阅读说明：本技术 一种全连续可降解聚酯的生产系统 (Full-continuous production system of degradable polyester ) 是由 肖洪卫 成强 张昕 于 2021-07-15 设计创作，主要内容包括：本发明涉及一种全连续可降解聚酯的生产系统,包括配料打浆釜、多功能塔式反应器、终缩聚反应器、切粒系统。配料打浆釜与芳香族二元酸和/或脂肪族二元酸料仓相连,配料打浆釜底部通过浆料输送泵与换热器底部相连,换热器与多功能塔式反应器通过管道连通,多功能塔式反应器上部与工艺塔相连,多功能塔式反应器下部通过管道与终缩聚反应器相连,终缩聚反应器通过熔体输送泵与终聚物过滤器相连,终聚物过滤器与切粒系统相连。本发明适用于可降解芳香族-脂肪族聚酯及可降解脂肪族聚酯。通过本发明,工艺流程为两釜流程,工艺合理、高效、节能,连续自动化程度高,设备投资及占地面积小、产品质量稳定均一性高。(The invention relates to a full-continuous production system of degradable polyester, which comprises a batching and pulping kettle, a multifunctional tower reactor, a final polycondensation reactor and a pelletizing system. The batching and pulping kettle is connected with an aromatic dibasic acid and/or aliphatic dibasic acid bin, the bottom of the batching and pulping kettle is connected with the bottom of a heat exchanger through a slurry delivery 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 delivery pump, and the final polymer filter is connected with a pelletizing system. The invention is suitable for degradable aromatic-aliphatic polyester and degradable aliphatic polyester. 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.)

1. A production system of full-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 a left-right alignment way; the aliphatic dibasic acid metering device is arranged at an outlet of the aliphatic dibasic acid bin, and the aromatic dibasic acid metering device is arranged at an outlet of the aromatic dibasic acid bin; the top of the pulping 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 pulping kettle (1), and the pulping kettle (1) is communicated with the left side of the heat exchanger (2) through a pulp delivery 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 at 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 right below the process tower (4) and is communicated with the multifunctional tower reactor esterification chamber (3-1) through the recycling aliphatic diol pump;

the pre-polycondensation reaction system comprises a multifunctional tower type reactor pre-polycondensation chamber, a flow regulating valve, a pre-polycondensation condenser (5) and a secondary polycondensation condenser (6); the multifunctional tower reactor pre-polycondensation chamber is positioned at the middle lower part of the multifunctional tower reactor and is communicated with the multifunctional tower reactor esterification chamber (3-1) at the upper part of the multifunctional tower reactor through an external ester flow regulating valve of the multifunctional tower reactor; the pre-condensation condenser (5) and the secondary condensation condenser (6) are arranged on the right side of the multifunctional tower reactor, and the pre-condensation condenser (5) and the secondary condensation condenser (6) are communicated with a pre-condensation 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); the final condensation condenser (7) is arranged above the final condensation reactor (8), and the final condensation condenser (7) is communicated with a gas phase outlet at the upper part of the rear end of the final condensation 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.

2. The system for producing fully continuous degradable polyester according to claim 1, wherein: the multifunctional tower reactor esterification chamber (3-1) and the multifunctional tower reactor pre-polycondensation chamber 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 both 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 from top to bottom gradually rises, and the absolute pressure of the multifunctional tower reactor gradually falls.

3. The system for producing fully continuous degradable polyester according to claim 1, wherein: when in use, the aliphatic dibasic acid and the aromatic dibasic acid are respectively added into the pulping kettle (1) together with the aliphatic dibasic alcohol according to the proportion required by setting after passing through the aliphatic dibasic acid metering device and the aromatic dibasic acid metering device, so as to realize batching and pulping.

4. 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; an esterification catalyst and a heat stabilizer adding port are arranged on a pipeline 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 (g 1), the process tower (4) is used for separating water vapor, micromolecule esterification byproducts and aliphatic diol generated by esterification reaction, and the water vapor and the micromolecule esterification byproducts are discharged from the top of the process tower and sent to a byproduct recovery system;

the heat exchanger (2) is a shell and tube heat exchanger.

5. The system for producing fully continuous degradable polyester according to claim 1, wherein: the multifunctional tower type reactor pre-polycondensation chamber is sequentially provided with an overflow 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, and the overflow tray reaction zone (3-2) is communicated with the depressurization reaction zone (3-3) through an external flow regulating valve of the multifunctional tower type reactor; a polycondensation catalyst is arranged on a pipeline communicated with the overflow 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 connection port of the pre-condensation 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 double-polycondensation condenser (6) is communicated with a vacuum system through a double-polycondensation gas-phase pipeline (g 3), and a connecting port of the double-polycondensation condenser (6) and the multifunctional tower reactor is positioned between the prepolymer temperature-rising reaction zone (3-4) and the prepolymer baffling reaction zone (3-5).

6. 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 connected to a vacuum system via a final polycondensation vapor line (g 4).

7. The system for producing fully continuous degradable polyester according to claim 5, wherein: the overflow type tray reaction area (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 trays; a first overflow weir and a gas phase pipe are uniformly distributed on each reaction tower tray, the gas phase pipe is vertically arranged in the first overflow weir, the top of the gas phase pipe is lower than a connecting port of the multifunctional tower reactor and the pre-condensation condenser (5) and higher than a weir plate of the first overflow weir, and the bottom of the gas phase pipe keeps a distance with the bottom of the first overflow weir;

the pressure reduction 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 positioned on 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 third overflow weirs, annular guide plates are uniformly arranged between each layer of baffle plates, and a pre-condensation condenser (5) and a multifunctional tower reactor connecting port are arranged between the bottommost baffle plate and the annular guide plate below the baffle plate.

8. The system for producing fully continuous degradable polyester according to claim 1, wherein:

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 diol feeding pipeline (c);

the esterification catalyst and heat stabilizer adding ports are 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 communicating the overflow tray reaction zone (3-2) and the depressurization reaction zone (3-3).

Technical Field

The invention relates to a production system of full-continuous degradable polyester, belonging to the technical field of production of full-continuous degradable polyester.

Background

In recent years, with the increase of environmental awareness, relevant regulations are successively formulated and issued globally, the use of non-degradable plastics is limited by measures such as local disablement, limitation, forced collection and collection of pollution tax, and new degradable materials are vigorously developed to protect the environment. The traditional polyester can cause serious white pollution in the nature due to non-degradability, and the degradable polyester gradually becomes a hotspot in the chemical fiber industry. The degradable polyester not only has good thermal stability and mechanical property, but also has good extensibility and tensile property. The degradable polyester molecular chain has reduced or eliminated rigid benzene ring, increased fatty carbon chain and easy-to-hydrolyze ester bond, enhanced molecular chain flexibility, and capacity of degrading into carbon dioxide, water and small molecular compounds under 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 esterification reaction, pre-polycondensation reaction and final polycondensation reaction are all carried out in a single reactor, the retention time of materials 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 provide a production system of full-continuous degradable polyester.

The technical scheme of the invention is as follows: a production system of full-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 a left-right alignment way; the aliphatic dibasic acid metering device is arranged at an outlet of the aliphatic dibasic acid bin, and the aromatic dibasic acid metering device is arranged at an outlet of the aromatic dibasic acid bin; the top part of the pulping kettle 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, a process tower, a recycling aliphatic diol pump and a heat exchanger; the heat exchanger is positioned on the right side of the pulping kettle, and the pulping kettle is communicated with the left side of the heat exchanger through a pulp delivery 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 right below 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 multifunctional tower type reactor pre-polycondensation chamber, a flow regulating valve, a pre-polycondensation condenser and a secondary polycondensation condenser; the multifunctional tower reactor pre-polycondensation 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 ester flow regulating valve of the multifunctional tower reactor; the pre-condensation condenser and the secondary condensation condenser are arranged on the right side of the multifunctional tower reactor and are communicated with a pre-condensation 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 with the pelletizing system through a pipeline.

The esterification chamber of the multifunctional tower reactor and the pre-polycondensation chamber of the multifunctional tower reactor are arranged from bottom to top or from top to bottom;

when the esterification chamber and the pre-polycondensation chamber of the multifunctional tower reactor are arranged from top to bottom, the esterification chamber and the pre-polycondensation chamber are both arranged in the multifunctional tower reactor, the esterification chamber and the 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 in use, the aliphatic dibasic acid and the aromatic dibasic acid are respectively added into the pulping kettle together with the aliphatic dibasic alcohol according to the proportion required by setting after passing through the aliphatic dibasic acid metering device and the aromatic dibasic acid metering device, so as to realize batching and pulping.

The esterification chamber of the multifunctional tower reactor is not limited to one reaction chamber, and a plurality of esterification reaction chambers of the multifunctional tower reactor can be sequentially arranged from top to bottom; an esterification catalyst and a heat stabilizer adding port are arranged on a pipeline which is communicated with the lower part of the esterification chamber of the multifunctional tower reactor at the bottom of the heat exchanger, so that the catalyst is uniformly dispersed, and the hydrolysis failure of the esterification catalyst is avoided;

the process tower is communicated with a vacuum system through an esterification gas phase pipeline, the process tower is used for separating water vapor, small molecular esterification byproducts and aliphatic diol generated by esterification reaction, and the water vapor and the small molecular esterification byproducts are discharged from the top of the process tower and sent to a byproduct recovery system;

the heat exchanger is a tube type heat exchanger.

The multifunctional tower type reactor pre-polycondensation chamber is sequentially provided with an overflow tower 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 tower tray reaction zone is communicated with the depressurization reaction zone through an external flow regulating valve of the multifunctional tower type reactor; a polycondensation catalyst is arranged on a pipeline communicating the overflow tray reaction zone with the depressurization reaction zone; the pre-condensation condenser is communicated with a vacuum system through a pre-condensation vacuum pipeline; the connection port of the pre-condensation condenser and the multifunctional tower reactor is positioned between the overflow tray reaction zone and the prepolymer baffling reaction zone; the secondary polycondensation condenser is communicated with the vacuum system through a secondary polycondensation gas phase pipeline, and a connecting port of the secondary 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 condensation condenser is communicated with a vacuum system through a final condensation gas phase pipeline.

The overflow type tray reaction area 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 trays; a first overflow weir and a gas phase pipe are uniformly distributed on each reaction tower tray, the gas phase pipe is vertically arranged in the first overflow weir, the top of the gas phase pipe is lower than a connecting port of the multifunctional tower reactor and the pre-condensation condenser and higher than a weir plate of the first overflow weir, and the bottom of the gas phase pipe keeps a distance with the bottom of the first overflow weir;

the pressure reduction reaction area 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 positioned on 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, the top ends of the baffle plates are provided with third overflow weirs, annular guide plates are uniformly 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 guide plate below the baffle plate.

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 pulping kettle is also connected with an aliphatic diol feed pipeline;

the esterification catalyst and heat stabilizer adding ports are connected with an esterification catalyst adding pipeline and a heat stabilizer adding pipeline;

and a polycondensation catalyst adding pipeline is arranged on a pipeline communicating the overflow tray reaction zone with the depressurization reaction zone.

The pelletizing system comprises a reversing valve, a cutting chamber, a template, a pelletizer with a driving system, a cooling pipeline, a dryer and a vibrating screen.

The invention is reasonable in combination and convenient to use, and the fully-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 the 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 retention time is short, and the side reaction degree is small;

3. the method realizes the continuous production of the degradable polyester, and is simple, convenient, efficient, energy-saving and controllable.

In conclusion, the production system of the full-continuous degradable polyester provided by the invention comprises a batching and pulping kettle, a multifunctional tower reactor, a final polycondensation reactor and a pelletizing system. The batching and pulping kettle is connected with an aromatic dibasic acid and/or aliphatic dibasic acid bin, the bottom of the batching and pulping kettle is connected with the bottom of a heat exchanger through a slurry delivery 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 delivery pump, and the final polymer filter is connected with a pelletizing system. The invention is suitable for degradable aromatic-aliphatic polyester and degradable aliphatic polyester. 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 structural view of the present invention;

wherein, the device comprises a pulping kettle 1, a heat exchanger 2, a multifunctional tower reactor esterification chamber 3-1, a tray reaction zone 3-2 overflow type, a pressure reduction reaction zone 3-3, a prepolymer heating reaction zone 3-4, a prepolymer baffling reaction zone 3-5, a process tower 4, a prepolycondensation condenser 5, a polycondensation condenser 6, a polycondensation condenser 7, a polycondensation condenser 8, a melt delivery pump 9, a melt filter 10, a pelletizing system 11, an aromatic dibasic acid feed pipeline a, an aliphatic dibasic acid feed pipeline b, an aliphatic dihydric alcohol feed pipeline c, an esterification catalyst adding pipeline d, a heat stabilizer adding pipeline e, a polymerization catalyst adding pipeline f, an esterification gas phase pipeline g1, a polycondensation vacuum pipeline g2, a polycondensation gas phase pipeline g3 and a polycondensation gas phase pipeline g 4.

Detailed description of the invention

The invention is further described with reference to specific examples. The scope of the invention is not limited thereto:

a production system of full-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 a left-right alignment way; the aliphatic dibasic acid metering device is arranged at an outlet of the aliphatic dibasic acid bin, and the aromatic dibasic acid metering device is arranged at an outlet of the aromatic dibasic acid bin; the top of the pulping 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 pulping kettle 1, and the pulping kettle 1 is communicated with the left side of the heat exchanger 2 through a pulp delivery 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 at 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 right below 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 type reactor pre-polycondensation chamber, a flow regulating valve, a pre-polycondensation condenser 5 and a secondary polycondensation condenser 6; the multifunctional tower reactor pre-polycondensation chamber is positioned at the middle lower part of the multifunctional tower reactor and is communicated with the multifunctional tower reactor esterification chamber 3-1 at the upper part of the multifunctional tower reactor through an external ester flow regulating valve of the multifunctional tower reactor; the pre-condensation condenser 5 and the secondary condensation condenser 6 are arranged on the right side of the multifunctional tower reactor, and the pre-condensation condenser 5 and the secondary condensation condenser 6 are communicated with a pre-condensation 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 at 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; 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; melt filter 10 is piped to pelletizing system 11.

Further, the esterification chamber 3-1 of the multifunctional tower reactor and the pre-polycondensation 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 both 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 gradually rises from top to bottom, and the absolute pressure gradually decreases.

When in use, the aliphatic dibasic acid and the aromatic dibasic acid are respectively added into the pulping kettle 1 together with the aliphatic dibasic alcohol according to the proportion required by setting after passing through the aliphatic dibasic acid metering device and the aromatic dibasic acid metering device, so as to realize batching and pulping.

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; an esterification catalyst and a heat stabilizer adding port are arranged on a pipeline 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, micromolecule esterification byproducts and aliphatic diol generated by esterification reaction, and the water vapor and the micromolecule esterification byproducts are discharged from the top of the process tower and sent to a byproduct recovery system; the heat exchanger 2 is a shell and tube heat exchanger.

The multifunctional tower type reactor pre-polycondensation chamber is sequentially provided with an overflow 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, and the overflow tray reaction zone 3-2 is communicated with the depressurization reaction zone 3-3 through an external flow regulating valve of the multifunctional tower type reactor; a polycondensation catalyst is arranged on a pipeline communicated with the overflow 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; a connecting port of the pre-condensation 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 secondary polycondensation condenser 6 is communicated with a vacuum system through a secondary polycondensation gas phase pipeline g3, and a connecting port of the secondary polycondensation condenser 6 and the multifunctional tower reactor is positioned between the prepolymer temperature-rising 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 connected to a vacuum system via a final polycondensation vapor 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 vertical to the reaction trays; a first overflow weir and a gas phase pipe are uniformly distributed on each reaction tower tray, the gas phase pipe is vertically arranged in the first overflow weir, the top of the gas phase pipe is lower than a connecting port of the multifunctional tower reactor and the pre-condensation condenser 5 and higher than a weir plate of the first overflow weir, and the bottom of the gas phase pipe keeps a distance with 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 on 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 third overflow weirs, annular guide plates are uniformly 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 guide plate below the baffle plate.

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 diol feed pipeline c; the esterification catalyst and heat stabilizer adding ports are 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 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, technical personnel in the industry do not need creative labor to make changes and substitutions on the technical characteristics of the invention, and the changes and substitutions are included in the protection scope of the invention.