Compatible high-viscosity semi-continuous polyester production equipment

Abstract

The utility model discloses compatible high-viscosity semi-continuous polyester production equipment which is characterized in that a titanium and antimony catalyst, CHDM / NPG, EG and BDO injection port is formed in the top of a slurry preparation tank, an outlet of the slurry preparation tank is connected with an inlet of a first esterification kettle through a slurry pump or directly connected with the inlet of the first esterification kettle, and an ester and titanium catalyst injection port is further formed in the top of the first esterification kettle; one path of a material outlet of the first esterification kettle extends to the bottom of the kettle and is provided with a first electric valve, the other path of the material outlet of the first esterification kettle extends to the middle of the kettle and is provided with a second electric valve, and outlets of the two electric valves are connected in parallel and then are connected with a feeding hole of a second esterification pre-polycondensation kettle through a filter; the top of the second esterification pre-polycondensation kettle is also provided with a stabilizer, a polycondensation catalyst and a nitrogen injection port; a material outlet of the second esterification pre-polycondensation kettle is connected with an inlet of the polycondensation kettle through a pre-polycondensation gear pump and a filter; and a material outlet of the polycondensation kettle is connected with granulator granulation equipment through a polycondensation gear pump. The equipment can realize product diversification and differentiation, and is high in compatibility, high in productivity and high in viscosity.

Description

Technical Field

[0001] The utility model relates to a polymer material production device, in particular to a compatible high-viscosity semi-continuous polyester production device, belonging to the technical field of polyester production equipment. Background Art

[0002] There are three main process routes for traditional semi-continuous polyester equipment: The first route is: slurry preparation tank + first esterification kettle + polycondensation kettle, which is characterized by only being able to produce conventional polyethylene terephthalate (PET), with a single product, weak competitiveness, and low production capacity, with only about 5 to 6 kettles of products produced per day.

[0003] The second route: slurry mixing tank + first esterification kettle + second esterification kettle + polycondensation kettle, which is suitable for making differentiated PET products. The utilization rate of the second esterification kettle is not high. It is mainly used to add additives, mix and disperse materials, and most of the time it is an empty kettle waiting; the production capacity is low, and about 5 to 6 kettles of products are produced every day.

[0004] The third route: slurry preparation tank + first esterification kettle + pre-condensation kettle + polycondensation kettle, which is suitable for conventional PET products, because only the first esterification kettle cannot meet the production of some differentiated products; because it has two-stage polycondensation kettle function, the production capacity is greatly improved, and the production of conventional PET products can produce about 9 to 10 kettles per day.

[0005] In addition, the frame-type agitator structure used in traditional polycondensation kettles cannot meet the needs of high-viscosity products. The polycondensation reaction is an exothermic reaction. Especially in the later stage of the polycondensation reaction for producing high-viscosity products, the material temperature rise caused by the stirring operation is very obvious. The high temperature can easily cause the side reaction rate to accelerate, which will cause the viscosity of the material to no longer increase, but instead decrease, seriously affecting the quality of the product. If the stirring speed is reduced too low to avoid the material temperature rise caused by the stirring operation, the liquid level of the material in the kettle will not be updated in time, and the small molecules generated by the polycondensation reaction cannot be volatilized and separated in time, affecting the devolatilization effect, and will also cause the side reaction rate to increase, and the material viscosity will no longer increase, affecting the quality of the product.

[0006] The existing polycondensation reactor agitator is suitable for producing PET with an intrinsic viscosity below 0.700 dl / g (using analytical reagents, phenol and tetrachloroethane in a ratio of 3:2) and PBT with an intrinsic viscosity below 1.100 dl / g. It cannot meet the requirements for producing PETG products with an intrinsic viscosity of 0.730~0.830 dl / g, and cannot meet the demand for higher product viscosities.

[0007] In short, the existing semi-continuous device products have poor compatibility, low production capacity, and a bottleneck in the viscosity of some products. Utility Model Content

[0008] The purpose of this section is to summarize some aspects of the embodiments of the present invention and briefly introduce some preferred embodiments. Some simplifications or omissions may be made in this section and the abstract and utility model title of this application, and such simplifications or omissions shall not be used to limit the scope of the present invention.

[0009] In view of the above problems and / or the problems existing in the prior art, the present utility model is proposed.

[0010] The purpose of the utility model is to overcome the problems existing in the prior art and provide a compatible high-viscosity semi-continuous polyester production equipment, which can achieve product diversification and differentiation, strong compatibility, high production capacity and high viscosity.

[0011] In order to solve the above technical problems, the utility model provides a compatible high-viscosity semi-continuous polyester production equipment, including a slurry mixing tank, a titanium catalyst, CHDM / NPG, an antimony catalyst, EG and BDO injection ports are provided on the top of the slurry mixing tank, a slurry outlet of the slurry mixing tank is connected to the inlet of the first esterification kettle through a slurry pump, and a slurry outlet of the slurry mixing tank is directly connected to the inlet of the first esterification kettle. The top of the first esterification kettle is also provided with an esterification catalyst and a titanium catalyst injection port. The material outlet of the first esterification kettle has two routes, one of which extends to the bottom of the kettle and is provided with a No. 1 electric valve, and the other extends in the middle of the kettle and is provided with a No. 2 electric valve at the outlet. The outlets of the No. 1 electric valve and the No. 2 electric valve are connected in parallel and connected to the feed port of the second esterification pre-polycondensation kettle through the first esterification filter. The top of the second esterification pre-polycondensation kettle is also provided with a stabilizer, a polycondensation catalyst and a nitrogen injection port; the material outlet of the second esterification pre-polycondensation kettle is connected to the material inlet of the polycondensation kettle through the pre-polycondensation gear pump and the second esterification polycondensation filter; the material outlet of the polycondensation kettle is connected to the inlet of the polycondensation gear pump, and the outlet of the polycondensation gear pump is connected to the pelletizer granulation equipment.

[0012] As an improvement of the present invention, the outlet of the polycondensation gear pump is connected to the inlet of the electric three-way valve and a viscometer is provided on the connecting pipe. The first outlet of the electric three-way valve is connected to the film spraying component on the upper part of the inner cavity of the polycondensation kettle through a connecting pipe. The film spraying component extends in the horizontal direction and has a slit-shaped outlet at the bottom; the second outlet of the electric three-way valve is connected to the pelletizer granulation equipment.

[0013] As a further improvement of the present invention, the film spraying component is a conical box extending in the horizontal direction, the upper part is a square cross-section, and the lower part is an isosceles triangle cross-section with a narrowed bottom.

[0014] As a further improvement of the present invention, the tops of the first esterification kettle and the second esterification pre-polycondensation kettle are respectively connected to other auxiliary agent pipes.

[0015] As a further improvement of the present invention, the inner cavities of the slurry preparation tank, the first esterification kettle, the second esterification pre-condensation kettle, and the polycondensation kettle are respectively provided with heating coils and agitators, and the outer walls of the slurry preparation tank, the first esterification kettle, the second esterification pre-condensation kettle, and the polycondensation kettle are respectively provided with heating jackets, and the heat medium circulation pipes of each heating jacket are respectively connected to the primary heat medium supply pipe through a temperature control regulating valve group.

[0016] As a further improvement of the present invention, the agitator in the inner cavity of the polycondensation reactor is a frame-type agitator, and a downward-directed spiral agitating blade is wound around the central axis of the frame-type agitator.

[0017] As a further improvement of the present utility model, the gas phase outlet of the first esterification kettle is connected to the inlet of the No. 1 process tower, the gas phase outlet of the No. 1 process tower is connected to the inlet of the first esterification cooler No. 1, the liquid phase outlet of the first esterification cooler No. 1 is connected to the inlet of the first esterification buffer tank, the first esterification buffer tank has two outlets, one outlet is connected to the liquid phase reflux port of the No. 1 process tower, and the other outlet is connected to the first esterification receiving tank; the gas phase outlet of the first esterification cooler No. 1 is connected to the inlet of the first esterification cooler No. 2, the liquid phase outlet of the first esterification cooler No. 2 is connected to the inlet liquid seal pipe of the liquid seal tank, and the gas phase outlet of the first esterification cooler No. 2 is connected to the inlet of the esterification vacuum pump.

[0018] As a further improvement of the present invention, one gas phase port of the second esterification pre-condensation kettle is connected to the inlet of the No. 2 process tower through a shut-off valve, the gas phase outlet of the No. 2 process tower is connected to the inlet of the second esterification cooler, the outlet of the second esterification cooler is connected to the inlet of the second esterification buffer tank, and the outlet of the second esterification buffer tank is divided into two routes, one route is connected to the top liquid phase reflux port of the No. 2 process tower, and the other route is connected to the second esterification receiving tank.

[0019] As a further improvement of the present invention, the other gas phase outlet of the second esterification pre-condensation kettle is connected to the inlet of the No. 1 cooler through the No. 3 electric valve, the top gas phase outlet of the No. 1 cooler is connected to the inlet of the No. 1 cyclone separator, the bottom liquid phase outlet of the No. 1 cooler and the No. 1 cyclone separator is connected to the No. 1 condensation receiving tank, the top balance outlet of the No. 1 cyclone separator is connected to the top balance inlet of the No. 1 condensation receiving tank, the top gas phase outlet of the No. 1 cyclone separator is connected to the No. 1 buffer tank, and the top outlet of the No. 1 buffer tank is connected to the pre-condensation vacuum pump group.

[0020] As a further improvement of the present invention, the gas phase outlet of the condensation kettle is connected to the inlet of the No. 2 cooler, the top gas phase outlet of the No. 2 cooler is connected to the inlet of the No. 2 cyclone separator, and the bottom liquid phase outlet of the No. 2 cooler and the No. 2 cyclone separator is connected to the No. 2 condensation receiving tank; the top balance outlet of the No. 2 cyclone separator is connected to the top balance inlet of the No. 2 condensation receiving tank, and the top gas phase outlet of the No. 2 cyclone separator is connected to the No. 2 buffer tank; the top outlet of the No. 2 buffer tank is connected to the condensation vacuum pump group.

[0021] Compared with the existing technology, the utility model has achieved the following beneficial effects: 1. Strong compatibility, diversified high-viscosity semi-continuous polyester production equipment, meeting the production process requirements of most PET / PBT / PETG and other related differentiated products.

[0022] 2. In order to diversify the raw material routes of the products, a secondary heat medium heating system is specially designed for the slurry mixing tank to provide suitable process temperature for slurry mixing with different raw materials, expand the use routes of product raw materials, and improve the market competitiveness of products.

[0023] 3. The first esterification kettle system is equipped with an esterification vacuum pump to meet the requirements of normal pressure and negative pressure reaction conditions; at the same time, the first esterification No. 2 cooler is added, which is more conducive to the condensation and collection of methanol (normal pressure boiling point 64.7℃) and tetrahydrofuran (normal pressure boiling point 66℃) under negative pressure of 60KPa(A).

[0024] 4. The second esterification pre-polycondensation kettle is equipped with two separation systems for two working conditions. One is the esterification stage reaction separation and cooling system headed by the No. 2 process tower, and the other is the polycondensation reaction stage separation cooling vacuum system headed by the No. 1 cooler. The two systems are switched between the esterification stage and the polycondensation stage, which not only meets the working condition requirements of differentiated products, but also has the working condition requirements of the polycondensation reaction. There will be no situation where the second esterification pre-polycondensation kettle is waiting empty, the equipment utilization rate is maximized, and the production capacity of the equipment is improved.

[0025] 5. The polycondensation frame agitator structure has been optimized. The agitator ribs on the periphery of the frame agitator are retained to scrape the inner wall of the kettle to refresh the material, preventing prolonged retention of material on the kettle wall and affecting quality. A spiral agitator blade has been designed in the center of the frame agitator, rotating to push the material downward. At the same speed, the new agitator structure achieves a far superior liquid level refreshment effect than traditional frame agitators.

[0026] 6. During the material reaction stage of the polycondensation kettle, the material passes through the polycondensation gear pump and the electric three-way valve, and then the film spraying component for self-circulation. The material coming out of the film spraying component is in a thin film state. The enlarged material evaporation surface is beneficial to the volatilization and separation of small molecules in the material, which accelerates the polycondensation reaction speed and plays a partial role of the agitator.

[0027] 7. The secondary heat medium system of the polycondensation kettle system is designed with a heat medium radiator, which can reduce the temperature of the secondary heat medium and is used to remove the excess heat energy generated by the exothermic reaction of the polycondensation kettle, so as to prevent the material from overheating and getting out of control in a high-viscosity state and reduce the impact of side reactions.

[0028] 8. The second esterification pre-condensation kettle system and the polycondensation kettle system respectively use mechanical vacuum pumps, including dry screw pumps and three-stage Roots pumps. Considering the diversity of products and raw materials, the use of vacuum jet pumps has limitations. One type of injection medium cannot meet diverse needs. Compared with the operating energy consumption, the energy consumption of mechanical vacuum pumps is lower than that of jet vacuum pumps. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the following briefly introduces the drawings required for describing the embodiments. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative work. The drawings are only provided for reference and explanation, and are not intended to limit the present invention. Among them:

[0030] Figure 1 This is a flow chart of the utility model's compatible high-viscosity semi-continuous polyester production equipment;

[0031] Figure 2 This is an enlarged view of the frame agitator in the polycondensation kettle;

[0032] Figure 3 This is the main view of the film spraying parts in the polycondensation kettle;

[0033] Figure 4 It is a cross-sectional view of the film spraying parts in the polycondensation reactor;

[0034] In the figure: 1. Slurry mixing tank; 1a. Slurry heat medium pump; 1b. Temperature control valve group; 1c. Slurry pump; 1d. Feed hopper;

[0035] 2. First esterification kettle; 2a. First esterification heat medium pump; 2b. Temperature control valve group; 2c. First esterification product filter;

[0036] 3. Process tower No. 1; 3a. First esterification cooler No. 1; 3b. First esterification cooler No. 2; 3c. First esterification buffer tank; 3d. First esterification receiving tank; 3e. Liquid seal tank;

[0037] 4. Esterification vacuum pump; 5. Second esterification pre-condensation kettle; 5a. Second esterification pre-condensation heat medium pump; 5b. Temperature control valve group; 5c. Second esterification pre-condensation filter; 5d. Cooler No. 1; 5e. Cyclone separator No. 1; 5f. Condensation receiving tank No. 1; 5g. Buffer tank No. 1; 5h. Pre-condensation gear pump;

[0038] 6. Process tower No. 2; 6a. Second esterification cooler; 6b. Second esterification buffer tank; 6c. Second esterification receiving tank;

[0039] 7. Pre-condensation vacuum pump assembly; 8. Condensation reactor; 8a. Condensation heat medium pump; 8b. Temperature control valve assembly; 8c. Condensation gear pump; 8d. Cooler No. 2; 8e. Cyclone separator No. 2; 8f. Condensation receiving tank No. 2; 8g. Buffer tank No. 2; 8h. Film spraying components; 8j. Frame agitator; 8k. Spiral agitator;

[0040] 9. Polycondensation vacuum pump unit; 10. Heat medium radiator; 11. Jacketed tube heat medium pump; 11a. Temperature control valve unit; 12. Viscometer; 13. Pelletizer and pelletizing equipment;

[0041] G1. Titanium catalyst tube; G2. CHDM / NPG tube; G3. Antimony catalyst tube; G4. EG tube; G5. BDO tube; G6. Other additive tube; G7. Transesterification catalyst tube; G8. Titanium catalyst tube; G9. Nitrogen tube; G10. Other additive tube; G11. Stabilizer tube; G12. Polycondensation catalyst tube; G13. Slurry tube; G14. Primary heat medium supply tube; G15. Primary heat medium return tube;

[0042] S1. Electric valve No. 1; S2. Electric valve No. 2; S3. Electric valve No. 3; S4. Shut-off valve; S5. Electric three-way valve. DETAILED DESCRIPTION

[0043] In the following description of the present invention, the terms "upper", "lower", "front", "back", "left", "right", "inside", "outside", etc. indicate directions or positional relationships based on the directions or positional relationships shown in the accompanying drawings. They are only for the convenience of describing the present invention and simplifying the description, and do not mean that the device must have a specific direction.

[0044] In order to make the technical means, creative features, objectives and effects of the present invention easier to understand, the present invention is further described below with reference to specific figures. Obviously, the embodiments described are only a part of the present invention, not all of the embodiments.

[0045] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as those commonly understood by those skilled in the art in the art of the present invention. The terms used herein in the specification of the present invention are only for the purpose of describing specific embodiments and are not intended to limit the present invention.

[0046] like Figure 1As shown, the compatible high-viscosity semi-continuous polyester production equipment of the present invention includes a slurry mixing tank system, a first esterification kettle system, a second esterification pre-condensation kettle system, a condensation kettle system, a jacketed pipe heat medium system and a pelletizer granulation equipment 13.

[0047] The main functions of the slurry mixing tank system are to mix the main and auxiliary raw materials according to the controlled ratio, control the temperature according to the process requirements, and control the slurry delivery speed according to the esterification reaction feed requirements.

[0048] The slurry preparation tank 1 is designed with an agitator, a jacket, an internal coil, and a feeding hopper 1d. It is also equipped with a slurry heat medium pump 1a. The primary heat medium supply pipe G14 is connected to the inlet of the slurry heat medium pump 1a through a temperature control valve group 1b. The inlet pipe of the slurry heat medium pump 1a is also connected to the primary heat medium return pipe G15. The slurry preparation tank 1 has two slurry outlets. One outlet is connected to the inlet of the slurry pump 1c, which is connected to the inlet of the first esterification kettle 2. The other outlet of the slurry preparation tank 1 is directly connected to the feed port of the first esterification kettle 2 via a slurry pipeline G13. The top inlet of the slurry preparation tank 1 is connected to the titanium catalyst G1, the CHDM / NPG tube G2, the antimony catalyst tube G3, the EG tube G4, and the BDO tube G5.

[0049] The normal operating process is to first add alcohol, such as ethylene glycol or 1,4-butanediol or 1,4-cyclohexanedimethanol or neopentyl glycol, into the slurry preparation tank 1, control the temperature according to the process requirements, start the agitator, and then add dimethyl terephthalate or terephthalic acid into the slurry preparation tank 1 in a quantitative manner through the feeding hopper 1d, and then add a suitable catalyst to complete the entire slurry preparation process.

[0050] The first esterification kettle system mainly provides conditions for the esterification or transesterification reaction of materials. It is temperature-controlled and can be controlled at normal pressure or negative pressure. It provides a larger space for the production of diversified products. The inconsistency between products and raw materials will result in different corresponding reaction conditions.

[0051] like Figure 1 As shown, the first esterification kettle 2 is provided with an agitator, an inner coil, a jacket, and is also equipped with a secondary heat medium, a first esterification heat medium pump 2a and a temperature control regulating valve group 2b. The first esterification kettle 2 has two slurry inlets, one inlet is connected to the outlet of the slurry pump 1c, and the other inlet is connected to the slurry pipe G13.

[0052] The gas phase outlet of the first esterification kettle 2 is connected to the inlet of the first process tower 3, which is in turn connected to the inlet of the first esterification cooler 3a. The liquid phase outlet of the first esterification cooler 3a is connected to the inlet of the first esterification buffer tank 3c. The first esterification buffer tank 3c has two outlets: one outlet is connected to the liquid phase reflux port of the first process tower 3, and the other outlet is connected to the inlet of the first esterification receiving tank 3d. The effluent from the first esterification receiving tank 3d is recycled or dehydrated. The gas phase outlet of the first esterification cooler 3a is connected to the inlet of the first esterification cooler 3b. The liquid phase outlet of the first esterification cooler 3b is connected to the inlet liquid seal pipe of the liquid seal tank 3e. The gas phase outlet of the first esterification cooler 3b is connected to the inlet of the esterification vacuum pump 4. The first esterification reactor 2 has two material outlets, located at different heights within the reactor. One outlet, controlled by electric valve S1, extends to the bottom of the reactor, while the other, controlled by electric valve S2, extends to the middle of the reactor. These two outlets are connected in parallel to the inlet of the first esterification filter 2c. The outlet of the first esterification filter 2c is connected to the feed port of the second esterification pre-polycondensation reactor 5.

[0053] Depending on the differences in raw materials and production processes, the material liquid level in the first esterification kettle 2 has two operating conditions. If the main raw materials are PTA and EG or PTA and BDO for esterification reaction, each kettle of the first esterification kettle 2 transfers the material to the second esterification pre-condensation kettle 5 through the pipeline of the second electric valve S2. After the material transfer, half of the esterified product (referred to as mother liquor) will remain in the first esterification kettle 2, which helps to speed up the esterification reaction speed of the next batch of materials.

[0054] When the main raw materials are DMT and EG, or DMT and BDO for ester exchange reaction, each kettle of the first esterification kettle 2 transfers the material to the second esterification pre-condensation kettle 5 through the pipeline of the first electric valve S1. After the material transfer, there is no need to leave the mother liquor in the first esterification kettle 2.

[0055] Byproducts of the esterification or transesterification reaction in the first esterification reactor 2 are separated through process tower 1 3, first esterification cooler 1 3a, and first esterification cooler 2 3b. The separated byproducts are cooled to a liquid phase and transferred to the first esterification receiving tank 3d and liquid seal tank 3e. The completion of the esterification or transesterification reaction is determined by the liquid level in the first esterification receiving tank 3d.

[0056] The top of the first esterification reactor 2 is connected to the transesterification catalyst tube G7, the titanium catalyst tube G8, and other auxiliary agent tubes G6. These are added based on product needs and production process requirements. When producing PBT products, the optimal esterification pressure is around 60 kPa (A). Other PET products are esterified at normal pressure.

[0057] The first esterification kettle 2 is equipped with an esterification vacuum pump 4. The first esterification kettle system can meet the requirements of normal pressure and negative pressure reaction conditions. At the same time, the first esterification No. 2 cooler 3b is added, which is conducive to the condensation and collection of methanol (normal pressure boiling point 64.7°C) and tetrahydrofuran (normal pressure boiling point 66°C) under negative pressure of 60 kPa (A).

[0058] To address the issues with the first existing route, this second esterification and pre-polycondensation reactor system is designed specifically for the production of differentiated PET / PETG / PBT products. Various required additives are added to the second esterification and pre-polycondensation reactor, and through temperature control and stirring, uniform mixing is achieved to meet the needs of various differentiated products. However, in actual production, the second esterification reactor is only used for approximately 40 minutes per batch, leaving the remaining approximately 3 hours empty, resulting in extremely low utilization. Without a second esterification and pre-polycondensation reactor, the production of differentiated products would be insufficient. Furthermore, without a pre-polycondensation reactor, there would only be one polycondensation reactor, resulting in low production capacity. To address this issue, the second esterification and pre-polycondensation reactor system was introduced.

[0059] like Figure 1 As shown, the material inlet of the second esterification and pre-polycondensation kettle 5 is connected to the outlet of the first esterification filter 2c, the second esterification and pre-polycondensation kettle 5 is equipped with a stirrer, an inner coil, and a jacket, the material outlet of the second esterification and pre-polycondensation kettle 5 is connected to the inlet of the pre-polycondensation gear pump 5h, the outlet of the pre-polycondensation gear pump 5h is connected to the inlet of the second esterification and polycondensation filter 5c, and the outlet of the second esterification and polycondensation filter 5c is connected to the material inlet of the polycondensation kettle 8.

[0060] The second esterification pre-condensation kettle 5 is equipped with a second esterification pre-condensation heat medium pump 5a and a temperature control regulating valve group 5b. The second esterification pre-condensation kettle 5 is provided with two gas phase outlets, one gas phase outlet is connected to the inlet of the No. 2 process tower 6, and there is a shut-off valve S4 in the connecting pipeline. The gas phase outlet of the No. 2 process tower 6 is connected to the inlet of the second esterification cooler 6a, and the outlet of the second esterification cooler 6a is connected to the inlet of the second esterification buffer tank 6b. The outlet of the second esterification buffer tank 6b is divided into two routes, one route is connected to the top liquid phase reflux port of the No. 2 process tower 6, and the other route is connected to the inlet of the second esterification receiving tank 6c. The discharge of the second esterification receiving tank 6c is recycled or dehydrated.

[0061] Another gas phase outlet of the second esterification pre-condensation kettle 5 is connected to the inlet of cooler No. 1 5d. There is a No. 3 electric valve S3 in the middle of the connecting pipeline. The top gas phase outlet of cooler No. 1 5d is connected to the inlet of cyclone separator No. 1 5e. The bottom liquid phase outlet of cooler No. 1 5d is connected to the inlet of polycondensation receiving tank No. 1 5f. The drainage of polycondensation receiving tank No. 1 5f is recycled. The bottom liquid phase outlet of cyclone separator No. 1 5e is also connected to the top inlet of polycondensation receiving tank No. 1 5f. The top balance outlet of cyclone separator No. 1 5e is connected to the top balance inlet of polycondensation receiving tank No. 1 5f. The top gas phase outlet of cyclone separator No. 1 5e is connected to the inlet of buffer tank No. 1 5g. The drainage of buffer tank No. 1 5g is recycled. The top outlet of buffer tank No. 5g is connected to the inlet of pre-condensation vacuum pump group 7. In addition, the top of the second esterification pre-polycondensation reactor 5 is connected to other auxiliary agent pipes G10, a stabilizer pipe G11, a polycondensation catalyst pipe G12 and a nitrogen pipe G9.

[0062] When the reaction in the first esterification reactor 2 is complete, electric valve No. 3 S3 is closed, shut-off valve S4 is opened, and nitrogen is introduced into the first esterification reactor 2 at 250 kPa (G) through nitrogen pipe G9. Depending on the product's process requirements, either electric valve No. 2 S2 or electric valve No. 1 S1 is opened, and the pressure differential is used to transfer the material from the first esterification reactor 2 to the second esterification pre-polycondensation reactor 5. The agitator in the second esterification pre-polycondensation reactor 5 is then started, and the required additives are added according to product requirements. The mixture is stirred and mixed for 10 to 40 minutes; the mixing time varies depending on the additives added. Excess alcohol vapor is separated from the second esterification cooler 6a by the second process tower 6 and then cooled to the second esterification receiving tank 6c. Close the shut-off valve S4, open the No. 3 electric valve S3, start the pre-condensation vacuum pump group 7, control the pumping rate and vacuum degree according to the process requirements, so that the second esterification pre-condensation kettle 5 can play the role of a condensation kettle, improve the polymerization degree and viscosity of the material in the second esterification pre-condensation kettle 5, and the characteristic viscosity of the product coming out of the second esterification pre-condensation kettle 5 can reach 0.330~0.400dl / g, thereby shortening the reaction time of the material in the condensation kettle 8, greatly improving the production capacity of the device, and can produce 9~10 kettles of differentiated products every day.

[0063] In view of the problem that the polycondensation kettle of the second route in the prior art cannot meet the demand for high-viscosity products, the polycondensation kettle has optimized the structure of the frame agitator, retaining the stirring ribs on the periphery of the frame agitator 8j for scraping and updating the inner wall of the kettle to prevent the material from staying on the kettle wall for a long time and affecting the quality; and a spiral stirring blade 8k centered on the axis is designed in the middle of the frame agitator 8j, and the stirring rotates in the form of spiral downward pressing of the material, such as Figure 2 At the same speed, the new structure agitator has a much better effect on material level renewal than the traditional frame agitator.

[0064] A film spraying component 8h is added to the polycondensation reactor 8. The structure of the film spraying component 8h is shown in FIG. Figure 3 、 Figure 4 During the reaction phase of the materials in the polycondensation reactor 8, the materials are self-circulated through the polycondensation gear pump 8c and the electric three-way valve S5, and then through the film spraying component 8h. The materials flowing out of the film spraying component 8h are in a thin film state, which enlarges the evaporation surface of the materials, is conducive to the volatilization and separation of small molecules in the materials, accelerates the polycondensation reaction speed, and plays a partial role of the agitator.

[0065] The heat medium pipe at the outlet of the polycondensation heat medium pump 8a supplies heat to the heating coil and heating jacket of the polycondensation kettle 8. The heat medium flowing out of the heating coil and heating jacket of the polycondensation kettle 8 returns to the inlet of the polycondensation heat medium pump 8a for circulation, or returns to the inlet of the polycondensation heat medium pump 8a for circulation through the heat medium radiator 10, or returns to the primary heat medium return pipe G15 for circulation; the primary heat medium supply pipe G14 is connected to the inlet pipe of the polycondensation heat medium pump 8a through the temperature control regulating valve group 8b.

[0066] The material inlet of the polycondensation kettle 8 is connected to the outlet of the second esterification polycondensation filter 5c. The polycondensation kettle 8 is equipped with an agitator, an inner coil, a jacket, and a polycondensation heat medium pump 8a and a temperature control regulating valve group 8b. The material outlet of the polycondensation kettle 8 is connected to the inlet of the polycondensation gear pump 8c. The outlet of the polycondensation gear pump 8c is connected to the inlet of the electric three-way valve S5. A viscometer 12 is provided on the connecting pipe between them. Outlet 1 of the electric three-way valve S5 is connected to the film spraying component 8h, and outlet 2 is connected to the pelletizer granulation equipment 13.

[0067] The gas phase outlet of the polycondensation kettle 8 is connected to the inlet of the second cooler 8d. The top gas phase outlet of the second cooler 8d is connected to the inlet of the second cyclone separator 8e. The bottom liquid phase outlet of the second cooler 8d is connected to the inlet of the second polycondensation receiving tank 8f. The drainage of the second polycondensation receiving tank 8f is recycled. The bottom liquid phase outlet of the second cyclone separator 8e is also connected to the top inlet of the second polycondensation receiving tank 8f. The top balance outlet of the second cyclone separator 8e is connected to the top balance inlet of the second polycondensation receiving tank 8f. The top gas phase outlet of the second cyclone separator 8e is connected to the inlet of the second buffer tank 8g. The drainage of the second buffer tank 8g is recycled. The top outlet of the second buffer tank 8g is connected to the inlet of the polycondensation vacuum pump group 9. A nitrogen pipe G9 is connected to the top of the polycondensation kettle 8.

[0068] When the reaction in the second esterification and pre-polycondensation reactor 5 is complete, both the second esterification and pre-polycondensation reactor 5 and the polycondensation reactor 8 are under vacuum, with a vacuum pressure of ≤60 Pa(A). The pre-polycondensation material is then transferred to the polycondensation reactor 8 via the pre-polycondensation gear pump 5h. The agitator and polycondensation gear pump 8c are activated to ensure material self-circulation. The reaction is then directly transferred to the vacuum environment. The agitator, film spraying components, temperature, and vacuum pressure are controlled to further promote the polycondensation reaction. Viscosity changes can be monitored online using a viscometer 12 to ensure that the required intrinsic viscosity of the product is achieved. Normally, the viscosity of PET is between 0.640 and 0.680 dl / g, that of PETG is between 0.730 and 0.830 dl / g, and that of PBT is between 0.900 and 1.25 dl / g. When the material viscosity meets the product requirements, the electric three-way valve S5 is switched on and off, and the polycondensation gear pump 8c is used as the power source to transfer the material to the pelletizer for pelletizing. The entire granulation process takes approximately 30 minutes. Maintaining negative pressure within the polycondensation reactor 8 during discharge effectively minimizes the viscosity drop between the head and tail of the material during discharge, achieving a viscosity drop of ≤0.004 dl / g. Conventional nitrogen-pressurized discharge achieves a viscosity drop of ≤0.008 dl / g between the head and tail, demonstrating that negative pressure discharge mitigates thermal degradation. Because the material has already undergone pre-polycondensation in the second esterification pre-polycondensation reactor 5, reaching an intrinsic viscosity of 0.330-0.400 dl / g, the residence time of the material within the polycondensation reactor 8 is shortened. The total reaction time plus discharge time is approximately 2.2-2.5 hours, enabling the production of 9-10 batches of differentiated PET products per day.

[0069] The jacketed pipe heat medium system is mainly used for heating the material jacketed pipe between the first esterification kettle 2 and the second esterification pre-polycondensation kettle 5, the gas phase jacketed pipe between the second esterification pre-polycondensation kettle 5 and the first cooler 5d, the material jacketed pipe between the second esterification pre-polycondensation kettle 5 and the polycondensation kettle 8, the gas phase jacketed pipe between the polycondensation kettle 8 and the second cooler 8d, and the material jacketed pipe between the electric three-way valve S5 and the pelletizer granulation equipment 13. It is equipped with a jacketed pipe heat medium pump 11 and a temperature control regulating valve group 11a. The heat medium outlet of the material jacketed pipe is connected to the inlet of the jacketed pipe heat medium pump 11, and the outlet of the jacketed pipe heat medium pump 11 is connected to the heat medium inlet of the material jacketed pipe. The inlet of the jacketed pipe heat medium pump 11 is also connected to the primary heat medium supply pipe G14 through the temperature control regulating valve group 11a, so that the temperature of the material jacketed pipe is controlled at about 285°C, which is gentler than the direct heating of the primary heat medium at 315°C, and improves the product quality.

[0070] 1. When producing polyethylene terephthalate (PET):

[0071] Route 1: Terephthalic acid (PTA) + ethylene glycol (EG) + antimony catalyst, mixed evenly in proportion, without heating.

[0072] EG is quantitatively metered into the slurry preparation tank 1 through the EG tube G4 and the pipeline flowmeter. The agitator is turned on, and a certain amount of PTA enters the slurry preparation tank 1 through the feeding hopper 1d. The antimony catalyst is quantitatively metered into the slurry preparation tank 1 through the antimony catalyst tube G3 and its pipeline flowmeter. All raw and auxiliary materials are mixed evenly in the slurry preparation tank 1.

[0073] The material in the slurry preparation tank 1 is uniformly transported to the first esterification kettle 2 through the slurry pump 1c. The first esterification kettle 2 needs to be stirred and mixed to update the material liquid level. The reaction is carried out under normal pressure, the reaction temperature is maintained at 255°C, and the reaction time is 2.2 to 2.5 hours. After the first esterification kettle 2 is transferred, half of the esterification material needs to be retained in the kettle as mother liquor. The water produced by the reaction is promptly separated from the No. 1 process tower 3 to the first esterification receiving tank 3d.

[0074] The material in the first esterification reactor 2 is transferred to the second esterification pre-polycondensation reactor 5 by nitrogen pressure. Stabilizer is added from the second esterification pre-polycondensation reactor 5, and other additives are added according to product requirements. Stirring and mixing are started to update the material liquid level. Normal pressure esterification reaction and negative pressure pre-polycondensation reaction are carried out, and the final reaction temperature of the material is 283°C. The small amount of water and excess alcohol produced by the reaction in the second esterification pre-polycondensation reactor 5 are promptly separated from the second process tower 6 to the second esterification receiving tank 6c. The esterification reaction and additive addition and mixing time are 10-40 minutes, and the pre-polycondensation reaction time is 2.2-2.5 hours. The resulting material has an intrinsic viscosity of 0.330-0.400 dl / g.

[0075] The second esterification pre-polycondensation kettle 5 and the polycondensation kettle 8 are both under high vacuum conditions. The material is transported to the polycondensation kettle 8 by the pre-polycondensation gear pump 5h. The polycondensation kettle 8 needs to be stirred to update the material liquid level. The vacuum degree is ≤60Pa(A). The final temperature of the material reaction is 286℃. The small amount of alcohol produced by the reaction needs to be devolatilized and separated in time. The polycondensation reaction time + the discharge time is a total of 2.2~2.5 hours. The intrinsic viscosity of the discharged material can be controlled in the range of 0.640~0.680dl / g.

[0076] Route 2: Dimethyl terephthalate (DMT) + EG. Since the melting point of DMT is 140.6°C, the crystalline DMT raw material needs to be pre-melted at 150°C and then mixed evenly with EG in a certain proportion.

[0077] EG is quantitatively metered into the slurry preparation tank 1 through the EG pipe G4 and the pipeline flowmeter, and the crystalline raw material DMT is quantitatively fed into the slurry preparation tank 1 through the feeding hopper 1d. The temperature is raised by the slurry heat medium pump 1a. After the slurry preparation tank 1 is heated to 150°C, stirring is started and pre-melted and mixed evenly in the slurry preparation tank 1.

[0078] The slurry in the slurry preparation tank 1 is all delivered to the first esterification kettle 2 through the slurry pipe G13 within eight minutes. The power source is the equipment potential difference. The first esterification kettle 2 is added with an esterification catalyst, and the material liquid level is updated by stirring and mixing. The reaction is carried out at normal pressure. The reaction temperature is controlled from 150°C to 230°C with a slow gradient temperature increase. The reaction time is 2.2 to 2.5 hours. The methanol produced by the reaction is promptly separated from the No. 1 process tower 3 to the first esterification receiving tank 3d.

[0079] The material in the first esterification reactor 2 is transferred to the second esterification pre-polycondensation reactor 5 by nitrogen pressure. Stabilizer, polycondensation catalyst and other additives are added from the second esterification pre-polycondensation reactor 5, and stirring and mixing are started to update the material liquid level. Normal pressure esterification reaction and negative pressure pre-polycondensation reaction are carried out, and the final reaction temperature of the material is 283°C. A small amount of methanol produced by the reaction and excess alcohol are promptly separated from the second process tower 6 to the second esterification receiving tank 6c. The cross-esterification reaction and additive addition mixing time are 10-40 minutes, and the pre-polycondensation reaction time is 2.2-2.5 hours. The resulting material has an intrinsic viscosity of 0.330-0.400 dl / g.

[0080] The second esterification pre-polycondensation kettle 5 and the polycondensation kettle 8 are both under high vacuum conditions. The material is transported to the polycondensation kettle 8 by the pre-polycondensation gear pump 5h. The polycondensation kettle 8 needs to be stirred to update the material liquid level. The vacuum degree is ≤60Pa(A). The final temperature of the material reaction is 286℃. The small amount of alcohol produced by the reaction needs to be devolatilized and separated in time. The polycondensation reaction time + the discharge time is a total of 2.2~2.5 hours. The intrinsic viscosity of the discharged material can be controlled in the range of 0.640~0.680dl / g.

[0081] 2. When producing polybutylene terephthalate (PBT):

[0082] Route 1: PTA + 1,4-butanediol (BDO) + ​​titanium catalyst. Since the melting point of BDO is 20.2°C, the temperature needs to be controlled at around 35°C and mixed evenly according to the proportion.

[0083] BDO is quantitatively metered into slurry preparation tank 1 via BDO tube G5 and an inline flowmeter. The agitator is turned on, and the slurry heat medium pump 1a is used to raise the temperature of slurry preparation tank 1 to 35°C. A predetermined amount of PTA is introduced into slurry preparation tank 1 via hopper 1d. A titanium catalyst is quantitatively metered into slurry preparation tank 1 via titanium catalyst tube G1 and an inline flowmeter. All raw materials and auxiliary materials are uniformly mixed in slurry preparation tank 1, and the slurry temperature is maintained at 35°C.

[0084] The material in the slurry preparation tank 1 is uniformly transported to the first esterification kettle 2 through the slurry pump 1c. The first esterification kettle 2 stirs and mixes the material to update the liquid level, and reacts under negative pressure. The vacuum pressure is controlled at 60 kPa (A). The reaction temperature is maintained at about 230 ° C, and the reaction time is about 2.5 to 3 hours. After the material is transferred from the first esterification kettle 2, half of the esterification material needs to be retained in the kettle as the mother liquor. The water and tetrahydrofuran produced by the reaction are promptly separated from the No. 1 process tower 3 to the first esterification receiving tank 3d and the liquid seal tank 3e.

[0085] The materials in the first esterification reactor 2 are transferred to the second esterification pre-polycondensation reactor 5 using nitrogen pressure. Stabilizers and other additives are added from the second esterification pre-polycondensation reactor 5, and stirring and mixing are initiated to refresh the liquid level. Esterification reaction at normal pressure is followed by pre-polycondensation reaction at negative pressure, with the final reaction temperature at 244°C. The small amount of tetrahydrofuran, water, and excess alcohol produced by the reaction are promptly separated from the second process tower 6 and transferred to the second esterification receiving tank 6c. The esterification reaction and additive addition and mixing time are 10-40 minutes, and the pre-polycondensation reaction time is 2-2.5 hours. The resulting material has an intrinsic viscosity of 0.350-0.420 dl / g.

[0086] The second esterification pre-polycondensation kettle 5 and the polycondensation kettle 8 are both under high vacuum conditions. The material is transported to the polycondensation kettle 8 by the pre-polycondensation gear pump 5h. The polycondensation kettle 8 needs to be stirred to update the material liquid level. The vacuum degree is ≤60Pa(A). The final temperature of the material reaction is 248°C. A small amount of alcohol and tetrahydrofuran produced by the reaction need to be devolatilized and separated in time. The polycondensation reaction time + discharge time is a total of 2.5 to 3 hours. The intrinsic viscosity of the discharged material can be controlled in the range of 0.900 to 1.250 dl / g.

[0087] Route 2: DMT+BDO. The DMT crystalline raw material needs to be pre-melted at 150°C and then mixed evenly with BDO in a certain proportion.

[0088] BDO is quantitatively metered into the slurry preparation tank 1 through the BDO pipe G5 and the pipeline flowmeter, and the crystalline raw material DMT is quantitatively fed into the slurry preparation tank 1 through the feeding hopper 1d. The temperature is raised by the slurry heat medium pump 1a. After the slurry preparation tank 1 is heated to 150°C, stirring is started and pre-melted and mixed evenly in the slurry preparation tank 1.

[0089] The slurry in slurry preparation tank 1 is delivered to the first esterification reactor 2 via slurry pipe G13 within eight minutes. The power source is the equipment head differential. The first esterification reactor 2 stirs and mixes the material to refresh the liquid level. The reaction is carried out under negative pressure, with the vacuum pressure controlled at 60 kPa(A). The reaction temperature is controlled to rise gradually from 150°C to 192°C, for a reaction time of 2.5-3 hours. The methanol, tetrahydrofuran, and water produced by the reaction are promptly separated from process tower 1 3 and transferred to the first esterification receiving tank 3d.

[0090] The material in the first esterification reactor 2 is transferred to the second esterification pre-polycondensation reactor 5 by nitrogen pressure. Stabilizer, polycondensation catalyst and other additives are added from the second esterification pre-polycondensation reactor 5, and stirring and mixing are started to refresh the material liquid level. Normal pressure esterification reaction and negative pressure pre-polycondensation reaction are carried out, and the final reaction temperature of the material is 244°C. The small amount of tetrahydrofuran, methanol and excess alcohol produced by the reaction are promptly separated from the second process tower 6 to the second esterification receiving tank 6c. The cross-esterification reaction and additive addition mixing time are 10-40 minutes, and the pre-polycondensation reaction time is 2-2.5 hours. The resulting material has an intrinsic viscosity of 0.350-0.420 dl / g.

[0091] The second esterification pre-polycondensation kettle 5 and the polycondensation kettle 8 are both under high vacuum conditions. The material is transported to the polycondensation kettle 8 by the pre-polycondensation gear pump 5h. The polycondensation kettle 8 needs to be stirred to update the material liquid level. The vacuum degree is ≤60Pa(A). The final temperature of the material reaction is 248°C. A small amount of alcohol and tetrahydrofuran produced by the reaction need to be devolatilized and separated in time. The polycondensation reaction time + discharge time is a total of 2.5 to 3 hours. The intrinsic viscosity of the discharged material can be controlled in the range of 0.900 to 1.250 dl / g.

[0092] 3. When producing polyethylene terephthalate-1,4-cyclohexane dimethanol (PETG):

[0093] Route 1: PTA + EG + 1,4-cyclohexanedimethanol (CHDM) + antimony catalyst. Since the melting point of CHDM is 31.5°C, the temperature needs to be controlled at around 50°C and then mixed evenly according to the proportion.

[0094] Taking the CHDM slurry preparation for PETG production as an example, EG is quantitatively metered into slurry preparation tank 1 via EG pipe G4 and a pipeline flowmeter. The agitator is turned on, and the temperature of slurry preparation tank 1 is raised via slurry heat medium pump 1a to control the temperature of slurry preparation tank 1 at 50°C. Pre-melted CHDM is quantitatively metered into slurry preparation tank 1 via CHDM / NPG pipe G2 and its pipeline flowmeter. A certain amount of PTA enters slurry preparation tank 1 via hopper 1d. Antimony-based catalyst is quantitatively metered into slurry preparation tank 1 via antimony-based catalyst pipe G3 and its pipeline flowmeter. All raw and auxiliary materials are evenly mixed in slurry preparation tank 1, and the slurry temperature is always controlled at 50°C.

[0095] The material in the slurry preparation tank 1 is uniformly transported to the first esterification kettle 2 through the slurry pump 1c. The titanium catalyst is added from the first esterification kettle 2. The first esterification kettle 2 needs to be stirred and mixed to update the material liquid level. The reaction is carried out at normal pressure, the reaction temperature is maintained at 250°C, and the reaction time is 2.5 to 3 hours. After the first esterification kettle 2 is transferred, half of the esterification material needs to be retained in the kettle as the mother liquor. The water produced by the reaction is promptly separated from the No. 1 process tower 3 to the first esterification receiving tank 3d.

[0096] The material in the first esterification reactor 2 is transferred to the second esterification pre-polycondensation reactor 5 by nitrogen pressure. Stabilizer and other additives are added from the second esterification pre-polycondensation reactor 5 and stirred and mixed to refresh the material liquid level. Normal pressure esterification reaction and negative pressure pre-polycondensation reaction are carried out. The final reaction temperature of the material is 282°C. The small amount of water and excess alcohol produced by the reaction are promptly separated from the second process tower 6 to the second esterification receiving tank 6c. The esterification reaction and additive addition and mixing time are 10-40 minutes, and the pre-polycondensation reaction time is 2-2.5 hours. The resulting material has an intrinsic viscosity of 0.350-0.420 dl / g.

[0097] The second esterification pre-polycondensation kettle 5 and the polycondensation kettle 8 are both under high vacuum conditions. The material is transported to the polycondensation kettle 8 by the pre-polycondensation gear pump 5h. The polycondensation kettle 8 needs to be stirred to update the material liquid level. The vacuum degree is ≤80Pa(A). The final temperature of the material reaction is 285℃. The small amount of alcohol and tetrahydrofuran produced by the reaction needs to be devolatilized and separated in time. The polycondensation reaction time + discharge time is 2.5~3 hours in total. The intrinsic viscosity of the discharged material can be controlled in the range of 0.730~0.830dl / g.

[0098] Cooling water is introduced into the cold side of the first esterification No. 1 cooler 3a, the cold side of the first esterification No. 2 cooler 3b, the cold side of the No. 1 cooler 5d, the jacket of the No. 1 cyclone separator 5e, the shell side of the No. 2 cooler 8d, and the jacket of the No. 2 cyclone separator 8e as a cooling medium.

[0099] The above description is only a preferred embodiment of the present invention, which shows and describes the basic principles, main features and advantages of the present invention, but does not limit the scope of patent protection of the present invention. Those skilled in the art should understand that the present invention is not limited by the above embodiments. In addition to the above embodiments, the present invention may have other implementation methods without departing from the spirit and scope of the present invention. The present invention may also have various changes and improvements, and all technical solutions formed by equivalent replacement or equivalent transformation fall within the scope of protection required by the present invention. The scope of protection required by the present invention is defined by the attached claims and their equivalents. Technical features not described in the present invention can be achieved by or using existing technologies, and will not be described here.

Claims

1. A compatible high-viscosity semi-continuous polyester production equipment, including a slurry mixing tank, characterized by: The top of the slurry preparation tank is provided with titanium catalyst, CHDM / NPG, antimony catalyst, EG and BDO injection ports. The slurry outlet 1 of the slurry preparation tank is connected to the inlet of the first esterification kettle through a slurry pump, and the slurry outlet 2 of the slurry preparation tank is directly connected to the inlet of the first esterification kettle. The top of the first esterification kettle is also provided with esterification catalyst and titanium catalyst injection ports. The first esterification kettle has two material outlets, one extends to the bottom of the kettle and is provided with a No. 1 electric valve at the outlet, and the other extends in the middle of the kettle and is provided with a No. 2 electric valve at the outlet. The outlets of the No. 1 electric valve and the No. 2 electric valve are connected in parallel and then connected to the feed port of the second esterification pre-polycondensation kettle through the first esterification filter. The top of the second esterification pre-polycondensation kettle is also provided with a stabilizer, a polycondensation catalyst and a nitrogen injection port; the material outlet of the second esterification pre-polycondensation kettle is connected to the material inlet of the polycondensation kettle through the pre-polycondensation gear pump and the second esterification polycondensation filter; the material outlet of the polycondensation kettle is connected to the inlet of the polycondensation gear pump, and the outlet of the polycondensation gear pump is connected to the pelletizer granulation equipment.

2. The compatible high-viscosity semi-continuous polyester production equipment according to claim 1, characterized in that: The outlet of the polycondensation gear pump is connected to the inlet of the electric three-way valve and a viscometer is provided on the connecting pipe. The first outlet of the electric three-way valve is connected to the film spraying component on the upper part of the inner cavity of the polycondensation kettle through a connecting pipe. The film spraying component extends in the horizontal direction and has a slit-shaped outlet at the bottom; the second outlet of the electric three-way valve is connected to the pelletizer granulation equipment.

3. The compatible high-viscosity semi-continuous polyester production equipment according to claim 2, characterized in that: The film spraying component is a tapered box extending in the horizontal direction, with an upper portion having a square cross section and a lower portion having an isosceles triangle cross section with a narrowed bottom.

4. The compatible high-viscosity semi-continuous polyester production equipment according to claim 1, characterized in that: The inner cavities of the slurry preparation tank, the first esterification kettle, the second esterification pre-polycondensation kettle, and the polycondensation kettle are respectively provided with heating coils and agitators, and the outer walls of the slurry preparation tank, the first esterification kettle, the second esterification pre-polycondensation kettle, and the polycondensation kettle are respectively provided with heating jackets, and the heat medium circulation pipes of each heating jacket are respectively connected to the primary heat medium supply pipe through a temperature control regulating valve group.

5. The compatible high-viscosity semi-continuous polyester production equipment according to claim 4, characterized in that: The agitator in the inner cavity of the polycondensation kettle is a frame-type agitator, and a downward-guiding spiral agitating blade is wound around the central axis of the frame-type agitator.

6. The compatible high-viscosity semi-continuous polyester production equipment according to claim 1, characterized in that: The gas phase outlet of the first esterification kettle is connected to the inlet of the No. 1 process tower, the gas phase outlet of the No. 1 process tower is connected to the inlet of the first esterification cooler No. 1, the liquid phase outlet of the first esterification cooler No. 1 is connected to the inlet of the first esterification buffer tank, and the first esterification buffer tank has two outlets, one outlet is connected to the liquid phase reflux port of the No. 1 process tower, and the other outlet is connected to the first esterification receiving tank; the gas phase outlet of the first esterification cooler No. 1 is connected to the inlet of the first esterification cooler No. 2, the liquid phase outlet of the first esterification cooler No. 2 is connected to the inlet liquid seal pipe of the liquid seal tank, and the gas phase outlet of the first esterification cooler No. 2 is connected to the inlet of the esterification vacuum pump.

7. The compatible high-viscosity semi-continuous polyester production equipment according to claim 1, characterized in that: One gas phase port of the second esterification pre-polycondensation kettle is connected to the inlet of the No. 2 process tower through a shut-off valve, the gas phase outlet of the No. 2 process tower is connected to the inlet of the second esterification cooler, the outlet of the second esterification cooler is connected to the inlet of the second esterification buffer tank, and the outlet of the second esterification buffer tank is divided into two routes, one route is connected to the top liquid phase reflux port of the No. 2 process tower, and the other route is connected to the second esterification receiving tank.

8. The compatible high-viscosity semi-continuous polyester production equipment according to claim 7, characterized in that: The other gas phase outlet of the second esterification pre-condensation kettle is connected to the inlet of the No. 1 cooler through the No. 3 electric valve, the top gas phase outlet of the No. 1 cooler is connected to the inlet of the No. 1 cyclone separator, the bottom liquid phase outlet of the No. 1 cooler and the No. 1 cyclone separator is connected to the No. 1 condensation receiving tank, the top balance outlet of the No. 1 cyclone separator is connected to the top balance inlet of the No. 1 condensation receiving tank, the top gas phase outlet of the No. 1 cyclone separator is connected to the No. 1 buffer tank, and the top outlet of the No. 1 buffer tank is connected to the pre-condensation vacuum pump group.

9. The compatible high-viscosity semi-continuous polyester production equipment according to claim 1, characterized in that: The gas phase outlet of the polycondensation kettle is connected to the inlet of the No. 2 cooler, the top gas phase outlet of the No. 2 cooler is connected to the inlet of the No. 2 cyclone separator, and the bottom liquid phase outlet of the No. 2 cooler and the No. 2 cyclone separator is connected to the No. 2 polycondensation receiving tank; the top balance outlet of the No. 2 cyclone separator is connected to the top balance inlet of the No. 2 polycondensation receiving tank, and the top gas phase outlet of the No. 2 cyclone separator is connected to the No. 2 buffer tank; the top outlet of the No. 2 buffer tank is connected to the polycondensation vacuum pump group.

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