CN211199083U - Full-continuous PETG's production facility - Google Patents
Full-continuous PETG's production facility Download PDFInfo
- Publication number
- CN211199083U CN211199083U CN201921992713.5U CN201921992713U CN211199083U CN 211199083 U CN211199083 U CN 211199083U CN 201921992713 U CN201921992713 U CN 201921992713U CN 211199083 U CN211199083 U CN 211199083U
- Authority
- CN
- China
- Prior art keywords
- reaction kettle
- kettle
- polycondensation
- esterification
- polycondensation reaction
- 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 provides a full continuous PETG's production facility, dispose the cauldron including NPG, the batching making beating cauldron, a reation kettle esterifies, two reation kettle esterify, technology tower, first polycondensation reation kettle in advance, first prepolymerization spraying system, second polycondensation reation kettle in advance, second prepolymerization spraying system, final polycondensation reation kettle, final polycondensation spray system, prepolymerization and final polymerization vacuum system, cut grain system etc.. The slurry batching and pulping kettle is connected with the first esterification reaction kettle, the first esterification reaction kettle is connected with the second esterification reaction kettle, the gas phases of the first esterification reaction kettle and the second esterification reaction kettle are connected with the process tower, and the recovery liquid of the process tower forms reflux with the first esterification reaction kettle and the second esterification reaction kettle; the esterification reaction kettle is connected with the first pre-polycondensation reaction kettle, and the gas phase of the first pre-polycondensation reaction kettle enters the first pre-polymerization spraying system. The utility model discloses compact structure, reasonable in process, degree of automation is high, and production efficiency is high, product quality is stable, operation safety and stability.
Description
Technical Field
The utility model belongs to the high molecular material field especially relates to a full continuous PETG's production facility.
Background
PETG is a non-crystalline copolyester. Since a certain amount of ethylene glycol is substituted by neopentyl glycol (NPG) during the production thereof, crystallization can be prevented, thereby improving the manufacturing process and transparency. The product is highly transparent, has excellent shock resistance, is particularly suitable for forming thick-wall transparent products, has excellent processing and forming performance, can be designed into any shape according to the intention of a designer, can be widely applied to the markets of plates, sheets, high-performance shrink films, bottles, profiles and the like by adopting traditional forming methods such as extrusion, injection molding, blow molding, plastic suction and the like, has excellent secondary processing performance and can be subjected to conventional machining decoration. The polyethylene terephthalate glycol neopentyl glycol ester (PETG) has high transparency, excellent impact resistance and good thermoplastic property, is widely used for sheet materials, and is a high-performance shrink film, excellent in comprehensive performance, high in cost performance and good in market prospect.
SUMMERY OF THE UTILITY MODEL
The utility model aims at achieving the above purpose, and provides a production device and a process flow of full-continuous PETG with reasonable process, high automation degree, high production efficiency, stable product quality and safe and stable operation.
The purpose of the utility model is realized like this:
the production equipment of the full-continuous PETG comprises a pulping system for carrying NPG, EG and PTA materials for mixing and pulping, and further comprises an esterification reaction system for carrying out esterification reaction on the mixed pulp, a polycondensation reaction system for carrying out pre-polycondensation and final polycondensation reaction on the finished raw materials, and a grain cutting system for melting and cutting grains on the raw materials subjected to pre-polycondensation and final polycondensation, and is characterized in that the pulping system comprises a preliminary pulp preparation tank, a buffer tank, an NPG preparation kettle and a batching and pulping kettle, wherein the bottom of the preliminary pulp preparation tank is connected with the top of the buffer tank through a pipeline, the buffer tank is connected with the top of the NPG preparation kettle through a pipeline, and the bottom of the NPG preparation kettle is connected with the batching and pulping kettle through a pipeline;
the esterification reaction system comprises an esterification first reaction kettle, an esterification second reaction kettle and a process tower, the esterification reaction system is connected with the pulping system through a screw pump, the esterification first reaction kettle is connected with the esterification second reaction kettle through a pipeline, the esterification first reaction kettle and the esterification second reaction kettle are connected with the lower part of the process tower through pipeline gas phases, and process tower recycled liquid forms reflux with the esterification first reaction kettle and the esterification second reaction kettle;
the polycondensation reaction system comprises a first pre-polycondensation reaction kettle, a first pre-polymerization spraying system, a second pre-polycondensation reaction kettle, a second pre-polymerization spraying system, a final polycondensation reaction kettle, a final polycondensation spraying system, a pre-polymerization and final polycondensation vacuum system, the polycondensation reaction system is arranged in the esterification reaction system, the first pre-polycondensation reaction kettle is connected with the second esterification reaction kettle through a pipeline, gas generated by the first pre-polycondensation reaction kettle is conveyed into the first pre-polymerization spraying system through a pipeline gas phase, the bottom of the first pre-polycondensation reaction kettle is connected with the bottom of the second pre-polycondensation front end, gas generated by the second pre-polycondensation reaction kettle is conveyed into the second pre-polymerization spraying system through a pipeline gas phase, the bottom of the second pre-polycondensation reaction kettle is connected with the bottom of the final polycondensation reaction kettle through a pipeline gas phase, and the gas generated by the final polycondensation reaction kettle is conveyed into the final polycondensation spraying system through a pipeline gas phase, the gas phases of the first pre-polymerization spraying system, the second pre-polymerization spraying system and the final polymerization spraying system are all connected with a pre-polymerization and final polymerization vacuum system; the melt produced by the final polycondensation reaction kettle enters a granulating system for granulation through pressurization;
furthermore, according to the requirements of different manufacturers, the NPG preparation kettle adopts intermittent preparation, and the feeding amounts of Ethylene Glycol (EG) and neopentyl glycol (NPG) are controlled according to a certain proportion;
further, feeding a catalyst of an esterification reaction kettle into the reaction kettle in a manner of diluting a mixed solution of the top and a refluxing process tower recovery liquid;
furthermore, the final polycondensation reaction kettle is a single-end-shaft disk vacuum reactor, a plurality of film-forming disks are arranged on the stirring shaft to form a two-disk stirring system, and the viscosity of the PETG product can meet higher requirements.
Compared with the prior art, the beneficial effects of the utility model reside in that:
the utility model discloses compact structure, reasonable in process, degree of automation is high, and production efficiency is high, product quality is stable, operation safety and stability. Through the mixing of EG and NPG, the slurry preparation is better carried out; the second pre-shrinking kettle adopts higher vacuum reaction to ensure the overflow of more micromolecules, thereby ensuring that the viscosity of the PETG product can meet higher requirements; and the underwater bracing and granulating mode is adopted, so that the forming of the sliced particles is ensured.
Drawings
Fig. 1 is a schematic flow chart of the present invention.
1. A preliminary slurry preparation tank; 2. a buffer tank; 3. NPG preparation kettle; 4. a material blending and pulping kettle; 5, esterifying a reaction kettle; 6. esterification reaction kettle II; 7. a process tower; 8. a first pre-polycondensation reaction kettle; 9. a first pre-polymerization spray system; 10. a second pre-polycondensation reaction kettle; 11. a second pre-polymerization spraying system; 12. a final polycondensation reaction kettle; 13. a final focusing spray system; 14. a prepolymerization and final polymerization vacuum system; 15. and a pelletizing system.
Detailed Description
As shown in figure 1, the full-continuous PETG production equipment and the batching and pulping system in the process flow as shown in figure 1 comprise a primary slurry mixing tank 1, a buffer tank 2, an NPG preparation kettle 3 and a batching and pulping kettle 4, wherein PTA and EG are buffered in the buffer tank 2 after the primary slurry mixing tank 1 is configured and then are sent into the NPG preparation kettle 3 to be configured according to the proportion and then are sent into the batching and pulping kettle 4, and the pulp after pulping is sent into an esterification reaction system through a screw pump.
As shown in figure 1, the esterification reaction kettle system in the production equipment and the process flow of the fully continuous PTEG comprises an esterification first reaction kettle 5, an esterification second reaction kettle 6 and a process tower 7. And (2) feeding the slurry from the blending and pulping kettle 4 into an esterification reaction kettle 5 for esterification reaction, controlling the reaction temperature to be 190-250 ℃ and the reaction pressure to be 80KPa (A), mixing a catalyst agent with the recovery liquid, adding the mixture into the reaction kettle for reaction, feeding the mixture into an esterification reaction kettle 6 after the reaction is finished, controlling the reaction temperature to be 190-250 ℃ and the reaction pressure to be 5KPa (A), mixing an additive with the recovery liquid, adding the mixture into the reaction kettle for continuous reaction, and controlling and conveying the esterified product to a first pre-polycondensation reaction kettle 8 through an adjusting valve. The process gas generated by the esterification reaction and the like are separated and recovered from the process tower 7 through a gas phase pipeline;
as shown in figure 1, the polycondensation reaction kettle system and the pelletizing system in the production equipment and the process flow of the fully continuous PETG comprise a first pre-polycondensation reaction kettle 8, a first pre-polymerization spraying system 9, a second pre-polycondensation reaction kettle 10, a second pre-polymerization spraying system 11, a final polycondensation reaction kettle 12, a final polymerization spraying system 13, a pre-polymerization and final polymerization vacuum system 14 and a pelletizing system 15. After the esterified substance enters a first pre-polycondensation reaction kettle 8, a pre-polycondensation reaction is carried out, the reaction temperature of the first pre-polycondensation reaction kettle 8 is controlled to be 260-270 ℃, the reaction pressure is 2-5 KPa (A), then the esterified substance enters a second pre-polycondensation reaction kettle 10 through an adjusting valve under the potential difference and the pressure difference for reaction, the temperature is controlled to be 265-275 ℃, the reaction pressure is 0.8-1 KPa (A), and the reacted prepolymer enters a final polycondensation reaction kettle 12. And the generated gas phase component water, EG and the like enter a corresponding prepolymerization spraying system. And (3) after the prepolymer enters a final polycondensation reaction kettle 12, carrying out final polycondensation reaction, wherein the reaction temperature is controlled to be 270-275 ℃, and the reaction pressure is 90-110 Pa (A). The melt after reaction has high viscosity, and is conveyed to a melt filter through a melt pump, filtered and then conveyed to a granulator for granulation. Gas-phase components generated in the final polycondensation reaction are recovered through a final polycondensation spraying system 13, and the vacuum of the final polycondensation reaction kettle and the spraying system is provided by a prepolymerization and final polycondensation vacuum system 14.
The utility model discloses compact structure, reasonable in process, degree of automation is high, and production efficiency is high, product quality is stable, operation safety and stability. Through the mixing of EG and NPG, the slurry preparation is better carried out; the second pre-shrinking kettle adopts higher vacuum reaction to ensure the overflow of more micromolecules, thereby ensuring that the viscosity of the PETG product can meet higher requirements; and the underwater bracing and granulating mode is adopted, so that the forming of the sliced particles is ensured.
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. The production equipment of the full-continuous PETG comprises a pulping system for carrying NPG, EG and PTA materials for mixing and pulping, and also comprises an esterification reaction system for carrying out esterification reaction on the mixed pulp, a polycondensation reaction system for carrying out pre-polycondensation and final polycondensation reaction on the finished raw materials, and a grain cutting system for cutting the pre-polycondensation and final polycondensation finished raw materials into grains, and is characterized in that the pulping system comprises a preliminary pulp mixing tank (1), a buffer tank (2), an NPG configuration kettle (3) and a batching and pulping kettle (4), wherein the bottom of the preliminary pulp mixing tank (1) is connected with the top of the buffer tank (2) through a pipeline, the buffer tank (2) is connected with the top of the NPG configuration kettle (3) through a pipeline, the bottom of the NPG configuration kettle (3) is connected with the batching and pulping kettle (4) through a pipeline,
the esterification reaction system comprises an esterification first reaction kettle (5), an esterification second reaction kettle (6) and a process tower (7), the esterification reaction system is connected with a pulping system through a screw pump, the esterification first reaction kettle (5) is connected with the esterification second reaction kettle (6) through a pipeline, the esterification first reaction kettle (5) and the esterification second reaction kettle (6) are both connected with the lower part of the process tower (7) through a pipeline gas phase, and a recovery liquid of the process tower (7) forms reflux with the esterification first reaction kettle (5) and the esterification second reaction kettle (6);
the polycondensation reaction system comprises a first pre-polycondensation reaction kettle (8), a first pre-polymerization spraying system (9), a second pre-polycondensation reaction kettle (10), a second pre-polymerization spraying system (11), a final polycondensation reaction kettle (12), a final polymerization spraying system (13) and a pre-polymerization and final polymerization vacuum system (14), the polycondensation reaction system is arranged on the right side of the esterification reaction system, the first pre-polycondensation reaction kettle (8) is connected with the second esterification reaction kettle (6) through a pipeline, gas generated by the first pre-polycondensation reaction kettle (8) is conveyed into the first pre-polymerization spraying system (9) through a pipeline gas phase, the bottom of the first pre-polycondensation reaction kettle (8) is connected with the bottom of the front end of the second pre-polycondensation reaction kettle (10) through a pipeline, gas generated by the second pre-polycondensation reaction kettle (10) is conveyed into the second pre-polymerization spraying system (11) through a pipeline gas phase, the bottom of the second pre-polycondensation reaction kettle (10) is connected with the bottom of the front end of the final polycondensation reaction kettle (12) through a pipeline, gas generated by the final polycondensation reaction kettle (12) is conveyed into a final polycondensation spraying system (13) through a pipeline gas phase, and the first pre-polymerization spraying system (9), the second pre-polymerization spraying system (11) and the final polycondensation spraying system (13) are all connected with a pre-polymerization and final polycondensation vacuum system (14) through pipeline gas phases; and the melt produced by the final polycondensation reaction kettle (12) enters a granulating system for granulation through pressurization.
2. The production equipment of the full-continuous PETG as claimed in claim 1, wherein the NPG preparation kettle (3) adopts batch preparation, and the feeding amounts of Ethylene Glycol (EG) and neopentyl glycol (NPG) are controlled according to the requirements of different manufacturers and a certain proportion.
3. The apparatus for producing the fully continuous PETG as claimed in claim 1, wherein the catalyst feed of the esterification reaction kettle (5) is added into the reaction kettle by diluting the mixed solution of the top and the recovery liquid of the reflux process tower (7).
4. The production equipment of the full-continuous PETG as claimed in claim 1, wherein the final polycondensation reaction kettle (12) is a single-end-shaft disc vacuum reactor, a plurality of film-forming discs are arranged on a stirring shaft to form a two-disc stirring system, and the viscosity of the PETG product can meet higher requirements.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921992713.5U CN211199083U (en) | 2019-11-18 | 2019-11-18 | Full-continuous PETG's production facility |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921992713.5U CN211199083U (en) | 2019-11-18 | 2019-11-18 | Full-continuous PETG's production facility |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211199083U true CN211199083U (en) | 2020-08-07 |
Family
ID=71881677
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921992713.5U Active CN211199083U (en) | 2019-11-18 | 2019-11-18 | Full-continuous PETG's production facility |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211199083U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114984888A (en) * | 2022-04-28 | 2022-09-02 | 华东理工大学 | Continuous esterification circulating reactor system for producing plasticizer |
-
2019
- 2019-11-18 CN CN201921992713.5U patent/CN211199083U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114984888A (en) * | 2022-04-28 | 2022-09-02 | 华东理工大学 | Continuous esterification circulating reactor system for producing plasticizer |
| CN114984888B (en) * | 2022-04-28 | 2023-10-03 | 华东理工大学 | Circulation reactor system for continuous esterification for producing plasticizer |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107652423B (en) | A kind of method of Waste Polyester alcoholysis method preparation regeneration low-melting point polyester | |
| WO2021004068A1 (en) | Continuous alcoholysis recovery method for waste polyester | |
| CN110724253A (en) | Full-continuous PBAT production equipment and process flow | |
| CN111138641A (en) | Method for preparing bottle-grade slices by recycling waste polyester bottles | |
| CN107793560A (en) | A kind of method that Waste Polyester alcoholysis method prepares regeneration high-contraction polyester | |
| CN111849026A (en) | Method and system for producing rPET bottle grade polyester chip | |
| CN107880255B (en) | Manufacturing method of optical film grade polyester chip | |
| CN210945446U (en) | Full-continuous PBAT production equipment | |
| CN106832397B (en) | The method of online reuse PET Polymerization Waste | |
| CN107652422A (en) | A kind of method that Waste Polyester alcoholysis method prepares cation regenerant dyeable polyester | |
| CN113045740B (en) | Preparation method of cyclic regeneration type water-soluble polyester chip | |
| CN211199083U (en) | Full-continuous PETG's production facility | |
| CN104098762B (en) | Bottle grade PET device and production technique thereof | |
| CN107892744A (en) | A kind of preparation method of Heat Shrinkage Film Polyester section | |
| CN112759746B (en) | Preparation method of high-cleanness food grade recycled bottle flakes | |
| CN110818888A (en) | Production equipment and process flow of fully-continuous PBS (Poly Butylene succinate) | |
| CN110790907A (en) | Production equipment and process flow of full-continuous PETG | |
| CN212425924U (en) | System for producing rPET bottle grade polyester chip | |
| CN107722249A (en) | A kind of method that Waste Polyester alcoholysis method prepares regeneration disperse dyeable polyester | |
| CN211199085U (en) | Full-continuous PBS production equipment | |
| CN212894539U (en) | Reaction system for producing high molecular weight polyester by continuous melt polycondensation | |
| CN204079855U (en) | A kind of bottle grade PET device | |
| CN114044892A (en) | Process for producing film-grade copolyester chips by chemical cyclic regeneration method | |
| CN113307954A (en) | Low-energy-consumption and high-benefit chemical recycling method for waste polyester | |
| CN114011357B (en) | High-viscosity copolyester production system and method with mixed alcohol separation and recovery functions |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CB03 | Change of inventor or designer information |
Inventor after: Yu Guoqing Inventor after: Hao Ruiqiang Inventor after: Liu Yong Inventor after: Yan Yu Inventor after: Yin Jie Inventor after: Liu Lin Inventor after: Li Guangzhi Inventor before: Yu Guoqing Inventor before: Hao Ruiqiang Inventor before: Liu Yong Inventor before: Yan Yu Inventor before: Yin Jie Inventor before: Liu Lin Inventor before: Li Guangzhi |
|
| CB03 | Change of inventor or designer information |