CN211546382U - Production equipment of full-continuous polylactic acid - Google Patents
Production equipment of full-continuous polylactic acid Download PDFInfo
- Publication number
- CN211546382U CN211546382U CN201922020569.5U CN201922020569U CN211546382U CN 211546382 U CN211546382 U CN 211546382U CN 201922020569 U CN201922020569 U CN 201922020569U CN 211546382 U CN211546382 U CN 211546382U
- Authority
- CN
- China
- Prior art keywords
- polymerization
- way valve
- kettle
- tower
- inlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Polyesters Or Polycarbonates (AREA)
Abstract
The utility model relates to a full continuous polylactic acid's production facility, include first polymeric kettle, condenser, second polymeric kettle, third polymeric tower, fourth polymeric tower, take off single cauldron, vacuum unit, underwater pelletizer, vacuum packaging machine. A reflux condenser is arranged at the top of the first polymerization kettle, and the first polymerization kettle is connected with an inlet of a first three-way valve through a melt gear pump; the outlet of the first three-way valve is respectively connected with the second polymerization kettle and the inlet of the first four-way valve; the second polymerization kettle adopts a special stirring heat tracing form and is connected with the inlet of the first four-way valve through a gear pump; the outlet of the first four-way valve is respectively connected with the third polymerization tower and the inlet of the second four-way valve; the third polymerization tower is connected with the inlet of the second four-way valve through a gear pump; and the outlet of the second four-way valve is respectively connected with the fourth polymerization tower and the second three-way valve. The utility model discloses degree of automation is high, but each cauldron reaction temperature independent operation, and technology control range is big.
Description
Technical Field
The utility model belongs to the full biodegradable materials field of polymer trade, especially relate to a production facility of full continuous polylactic acid.
Background
The synthesis of poly-L-lactic acid (PLLA) includes two processes of ring-opening polymerization (ROP) and direct polycondensation (DPc). The process for synthesizing polylactic acid by DPc method is relatively simplified, but DPc method hardly removes the generated moisture at the late stage of polymerization reaction, and thus ultra-high molecular weight PLLA cannot be synthesized. The ROP method process needs high-purity lactide monomer, the presence of trace impurities can affect the polymerization reaction repeatability, but the process can synthesize PLLA with low molecular weight to ultrahigh molecular weight, the yield is high, and if the controlled synthesis of PLLA with low molecular weight to high molecular weight can be realized, the product PLLA has wide application. The poor flowability and easy degradation of the polylactic acid melt with high molecular weight are also important reasons for limiting the synthesis of the polylactic acid with high molecular weight.
The utility model adopts the technique of synthesizing polylactic acid by ring-opening polymerization, and can realize the controlled synthesis of PLLA with different molecular weights through the combination of the melt reversing valve to obtain the whole-course and multipurpose PLLA with low molecular weight to high molecular weight (5.0 multiplied by 103-1.8 multiplied by 105); the heat transfer problem of high-viscosity materials is improved by a specially designed polymerization device.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the problem of the above-mentioned controlled synthesis from low molecular weight PLLA to high molecular weight PLLA, provide a production facility and process flow for full continuous polylactic acid of easy operation, degree of automation is high, operation safety and stability.
The purpose of the utility model is realized like this:
a production device of full-continuous polylactic acid comprises a first polymerization kettle, a condenser, a second polymerization kettle, a third polymerization tower, a fourth polymerization tower, a demonomerization kettle, a vacuum unit, an underwater pelletizer and a vacuum packaging machine, wherein a raw material melting configurator and a reflux condenser are arranged above the first polymerization kettle, the melting configurator and the reflux condenser are arranged in a left-right alignment manner, and the first polymerization kettle is provided with an independent heating medium heating system;
a first gear pump and a first three-way valve are arranged between the second polymerization kettle and the first polymerization kettle, the first gear pump is communicated with the inlet of the first three-way valve through a pipeline, one outlet of the first three-way valve is communicated with the inlet of the second polymerization kettle through a pipeline, the other outlet of the first three-way valve is communicated with one inlet of a first four-way valve through a pipeline, and polylactic acid produced by the first polymerization kettle can be sent to the second polymerization kettle or can be directly sent to a third polymerization tower or a fourth polymerization tower or a demonomerization kettle;
a second gear pump and a first four-way valve are arranged between the third polymerization tower and the second polymerization kettle, the second gear pump is communicated with the other inlet of the first four-way valve through a pipeline, the other outlet of the first four-way valve is communicated with the inlet of the second four-way valve through a pipeline, and polylactic acid produced by the second polymerization kettle can be sent to the third polymerization tower or directly sent to a fourth polymerization tower or a demonomerization kettle;
a third gear pump and a second four-way valve are arranged between the fourth polymerization tower and the third polymerization tower, the third gear pump is communicated with the other inlet of the second four-way valve through a pipeline, the other outlet of the second four-way valve is communicated with the inlet of the second three-way valve through a pipeline, and polylactic acid produced by the third polymerization tower can be sent into the fourth polymerization tower or directly sent into or removed from a single kettle;
a fourth gear pump and a second three-way valve are arranged between the demonomerization reactor and a fourth polymerization tower, the outlet of the fourth gear pump is communicated with the other inlet of the second three-way valve through a pipeline, and the outlet of the second three-way valve is communicated with the demonomerization reactor through a pipeline. And a monomer trapping system is arranged between the monomer removing kettle and the vacuum pump set. The bottom of the demould kettle is connected with an underwater pelletizer, and the melt in the demould kettle is pelletized by the underwater pelletizer and then sent to a vacuum packaging machine for packaging.
Furthermore, the second polymerization kettle adopts a stirring heat tracing mode combining a plurality of layers of heat exchange pipe coil pipes and a plurality of layers of paddle type stirring, so that the requirements of large heat exchange area and high-viscosity material stirring are met;
furthermore, the third polymerization tower (10) and the fourth polymerization tower (13) adopt reactors in the form of heat exchange mixing tubes in Chinese knot shapes, so that the high-efficiency heat transfer of the ultrahigh-viscosity polymer is realized;
furthermore, the demonomerization kettle (16) adopts a vertical rotary evaporator form, so that the demonomerization efficiency is improved.
Compared with the prior art, the beneficial effects of the utility model reside in that:
the utility model discloses degree of automation is high, but each cauldron reaction temperature independent operation, and technology control range is big, can realize that the controlled synthesis of different molecular weight PLLA obtains from low molecular weight to high molecular weight (5.0X 103-1.8X 105) whole journey, the PLLA of multipurpose.
Drawings
Fig. 1 is a schematic flow chart of the present invention.
Wherein, 1, a melting configuration device; 2. a first polymerizer; 3. a first gear pump; 4. a separate heating medium system; 5. a first three-way valve; 6. a second polymerization vessel; 7. a reflux condenser; 8. a second gear pump; 9. a first four-way valve; 10. a third polymerization column; 11. a third gear pump; 12. a second four-way valve; 13. a fourth polymerization tower; 14. a fourth gear pump; 15. a second three-way valve; 16. removing the single kettle; 17. an underwater pelletizer; 18. a vacuum packaging machine; 19. a monomer capture system; 20. and a vacuum pump set.
Detailed Description
As shown in figure 1, the full-continuous polylactic acid production equipment as shown in figure 1 mainly comprises a first polymerization kettle 2, a reflux condenser 7, a second polymerization kettle 6, a third polymerization tower 10, a fourth polymerization tower 13, a demonomerization kettle 16, an underwater pelletizer 18, a vacuum packaging machine 19 and a vacuum pump set 20.
As shown in fig. 1, a fully continuous polylactic acid production apparatus, slurry prepared from a melting configurator 1 enters a first polymerization kettle 2 for preliminary polymerization, the first polymerization kettle 2 is of a jacket structure and is connected with an independent heat medium system 4 for independent temperature adjustment, a first gear pump 3 is arranged at the bottom of the first polymerization kettle 2, and the first gear pump 3 is connected with a first three-way valve 5 for melt direction adjustment and adaptation to production of polylactic acid with different molecular weights; the first three-way valve 5 is connected with the second polymerizer 6 and the first four-way valve 9; the second polymerization kettle 6 adopts a mode of combining a multilayer heating medium coil pipe with a layered stirrer, so that the heat transfer performance of the high-viscosity polymer is improved; a second gear pump 8 is arranged at the bottom of the second polymerization kettle 6 and connected with a first four-way valve 9, the first four-way valve 9 is respectively connected with a third polymerization tower 10 and a second four-way valve 12, so that the connection among the reaction kettles is realized, and a third gear pump 11 is arranged at the bottom of the third polymerization tower 10 and connected with the second four-way valve 12; the second four-way valve 12 is connected with a fourth polymerization tower 13 and a second three-way valve 15; the combination of multiple reation kettle has been realized through four three-way valves and cross valves, for example: 2-6-10-13, 2-6-10, 2-10-13, 2-6, 2-10, 2-13, etc. the combined reaction system has different reaction times, and the polymerization products with different molecular weights are obtained due to different reaction times of materials.
The third polymerization tower 10 and the fourth polymerization tower 13 are a multi-section tubular reactor which adopts multiple heating medium coil pipes and comprises a heating medium jacket, the multi-section tubular reactor is of a vertical structure and is divided into one section with the length of 1.5 meters, the temperature of the independent secondary heating medium is controlled, materials pass through the heating medium coil pipes which are arranged according to the Chinese knot form under the pushing of the pressure of a melt pump, the flowing direction of the materials is continuously guided and changed by the coil pipes, the internal and external exchange of the melt in the pipeline is realized, and the flowing direction of the melt is continuously changed by rotating the heating medium coil pipe at the next section back by 90 degrees.
The utility model discloses degree of automation is high, but each cauldron reaction temperature independent operation, and technology control range is big, can realize that the controlled synthesis of different molecular weight PLLA obtains from low molecular weight to high molecular weight (5.0 × 10)3-1.8×105) The whole course and the multi-purpose PLLA.
The present invention is not limited to the above embodiments, and based on the technical solutions disclosed in the present invention, those skilled in the art can make some replacements and transformations for some technical features without creative labor according to the disclosed technical contents, and these replacements and transformations are all within the protection scope of the present invention.
Claims (4)
1. A production device of full-continuous polylactic acid comprises a first polymerization kettle (2), a second polymerization kettle (6), a third polymerization tower (10), a fourth polymerization tower (13), a demonomerization kettle (16), a vacuum pump set (20), an underwater pelletizer (17) and a vacuum packaging machine (18), and is characterized in that a raw material melting configurator (1) and a reflux condenser (7) are arranged above the first polymerization kettle (2), the melting configurator (1) and the reflux condenser (7) are arranged in a left-right alignment manner, and an independent heat medium heating system (4) is arranged on the first polymerization kettle (2);
a first gear pump (3) and a first three-way valve (5) are arranged between the second polymerization kettle (6) and the first polymerization kettle (2), the first gear pump (3) is communicated with a feed inlet of the first three-way valve (5) through a pipeline, one outlet of the first three-way valve (5) is communicated with an inlet of the second polymerization kettle (6) through a pipeline, the other outlet of the first three-way valve (5) is communicated with one inlet of the first four-way valve (9) through a pipeline, polylactic acid produced by the first polymerization kettle (2) can be sent to the second polymerization kettle (6) or directly sent to a third polymerization tower (10) or a fourth polymerization tower (13) or a demonomerization kettle (16);
a second gear pump (8) and a first four-way valve (9) are arranged between the third polymerization tower (10) and the second polymerization kettle (6), the second gear pump (8) is communicated with the other inlet of the first four-way valve (9) through a pipeline, the other outlet of the first four-way valve (9) is communicated with the inlet of the second four-way valve (12) through a pipeline, and polylactic acid produced by the second polymerization kettle (6) can be sent to the third polymerization tower (10) or directly sent to a fourth polymerization tower (13) or a demonomerization kettle (16);
a third gear pump (11) and a second four-way valve (12) are arranged between the fourth polymerization tower (13) and the third polymerization tower (10), the third gear pump (11) is communicated with the other inlet of the second four-way valve (12) through a pipeline, the other outlet of the second four-way valve (12) is communicated with the inlet of the second three-way valve (15) through a pipeline, and polylactic acid produced by the third polymerization tower (10) can be sent to the fourth polymerization tower (13) or directly sent to or removed from a single kettle (16);
a fourth gear pump (14) and a second three-way valve (15) are arranged between the demonomerization kettle (16) and a fourth polymerization tower, the outlet of the fourth gear pump (14) is communicated with the other inlet of the second three-way valve (15) through a pipeline, the outlet of the second three-way valve (15) is communicated with the demonomerization kettle (16) through a pipeline, a monomer trapping system (19) is arranged between the demonomerization kettle (16) and the vacuum pump set (20), the bottom of the demonomerization kettle (16) is connected with an underwater pelletizer (17), and the melt in the demonomerization kettle (16) is granulated through the underwater pelletizer (17) and then is sent into a vacuum packaging machine (18) for packaging.
2. The production equipment of the full continuous polylactic acid according to claim 1, wherein the second polymerization kettle (6) adopts a stirring heat tracing mode combining a plurality of layers of heat exchange pipe coils and a plurality of layers of paddle stirring, so that the requirements of heat exchange area and high-viscosity material stirring are met.
3. The production equipment of the full continuous polylactic acid according to claim 1, wherein the third polymerization tower (10) and the fourth polymerization tower (13) adopt reactors in the form of heat exchange mixing tubes in Chinese knot shapes, so that the efficient heat transfer of the ultra-high viscosity polymer is realized.
4. The fully continuous polylactic acid production equipment according to claim 1, wherein the demonomerization kettle (16) is in the form of a vertical rotary evaporator, so that the demonomerization efficiency is improved.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201922020569.5U CN211546382U (en) | 2019-11-21 | 2019-11-21 | Production equipment of full-continuous polylactic acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201922020569.5U CN211546382U (en) | 2019-11-21 | 2019-11-21 | Production equipment of full-continuous polylactic acid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211546382U true CN211546382U (en) | 2020-09-22 |
Family
ID=72501417
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201922020569.5U Active CN211546382U (en) | 2019-11-21 | 2019-11-21 | Production equipment of full-continuous polylactic acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211546382U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110698657A (en) * | 2019-11-21 | 2020-01-17 | 扬州普立特科技发展有限公司 | Production equipment and process flow of full-continuous polylactic acid |
-
2019
- 2019-11-21 CN CN201922020569.5U patent/CN211546382U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110698657A (en) * | 2019-11-21 | 2020-01-17 | 扬州普立特科技发展有限公司 | Production equipment and process flow of full-continuous polylactic acid |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN211546382U (en) | Production equipment of full-continuous polylactic acid | |
| CN113893573B (en) | Lactide continuous melting crystallization purification system and method | |
| CN101580974B (en) | Continuous cation modified polyester preparation method and system for continuously preparing modified polyester melt and directly spinning polyester fiber | |
| CN103304791A (en) | Preparation process of high-quality fusant | |
| CN102399332B (en) | Propylene polymerization production technology by loop reactor batch liquid bulk method | |
| CN104098762B (en) | Bottle grade PET device and production technique thereof | |
| CN110698657A (en) | Production equipment and process flow of full-continuous polylactic acid | |
| CN101735182A (en) | Process for continuously producing succinic anhydride through hydrogenation of maleic anhydride | |
| CN210855928U (en) | Differential flexible polyester device for membranes | |
| CN103835013B (en) | Method for producing elastic PBT (polybutylene terephthalate) filaments by melt direct spinning | |
| CN115819745B (en) | Continuous preparation method of polyglycolic acid | |
| CN218901857U (en) | Device for continuously producing high-solid-content polymer products | |
| CN103539875A (en) | Control method for temperature of cooling medium of reactant outer circulation heat exchanger | |
| CN212142558U (en) | Continuous production system | |
| CN201912933U (en) | Rotating thin film interesterification flow reactor | |
| CN112194782A (en) | Device and method for producing PBT synthetic resin | |
| CN114031761B (en) | PPC synthesis system and synthesis process thereof | |
| CN208406979U (en) | Novel whole polycondensation vessel | |
| CN202876777U (en) | Novel esterification pre-reactor | |
| CN112973612B (en) | System device and method for continuously synthesizing methyl tetrahydrophthalic anhydride | |
| CN220990756U (en) | Solid phase tackifying device | |
| CN106543297B (en) | A kind of polymerization of bimodal polyethylene | |
| CN105126726A (en) | Polymerization device in production process of polyethylene oxide products | |
| CN112694460B (en) | Method and device for continuously synthesizing tetrahydrophthalic anhydride | |
| CN203820962U (en) | Device for melt direct spinning production of PBT (polybutylece terephthalate) elastic filament |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CB03 | Change of inventor or designer information |
Inventor after: Wang Dubin Inventor after: Ji Xueguang Inventor after: Yan Hongwei Inventor after: Xia Xinrong Inventor after: Ji Feng Inventor after: Liu Lin Inventor after: Qian Xinghui Inventor before: Wang Dubin Inventor before: Ji Xueguang Inventor before: Yan Hongwei Inventor before: Xia Xinrong Inventor before: Ji Feng Inventor before: Liu Lin Inventor before: Qian Xinghui |
|
| CB03 | Change of inventor or designer information |