction system comprises a final polycondensation reactor 8, a final polycondensation condenser 7, a melt conveying pump 9 and a melt filter 10; the final polycondensation reactor 8 is arranged on the right side of the multifunctional tower reactor, and a prepolymer outlet at the bottom of the multifunctional tower reactor is communicated with a prepolymer inlet at the bottom of the front end of the final polycondensation reactor 8; a final polycondensation condenser 7 is arranged above the final polycondensation reactor 8, and the final polycondensation condenser 7 is communicated with a gas phase outlet at the upper part of the rear end of the final polycondensation reactor 8; the melt conveying pump 9 is arranged right below the rear end of the final polycondensation reactor 8, and a melt outlet at the lower part of the rear end of the final polycondensation reactor 8 is communicated with the melt filter 10 through the melt conveying pump 9 and a pipeline; the melt filter 10 is connected to a pelletizing system 11 via a pipe.
Further, the esterification chamber 3-1 of the multifunctional tower reactor and the precondensation chamber of the multifunctional tower reactor are arranged from bottom to top or from top to bottom; when the multifunctional tower reactor esterification chamber 3-1 and the multifunctional tower reactor pre-polycondensation chamber are arranged from top to bottom, the multifunctional tower reactor esterification chamber 3-1 and the multifunctional tower reactor pre-polycondensation chamber are uniformly arranged in the multifunctional tower reactor, the multifunctional tower reactor esterification chamber 3-1 and the multifunctional tower reactor pre-polycondensation chamber are arranged from top to bottom, the temperature of the multifunctional tower reactor is gradually increased from top to bottom, and the absolute pressure is gradually reduced.
When the device is used, the aliphatic dibasic acid and the aromatic dibasic acid are respectively added into the beating kettle 1 after passing through the aliphatic dibasic acid metering device and the aromatic dibasic acid metering device according to the set required proportion with the aliphatic dibasic alcohol, so that the mixing and beating are realized.
The multifunctional tower reactor esterification chamber 3-1 is not limited to one reaction chamber, and a plurality of multifunctional tower reactor esterification reaction chambers 3-1 can be sequentially arranged from top to bottom; the esterification catalyst and the heat stabilizer adding port are arranged on a pipeline which is communicated with the lower part of the esterification chamber 3-1 of the multifunctional tower reactor at the bottom of the heat exchanger 2, so that the catalyst is uniformly dispersed, and the hydrolysis failure of the esterification catalyst is avoided; the process tower 4 is communicated with a vacuum system through an esterification gas phase pipeline g1, the process tower 4 is used for separating water vapor, micromolecular esterification byproducts and aliphatic dihydric alcohol generated by the esterification reaction, and the water vapor and the micromolecular esterification byproducts are discharged from the top of the process tower and are sent to a byproduct recovery system; the heat exchanger 2 is a tube type heat exchanger.
The pre-polycondensation chamber of the multifunctional tower reactor is sequentially provided with an overflow type tray reaction zone 3-2, a depressurization reaction zone 3-3, a prepolymer heating reaction zone 3-4 and a prepolymer baffling reaction zone 3-5 from top to bottom, wherein the overflow type tray reaction zone 3-2 is communicated with the depressurization reaction zone 3-3 through an external flow regulating valve of the multifunctional tower reactor; a polycondensation catalyst is arranged on a pipeline communicated with the overflow type tray reaction zone 3-2 and the depressurization reaction zone 3-3; the pre-condensation condenser 5 is communicated with a vacuum system through a pre-condensation vacuum pipeline g 2; the connecting port of the prepolycondensation condenser 5 and the multifunctional tower reactor is positioned between the overflow type tray reaction zone 3-2 and the prepolymer baffling reaction zone 3-5; the di-polycondensation condenser 6 is communicated with a vacuum system through a di-polycondensation gas phase pipeline g3, and a connecting port of the di-polycondensation condenser 6 and the multifunctional tower reactor is positioned between the prepolymer heating reaction zone 3-4 and the prepolymer baffling reaction zone 3-5.
The final polycondensation reactor 8 is a horizontal double-shaft stirring vacuum reactor; the final polycondensation condenser 7 is communicated with a vacuum system through a final polycondensation gas phase line g 4.
The overflow type tray reaction zone 3-2 is provided with a plurality of reaction trays, and each reaction tray is communicated with each other through a material pipeline perpendicular to the reaction tray; each reaction tray is provided with a first overflow weir and a gas phase pipe, the gas phase pipe is vertically arranged inside the first overflow weir, the top of the gas phase pipe is lower than a connecting port of the multifunctional tower reactor and the precondensation condenser 5 and higher than a first overflow weir plate, and the bottom of the gas phase pipe is kept at a distance from the bottom of the first overflow weir;
the depressurization reaction zone 3-3 is provided with a baffle plate, and a plurality of annular guide plates are arranged on the baffle plate;
the prepolymer heating reaction zone 3-4 is provided with a plurality of tubes, the tops of the tubes are all at the same horizontal plane, and each tube is provided with a second overflow weir;
the prepolymer baffling reaction zone 3-5 is provided with a plurality of groups of symmetrical baffle plates, the top ends of the baffle plates are provided with a third overflow weir, annular baffle plates are arranged between each layer of baffle plates, and a precondensation condenser 5 and a multifunctional tower reactor connecting port are arranged between the bottommost baffle plate and the annular baffle plates below the baffle plates.
The aromatic dibasic acid bin is communicated with the pulping kettle 1 through an aromatic dibasic acid feeding pipeline a; the aliphatic dibasic acid bin is communicated with the pulping kettle 1 through an aliphatic dibasic acid feeding pipeline b; the pulping kettle 1 is also connected with an aliphatic dihydric alcohol feeding pipeline c; the esterification catalyst and heat stabilizer adding port is connected with an esterification catalyst adding pipeline d and a heat stabilizer adding pipeline e;
and a polycondensation catalyst adding pipeline f is arranged on a pipeline communicated with the overflow type tray reaction zone 3-2 and the depressurization reaction zone 3-3.
The invention is not limited to the two-kettle device consisting of the multifunctional tower reactor and the final polycondensation reactor, and on the basis of the device, the technical characteristics of the invention are modified and replaced by the technical personnel without creative labor, and the modification and the replacement are included in the protection scope of the invention.
Claims (4)
1. A production system of fully continuous degradable polyester comprises a batching and pulping system, an esterification reaction system, a pre-polycondensation reaction system, a final polycondensation reaction system and a granulating system (11) which are used for pulping aromatic dibasic acid and/or aliphatic dibasic acid raw materials; the method is characterized in that:
the batching and pulping system comprises an aliphatic dibasic acid bin, an aromatic dibasic acid bin, an aliphatic dibasic acid metering device, an aromatic dibasic acid metering device and a pulping kettle (1); the aliphatic dibasic acid bin and the aromatic dibasic acid bin are arranged in left-right alignment; the aliphatic dibasic acid metering device is arranged at the outlet of the aliphatic dibasic acid bin, and the aromatic dibasic acid metering device is arranged at the outlet of the aromatic dibasic acid bin; the top of the beating kettle (1) is respectively communicated with an aliphatic dibasic acid metering device and an aromatic dibasic acid metering device through pipelines;
the esterification reaction system comprises a multifunctional tower reactor esterification chamber (3-1), a process tower (4), a recycling aliphatic diol pump and a heat exchanger (2); the heat exchanger (2) is positioned on the right side of the beating kettle (1), and the beating kettle (1) is communicated with the left side of the heat exchanger (2) through a slurry conveying pump; the multifunctional tower reactor esterification chamber (3-1) is positioned at the upper part of the multifunctional tower reactor, the bottom of the heat exchanger (2) is communicated with the lower part of the multifunctional tower reactor esterification chamber (3-1) through a pipeline, and the right side of the heat exchanger (2) is communicated with the upper part of the multifunctional tower reactor esterification chamber (3-1); the process tower (4) is arranged on the right side of the multifunctional tower reactor, and the top of the esterification chamber (3-1) of the multifunctional tower reactor is communicated with the middle part of the process tower (4) through a pipeline; the recycling aliphatic diol pump is arranged under the process tower (4) and is communicated with the esterification chamber (3-1) of the multifunctional tower reactor through the recycling aliphatic diol pump;
the pre-polycondensation reaction system comprises a multi-functional tower reactor pre-polycondensation chamber, a flow regulating valve, a pre-polycondensation condenser (5) and a di-polycondensation condenser (6); the pre-condensing chamber of the multifunctional tower reactor is positioned at the middle lower part of the multifunctional tower reactor and is communicated with the esterification chamber (3-1) of the multifunctional tower reactor at the upper part of the multifunctional tower reactor through an external esterification flow regulating valve of the multifunctional tower reactor; the prepolycondensation condenser (5) and the two-condensation condenser (6) are arranged on the right side of the multifunctional tower reactor, and the prepolycondensation condenser (5) and the two-condensation condenser (6) are communicated with a prepolycondensation chamber of the multifunctional tower reactor;
the final polycondensation reaction system comprises a final polycondensation reactor (8), a final polycondensation condenser (7), a melt conveying pump (9) and a melt filter (10); the final polycondensation reactor (8) is arranged on the right side of the multifunctional tower reactor, and the prepolymer outlet at the bottom of the multifunctional tower reactor is communicated with the prepolymer inlet at the bottom of the front end of the final polycondensation reactor (8); the final polycondensation condenser (7) is arranged above the final polycondensation reactor (8), and the final polycondensation condenser (7) is communicated with a gas phase outlet at the upper part of the rear end of the final polycondensation reactor (8); the melt conveying pump (9) is arranged right below the rear end of the final polycondensation reactor (8), and a melt outlet at the lower part of the rear end of the final polycondensation reactor (8) is communicated with the melt filter (10) through the melt conveying pump (9) and a pipeline;
the melt filter (10) is connected with the granulating system (11) through a pipeline;
the esterification chamber (3-1) of the multifunctional tower reactor and the precondensation chamber of the multifunctional tower reactor are arranged from bottom to top or from top to bottom;
when the multifunctional tower reactor esterification chamber (3-1) and the multifunctional tower reactor pre-polycondensation chamber are arranged from top to bottom, the multifunctional tower reactor esterification chamber (3-1) and the multifunctional tower reactor pre-polycondensation chamber are all arranged in the multifunctional tower reactor, the multifunctional tower reactor esterification chamber (3-1) and the multifunctional tower reactor pre-polycondensation chamber are arranged from top to bottom, the temperature of the multifunctional tower reactor is gradually increased from top to bottom, and the absolute pressure is gradually reduced;
the pre-polycondensation chamber of the multifunctional tower reactor is sequentially provided with an overflow type tray reaction zone (3-2), a depressurization reaction zone (3-3), a prepolymer heating reaction zone (3-4) and a prepolymer baffling reaction zone (3-5) from top to bottom, wherein the overflow type tray reaction zone (3-2) is communicated with the depressurization reaction zone (3-3) through an external flow regulating valve of the multifunctional tower reactor; a polycondensation catalyst is arranged on a pipeline communicated with the overflow type tray reaction zone (3-2) and the depressurization reaction zone (3-3); the pre-condensation condenser (5) is communicated with a vacuum system through a pre-condensation vacuum pipeline (g 2); the connecting port of the precondensation condenser (5) and the multifunctional tower reactor is positioned between the overflow tray reaction zone (3-2) and the prepolymer baffling reaction zone (3-5); the second polycondensation condenser (6) is communicated with the vacuum system through a second polycondensation gas phase pipeline (g 3), and a connecting port of the second polycondensation condenser (6) and the multifunctional tower reactor is positioned between the prepolymer heating reaction zone (3-4) and the prepolymer baffling reaction zone (3-5);
the overflow type tray reaction zone (3-2) is provided with a plurality of reaction trays, and each reaction tray is communicated with each other through a material pipeline vertical to the reaction tray; each reaction tray is provided with a first overflow weir and a gas phase pipe, the gas phase pipe is vertically arranged inside the first overflow weir, the top of the gas phase pipe is lower than a connecting port of the multifunctional tower reactor and the precondensation condenser (5), and is higher than a first overflow weir plate, and the bottom of the gas phase pipe is kept at a distance from the bottom of the first overflow weir;
the depressurization reaction zone (3-3) is provided with a baffle plate, and a plurality of annular guide plates are arranged on the baffle plate;
the prepolymer heating reaction zone (3-4) is provided with a plurality of tubes, the tops of the tubes are all at the same horizontal plane, and each tube is provided with a second overflow weir;
the prepolymer baffling reaction zone (3-5) is provided with a plurality of groups of symmetrical baffle plates, a third overflow weir is arranged at the top end of each baffle plate, annular baffle plates are arranged between each layer of baffle plates, and a precondensation condenser (5) and a multifunctional tower reactor connecting port are arranged between the bottommost baffle plate and the annular baffle plates below the baffle plates;
the aromatic dibasic acid bin is in through connection with the pulping kettle (1) through an aromatic dibasic acid feeding pipeline (a);
the aliphatic dibasic acid bin is in through connection with the pulping kettle (1) through an aliphatic dibasic acid feeding pipeline (b);
the pulping kettle (1) is also connected with an aliphatic dihydric alcohol feeding pipeline (c);
the esterification catalyst and heat stabilizer adding port is connected with an esterification catalyst adding pipeline (d) and a heat stabilizer adding pipeline (e);
and a polycondensation catalyst adding pipeline (f) is arranged on a pipeline communicated with the overflow type tray reaction zone (3-2) and the depressurization reaction zone (3-3).
2. The system for producing fully continuous degradable polyester according to claim 1, wherein: when the device is used, the aliphatic dibasic acid and the aromatic dibasic acid are respectively added into the beating kettle (1) after passing through the aliphatic dibasic acid metering device and the aromatic dibasic acid metering device according to the set required proportion, so that the mixing and beating are realized.
3. The system for producing fully continuous degradable polyester according to claim 1, wherein: the multifunctional tower reactor esterification chamber (3-1) is not limited to one reaction chamber, and a plurality of multifunctional tower reactor esterification reaction chambers (3-1) can be sequentially arranged from top to bottom; the esterification catalyst and the heat stabilizer adding port are arranged on a pipeline, the bottom of the heat exchanger (2) is communicated with the lower part of the esterification chamber (3-1) of the multifunctional tower reactor, so that the catalyst is uniformly dispersed, and the hydrolysis failure of the esterification catalyst is avoided;
the process tower (4) is communicated with a vacuum system through an esterification gas phase pipeline (g 1), the process tower (4) is used for separating water vapor, micromolecular esterification byproducts and aliphatic dihydric alcohol generated by the esterification reaction, and the water vapor and the micromolecular esterification byproducts are discharged from the top of the process tower and are sent to a byproduct recovery system;
the heat exchanger (2) is a tube type heat exchanger.
4. The system for producing fully continuous degradable polyester according to claim 1, wherein: the final polycondensation reactor (8) is a horizontal double-shaft stirring vacuum reactor; the final polycondensation condenser (7) is communicated with a vacuum system through a final polycondensation gas phase pipeline (g 4).
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| US5786443A (en) * | 1995-12-14 | 1998-07-28 | E. I. Du Pont De Nemours And Company | Process of making polyester prepolymer |
| DE10155419B4 (en) * | 2001-11-12 | 2005-06-16 | Inventa-Fischer Gmbh & Co. Kg | Process for the continuous production of high molecular weight polyester and apparatus for carrying out the process |
| DE10246251A1 (en) * | 2002-10-02 | 2004-04-15 | Zimmer Ag | Continuous production of polyesters by the (trans)esterification of dicarboxylic acids, comprises use of a vertical reactor having three reaction zones with a pressure of 10-40% of the diol equilibrium pressure |
| DE10351085A1 (en) * | 2003-10-31 | 2005-06-16 | Inventa-Fischer Gmbh & Co. Kg | Tower reactor and its use for the continuous production of high molecular weight polyester |
| CN102585191B (en) * | 2012-01-13 | 2014-10-22 | 华东理工大学 | Novel tower reactor and application of novel tower reactor in continuously producing polyester polyol |
| CN210945446U (en) * | 2019-11-14 | 2020-07-07 | 扬州普立特科技发展有限公司 | Full-continuous PBAT production equipment |
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| CN111423570B (en) * | 2020-05-20 | 2023-06-06 | 北京芯友工程技术有限公司 | Process and device for continuously producing degradable polyester |
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