Polymer production system

Abstract

The utility model provides a polymer production system which is characterized in that a first separation device is used for separating an oil-water mixture from a reaction device so as to obtain a water-phase product and oil-phase products with different boiling points; the second separation device is used for rectifying, condensing and separating the oil-water mixture from the reaction device to obtain an oil-phase product and a water-phase product; the solid material treatment device is used for granulating the solid material in the reaction device and obtaining polymer granules; and the heat-conducting oil device is connected with the reaction device and is used for providing heat-conducting oil for heating or cooling for the reaction device. The first separation device and / or the second separation device can be selectively used according to the production requirements of polymers; the heat conduction oil device can provide different reaction temperature conditions for the reaction device according to polymer production requirements, so that the production system can be used for production of different polymers, meanwhile, one production system can meet various production conditions, and the production cost is reduced.

Description

Technical Field

[0001] The utility model relates to the technical field of polymer production, in particular to a polymer production system. Background Art

[0002] High temperature resistant nylon refers to nylon engineering plastics that can be used for a long time at temperatures above 150°C. High temperature resistant nylon has good wear resistance, heat resistance, oil resistance and chemical resistance. It also greatly reduces the water absorption and shrinkage of raw materials, and has excellent dimensional stability and excellent mechanical strength.

[0003] PA6T is a typical representative of semi-aromatic nylon, which is formed by polycondensation of hexamethylenediamine and terephthalic acid. The melting point of pure PA6T is as high as 370℃. At this temperature, nylon has been degraded and cannot be thermoformed. Therefore, the PA6T circulating in the market is a copolymer or compound with other monomers to reduce the melting point.

[0004] Alkyd resin has mature synthesis technology, a wide range of raw materials, and good coating performance. It is currently the largest resin for coatings. Alkyd resin accounts for more than half of the total amount of synthetic resins for coatings in China. Alkyd resin and alkyd resin coatings play an important and irreplaceable role in the current coatings industry.

[0005] Alkyd resin is an important resin for coatings. It is synthesized by esterification and polycondensation reaction of polyols, polyacids and fatty acids. Alkyd resin is a synthetic resin that is widely used in coatings and is also one of the most widely used synthetic resins in my country. It is cheap, simple to construct, has abundant raw material sources, can be dissolved in a variety of organic solvents, and is suitable for surface coating of all wood and metals.

[0006] In the prior art, nylon 66 is produced directly from hexamethylenediamine and adipic acid as raw materials to produce nylon 66 melt, which is then pelletized by a pelletizer. The main process routes are divided into continuous polymerization, intermittent polymerization, semi-continuous polymerization, etc.

[0007] As a new type of plastic material, polybutylene succinate (PBS) is an ester formed by the frequent double decomposition reaction of succinic acid and butanediol. It has excellent biodegradability and a wide range of uses. It is often used in plastic packaging, tableware, agricultural films, medical polymer materials, etc. Compared with other degradable plastics, PBS has low cost and good performance. It can be effectively polymerized with other different materials. Therefore, its industrial application prospects are very broad and it has good market and economic value.

[0008] Conventional polymerization equipment cannot provide a variety of reaction conditions for polymer production, so it can only produce a single polymer product with poor market competitiveness. If different polymers are produced, different equipment needs to be used, which requires large equipment investment and high cost. Utility Model Content

[0009] The purpose of the embodiments of the utility model is to provide a polymer production system to solve the problem that polymer production equipment in the prior art cannot meet various polymer production conditions.

[0010] The embodiment of the utility model adopts the following technical solution: a polymer production system, comprising:

[0011] A reaction device, which is used to stir the materials to be reacted so that the materials to be reacted can react in the reaction device to generate oil-water mixture materials and solid materials;

[0012] A first separation device, which is connected to the top of the reaction device and is used to receive the oil-water mixture from the reaction device and separate the oil-water mixture to obtain a water phase output and an oil phase output with different boiling points;

[0013] a second separation device, which is connected to the top of the reaction device, and is used to receive the oil-water mixture from the reaction device, and to perform rectification, condensation and separation treatment on the oil-water mixture to obtain an oil phase output and a water phase output;

[0014] A solid material processing device, connected to the bottom of the reaction device, for pelletizing the solid material in the bottom of the reaction device to obtain polymer pellets;

[0015] A heat transfer oil device is connected to the reaction device and is used to provide heat transfer oil for heating or cooling the reaction device.

[0016] In some embodiments, the first separation device includes a phase separator, an oil phase collection tank, a first heat exchanger, a water phase collection tank, and a vacuum unit;

[0017] The feed port of the phase separator is communicated with the top of the reaction device, and the first discharge port of the phase separator is connected to the oil phase collection tank, so as to transport the oil phase output separated by the phase separator to the oil phase collection tank;

[0018] The second discharge port of the phase separator is connected to the first heat exchanger, and the vacuum unit is connected to the first heat exchanger through a vacuum pipeline, wherein the vacuum unit can enable the reaction device to maintain different vacuum degrees;

[0019] The vacuum pipeline between the first heat exchanger and the vacuum unit is provided with the water phase collection tank for receiving the water phase output separated by the phase separator.

[0020] In some embodiments, a vacuum regulating valve is provided on the vacuum pipeline between the phase separator and the reactor, and the opening of the vacuum regulating valve can be adjusted according to the pressure in the reaction device, thereby adjusting the vacuum degree in the reaction device.

[0021] In some embodiments, the first separation device further comprises a vacuum buffer tank, and the vacuum buffer tank is disposed on the vacuum pipeline between the water phase collection tank and the vacuum unit.

[0022] In some embodiments, the second separation device includes a distillation tower, a second heat exchanger, and an oil-water separation tank;

[0023] The distillation tower is connected to the top of the reaction device and is used to perform distillation treatment on the oil-water mixture from the reaction device;

[0024] The feed port of the second heat exchanger is connected to the distillation tower and is used to perform heat exchange treatment on the oil-water mixture after distillation treatment by the distillation tower to separate the oil phase product and the water phase product;

[0025] The oil-water separation tank is connected to the discharge port of the second heat exchanger to receive the oil phase product and the water phase product from the second heat exchanger. The oil-water separation tank is also connected to the top of the reaction device to transport the oil phase product back to the reaction device; the oil-water separation tank is also connected to the water phase collection tank to transport the water phase product to the water phase collection tank.

[0026] In some embodiments, a pressure regulating valve is provided on the connecting pipeline connecting the distillation tower and the feed port of the second heat exchanger, and the opening of the pressure regulating valve can be adjusted according to the pressure in the reaction device, thereby achieving the pressure regulation in the reaction device.

[0027] In some embodiments, the discharge port of the second heat exchanger is connected to the oil-water separation tank through a first production pipeline, and a first switch valve is provided on the first production pipeline;

[0028] The second separation device also includes a second production pipeline, one end of which is connected to the discharge port of the second heat exchanger, and the other end of which is connected to the feed port of the second heat exchanger. A second switch valve is provided on the second production pipeline. When the second switch valve is opened, at least part of the oil phase product and at least part of the water phase product discharged through the discharge port of the second heat exchanger are transported back to the second heat exchanger.

[0029] In some embodiments, the thermal oil device includes a thermal oil inlet tee pipe;

[0030] One end of the bypass pipeline is connected to the reaction device, and the other end of the bypass pipeline is connected to the first pipe opening of the tee; the second pipe opening of the tee and the third pipe opening of the tee are respectively connected to the liquid inlets of the distillation tower and the second heat exchanger.

[0031] In some embodiments, the second separation device further comprises a bypass line and a three-way regulating valve;

[0032] One end of the bypass pipeline is connected to the reaction device, and the other end of the bypass pipeline is connected to the first valve port of the three-way regulating valve. The second valve port of the three-way regulating valve and the third valve port of the three-way regulating valve are respectively connected to the liquid inlet of the distillation tower and the second heat exchanger.

[0033] In some embodiments, the solid material processing device includes a bottom valve, a melt pump, a water tank, a blow dryer and a pelletizer;

[0034] The reaction device comprises a reaction kettle, the bottom of which is detachably provided with the kettle bottom valve, the kettle bottom valve is connected to the melt pump, and the melt pump extracts the solid material in the bottom of the reaction kettle;

[0035] The bottom outlet of the melt pump is detachably provided with a casting strip head, so that the solid material in the melt pump can be extruded in a strip shape through the casting strip head;

[0036] The water tank is used to receive the extruded strip-shaped fixed material and cool the strip-shaped solid material;

[0037] The blow dryer is used to blow dry the strip-shaped fixed material after being cooled in the water tank;

[0038] The pelletizer is used to cut the strip-shaped solid material after the blow-drying process and obtain polymer pellets.

[0039] The beneficial effects of the embodiments of the utility model are:

[0040] By arranging the first separation device, the second separation device and the heat transfer oil device in the production system, the first separation device or the second separation device can be selected according to the production needs of the polymer. At the same time, the heat transfer oil device can provide different reaction temperature conditions for the reaction device according to the needs of polymer production, so that the production system can be used for the production of different polymers. At the same time, one production system can meet a variety of production conditions, thereby reducing production costs. BRIEF DESCRIPTION OF THE DRAWINGS

[0041] In order to more clearly illustrate the technical solutions in the embodiments of the utility model or related technologies, the drawings required for use in the embodiments or related technical descriptions are briefly introduced below. Obviously, the drawings described below are only some embodiments recorded in the utility model. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative labor.

[0042] Figure 1 It is a structural schematic diagram of the polymer production system of the utility model.

[0043] Figure numerals: 1. Reactor; 2. Distillation tower; 3. Phase separator; 4. Melt pump; 5. Oil-water separation tank; 6. Pelletizer; 7. Blow dryer; 8. Water tank; 9. Circulation heater; 10. Oil chiller; 11. Water phase collecting tank; 12. Vacuum buffer tank; 13. Oil phase collecting tank; 14. Vacuum unit; 15. Second heat exchanger; 16. First heat exchanger; 17. Condenser; 18. Hot oil pump; 19. Kettle bottom valve; 20. Casting strip head. DETAILED DESCRIPTION

[0044] Various aspects and features of the present invention are described herein with reference to the accompanying drawings.

[0045] It should be understood that various modifications may be made to the embodiments of the present application. Therefore, the above description should not be considered as limiting, but only as an example of the embodiments. Other modifications within the scope and spirit of the present utility model will occur to those skilled in the art.

[0046] The accompanying drawings, which are included in and constitute a part of the specification, illustrate embodiments of the present invention and, together with the general description of the present invention given above and the detailed description of the embodiments given below, are used to explain the principles of the present invention.

[0047] These and other characteristics of the invention will become apparent from the following description of a preferred form of embodiment given as a non-limiting example, with reference to the accompanying drawings.

[0048] It should also be understood that, although the present invention has been described with reference to some specific examples, those skilled in the art will be able to realize many other equivalent forms of the present invention with certainty, which have features such as the above-mentioned "utility model content" and are therefore within the scope of protection defined thereby.

[0049] The above and other aspects, features and advantages of the present invention will become more apparent from the following detailed description when taken in conjunction with the accompanying drawings.

[0050] Specific embodiments of the present invention are described hereinafter with reference to the accompanying drawings; however, it should be understood that the embodiments applied for are merely examples of the present invention, which may be implemented in a variety of ways. Well-known and / or repeated functions and structures are not described in detail to avoid unnecessary or redundant details that obscure the present invention. Therefore, the specific structural and functional details applied for herein are not intended to be limiting, but merely serve as the basis and representative basis for the above-mentioned "utility model content" to teach those skilled in the art to use the present invention in a variety of ways with substantially any suitable detailed structure.

[0051] This specification may use the phrases "in one embodiment", "in another embodiment", "in yet another embodiment" or "in other embodiments", all of which may refer to one or more of the same or different embodiments according to the present invention.

[0052] In order to solve the problems in the background technology, the utility model provides a polymer production system.

[0053] like Figure 1 As shown, the polymer production system includes a reaction device, a first separation device, a second separation device, a solid material processing device and a heat transfer oil device. Among them, the first separation device and the second separation device can be used separately as two independent separation devices. For example, according to the needs of polymer production, the first separation device can be used in conjunction with the reaction device, the solid material processing device and the heat transfer oil device to produce a polymer; and when it is necessary to produce another polymer different from the polymer, the second separation device can be used in conjunction with the reaction device, the solid material processing device and the heat transfer oil device for production. Of course, it can be understood that the first separation device can be used in conjunction with the reaction device, the solid material processing device and the heat transfer oil device to produce another polymer different from the above two polymers by adjusting the reaction conditions.

[0054] Specifically, the reaction device is used to stir the materials to be reacted so that the materials to be reacted can react in the reaction device to generate oil-water mixture materials and solid materials. The reaction device has a storage space that can accommodate the materials to be reacted, and a stirrer structure can be set in the storage space to stir the reaction materials. While stirring, the reaction device is equipped with production conditions corresponding to the materials to be reacted. For example, corresponding to the polymer to be produced, the reaction device is equipped with reaction conditions required for the materials to be reacted. The reaction conditions can be a set pressure range, a set vacuum range, or a set temperature range, etc. Under the above reaction conditions, the materials to be reacted react to generate an oil-water mixture and solid materials corresponding to the polymer to be produced.

[0055] The first separation device is connected to the top of the reaction device, and is used to receive the oil-water mixture from the reaction device. A first discharge switch valve S1 is provided between the first separation device and the top of the reaction device. When the first discharge switch valve S1 is opened, the oil-water mixture in the reaction device can enter the first separation device from the top of the reaction device for separation treatment. For example, the first separation device can perform separation treatment on the oil-water mixture within a set vacuum range to obtain water phase output and oil phase outputs with different boiling points. For example, the same reacted material in the reaction device can generate different oil-water mixtures and solid materials within different vacuum ranges. Similarly, by using the first separation device to separate the oil-water mixture, different water phase outputs and oil phase outputs with different boiling points can be obtained.

[0056] The second separation device is connected to the top of the reaction device, and is used to receive the oil-water mixture from the reaction device, and to perform distillation, condensation and separation treatment on the oil-water mixture to obtain an oil phase output and an aqueous phase output. A second discharge switch valve S2 is provided between the second separation device and the top of the reaction device. When the second discharge switch valve S2 is opened, the oil-water mixture in the reaction device can enter the second separation device from the top of the reaction device for separation treatment. For example, the oil-water mixture is subjected to distillation treatment, condensation treatment and separation treatment to obtain an oil phase output and an aqueous phase output, and the oil phase output and the aqueous phase output here may be different from the oil phase output and the aqueous phase output obtained by the separation treatment of the first separation device.

[0057] Whether to use the first separation device and the second separation device can be selected by opening or closing the first discharge switch valve S1 and the second discharge switch valve S2. By selecting the first separation device and the second separation device, the polymer production system can be used to produce different polymers.

[0058] The solid material processing device is connected to the bottom of the reaction device and is used to pelletize the solid material in the bottom of the reaction device to obtain polymer pellets. The solid material generated in the reaction device when the first separation device is used is different from the solid material generated in the reaction device when the second separation device is used, and different polymer pellets are obtained after pelletizing by the solid material processing device.

[0059] The heat transfer oil device is connected to the reaction device and is used to provide the reaction device with heat transfer oil for heating or cooling. When the reaction device needs to be heated or kept warm, the heat transfer oil device can provide the reaction device with heat transfer oil for heating; when the reaction device needs to be cooled, the heat transfer oil device can provide the reaction device with heat transfer oil for cooling.

[0060] The embodiment of the utility model sets a first separation device, a second separation device and a heat transfer oil device in the production system. According to the production needs of the polymer, the first separation device or the second separation device can be selected for use. At the same time, the heat transfer oil device can provide different reaction temperature conditions for the reaction device according to the needs of polymer production, so that the production system can be used for the production of different polymers. At the same time, one production system can meet multiple production conditions, reducing production costs.

[0061] In one embodiment of the present invention, Figure 1 As shown, the first separation device includes a phase separator 3, an oil phase collecting tank 13, a first heat exchanger 16, a water phase collecting tank 11 and a vacuum unit 14.

[0062] The feed port of the phase separator 3 is connected to the top of the reaction device through the phase separator pipeline G7, and the first discharge switch valve S1 is arranged on the phase separator pipeline G7. The main body of the phase separator 3 is a tank body, and the tank body is provided with a first discharge port and a second discharge port. The phase separator 3 is used to separate the oil-water mixture so that the oil phase and the water phase in the oil-water mixture are separated. For example, the first discharge port of the phase separator 3 is connected to the oil phase collection tank 13 to transport the oil phase output separated by the phase separator 3 to the oil phase collection tank 13. The second discharge port of the phase separator 3 is connected to the first heat exchanger 16, and the vacuum unit 14 is connected to the first heat exchanger 16 through the vacuum pipeline G1, wherein the vacuum unit 14 can enable the reaction device to maintain different vacuum degrees, so that the reaction device can have different vacuum reaction conditions to produce different polymers.

[0063] The vacuum pipeline G1 between the first heat exchanger 16 and the vacuum unit 14 is provided with a water phase collection tank 11 for receiving the water phase output separated by the phase separator 3. That is, the water phase separated by the phase separator 3 can enter the water phase collection tank 11 through the first heat exchanger 16 and the vacuum pipeline G1.

[0064] In one embodiment of the utility model, a vacuum regulating valve V1 is provided on the vacuum pipeline G7 between the phase separator 3 and the reactor. The opening of the vacuum regulating valve V1 can be adjusted according to the pressure in the reaction device, thereby adjusting the vacuum degree in the reaction device to meet the requirements of the reaction device for the required vacuum degree during polymer production.

[0065] In one embodiment of the utility model, the first separation device further includes a vacuum buffer tank 12, which is arranged on the vacuum pipeline G1 between the water phase collection tank 11 and the vacuum unit 14. That is, a vacuum buffer tank 12 is also arranged on the vacuum pipeline G1 between the water phase collection tank 11 and the vacuum unit 14. The function of the vacuum buffer tank 12 is to buffer the pressure and prevent backflow, and it can also be used to provide a stable vacuum degree for gas-liquid separation in the oil-water mixture (to avoid the vacuum degree failing to meet the production requirements).

[0066] In one embodiment of the present invention, Figure 1 As shown, the second separation device includes a distillation tower 2 , a second heat exchanger 15 and an oil-water separation tank 5 .

[0067] A second discharge switch valve S2 is provided on the connecting pipeline between the distillation tower 2 and the top of the reaction device. When the second discharge switch valve S2 is opened, the oil-water mixture in the reaction device will enter the distillation tower 2 for distillation treatment.

[0068] The second heat exchanger 15 has a feed port and a discharge port. The feed port of the second heat exchanger 15 can be connected to the top of the distillation tower 2. The second heat exchanger 15 is used to perform heat exchange treatment on the oil-water mixture after distillation treatment by the distillation tower 2 to separate the oil phase product and the water phase product. The oil phase product and the water phase product are discharged through the discharge port of the second heat exchanger 15.

[0069] The oil-water separation tank 5 is connected to the discharge port of the second heat exchanger 15 to receive the oil phase product and the water phase product from the second heat exchanger 15. The oil-water separation tank 5 is also connected to the top of the reaction device through the oil phase return pipeline G9 to transport the oil phase product back to the reaction device. The oil phase return pipeline G9 is provided with a pneumatic stop valve V5, and the conduction and cutoff of the oil phase return pipeline G9 can be controlled by controlling the opening and closing of the pneumatic stop valve V5. The oil-water separation tank 5 is also connected to the water phase collection tank 11 through the water phase collection pipeline G2 of the distillation tower 2 to transport the water phase product to the water phase collection tank 11. That is, the water phase product separated by the oil-water separation tank 5 can be transported to the water phase collection tank 11 through the water phase collection pipeline G2 of the distillation tower 2, thereby realizing the collection and storage of the water phase product, and can be discharged and processed as needed later.

[0070] In one embodiment of the utility model, a pressure regulating valve V2 is provided on the connecting pipeline connecting the distillation tower 2 and the feed port of the second heat exchanger 15. The opening of the pressure regulating valve V2 can be adjusted according to the pressure in the reaction device, thereby realizing automatic adjustment of the pressure in the reaction device to meet the pressure reaction conditions required for the production of different polymers.

[0071] In one embodiment of the utility model, the discharge port of the second heat exchanger 15 is provided with a production pipeline G10, and the production pipeline is divided into two branches, namely the first production pipeline and the second production pipeline. Among them, the production buckle of the second heat exchanger 15 is connected to the oil-water separation tank 5 through the first production pipeline, and the first production pipeline is provided with a first switch valve K1. When the first switch valve K1 is opened, the oil phase product and the water phase product discharged from the second heat exchanger 15 enter the oil-water separation tank 5 for re-separation.

[0072] One end of the second extraction pipeline is connected to the discharge port of the second heat exchanger 15, and the other end of the second extraction pipeline is connected to the feed port of the second heat exchanger 15. A second switch valve K2 is provided on the second extraction pipeline. When the second switch valve is opened, at least part of the oil phase product and at least part of the water phase product discharged through the discharge port of the second heat exchanger 15 are transported back to the second heat exchanger 15. The first switch valve K1 and the second switch valve K2 are opened and closed in conjunction.

[0073] In one embodiment of the present invention, the thermal oil device includes a thermal oil inlet three-way valve, a thermal oil outlet three-way valve, a hot oil delivery component and a cold oil delivery component.

[0074] An interlayer is arranged outside the reaction device, and the interlayer has an oil inlet and an oil outlet. Heat-conducting oil can flow in the interlayer, so as to heat, keep warm, or cool the reaction device through the heat-conducting oil.

[0075] The hot oil delivery assembly includes a hot oil pump 18 and a circulating heater 9 connected to the outlet of the hot oil pump 18 via a hot oil inlet pipeline G3. The inlet of the hot oil pump 18 is connected to the first valve port of the thermal oil inlet three-way valve V3 via a hot oil outlet pipeline G5. The circulating heater 9 is also connected to the first valve port of the thermal oil outlet three-way valve V4 to heat the thermal oil and then transport it back to the oil inlet of the interlayer. The thermal oil enters the interlayer through the oil inlet of the interlayer.

[0076] The cold oil delivery component includes an oil chiller 10 and a condenser 17 connected to the oil chiller 10. The oil chiller 10 is also connected to the second valve port of the thermal oil outlet three-way valve V4 through a cold oil inlet pipeline G4. The condenser 17 is also connected to the second valve port of the thermal oil inlet three-way valve V3 through a cold oil outlet pipeline G6, so as to cool the thermal oil and then transport it back to the oil inlet of the interlayer. The thermal oil enters the interlayer through the oil inlet of the interlayer.

[0077] The third valve port of the heat transfer oil inlet three-way valve V3 is connected to the oil outlet of the interlayer, so that the heat transfer oil in the interlayer is discharged through the oil outlet of the interlayer and then passes through the heat transfer oil inlet three-way valve V3. The third valve port of the heat transfer oil outlet three-way valve V4 is connected to the oil inlet of the interlayer.

[0078] In one embodiment of the present invention, the second separation device further includes a bypass pipeline G8 and a tee pipe.

[0079] One end of the bypass line G8 is connected to the reaction device, and the other end of the bypass line G8 is connected to the first pipe port of the tee, and the second pipe port and the third pipe port of the tee are respectively connected to the liquid inlet of the distillation tower 2 and the second heat exchanger 15.

[0080] When producing a certain polymer product, the first discharge switch valve S1 can be closed, the second discharge switch valve S2 can be opened, and at the same time, the second pipe outlet of the three-way pipe connected to the distillation tower 2 can be directly connected to the distillation tower 2. That is, the oil-water mixture in the reaction device can enter the second heat exchanger 15 directly through the bypass line G8 for heat exchange treatment without undergoing the distillation treatment of the distillation tower 2.

[0081] In one embodiment of the present invention, the solid material processing device includes a bottom valve 19 , a melt pump 4 , a water tank 8 , a blow dryer 7 and a pelletizer 6 .

[0082] The reaction device includes a reactor 1, and a bottom valve 19 is detachably provided at the bottom of the reactor 1. The bottom valve 19 is connected to a melt pump 4, and the melt pump 4 extracts the solid material in the bottom of the reactor 1. Of course, it can be understood that the bottom valve 19 can also be a ball valve for discharging, and the bottom outlet of the reactor 1 can be replaced with a valve according to different solid material conditions.

[0083] The bottom outlet of the melt pump 4 is detachably provided with a strip casting head 20 so that the solid material in the melt pump 4 can be extruded in a strip shape through the strip casting head 20 .

[0084] The water tank 8 may be disposed below the strip casting head 20 to receive the extruded strip-shaped fixed material and cool the strip-shaped solid material.

[0085] The blow dryer 7 is used to blow dry the strip-shaped fixed material after being cooled by the water tank 8, so as to facilitate the subsequent cutting of the strip-shaped fixed material by the pelletizer 6.

[0086] The pelletizer 6 is used to cut the strip-shaped solid material after the blow-drying process and obtain polymer pellets.

[0087] In order to explain the polymer production system more clearly, the utility model will list the production principle of concentrated polymers, as follows:

[0088] Production of the first polymer: Add high-temperature nylon raw materials with a mass concentration of 30% to 80% to the reactor 1 for stirring and mixing, and concentrate and pre-condense after sufficient mixing. Open the hot oil component and heat it with the heat-conducting oil in the interlayer set outside the reactor 1. The working pressure in the reactor 1 is 1.0 to 3.0 MPa, and the working force of the reactor 1 is 3.0 MPa, which can meet the requirements of different materials to be reacted. The materials to be reacted complete a certain pre-condensation reaction in the reactor 1 by heating, increasing pressure, and constant pressure. After the reaction reaches the set process value requirements, continue to reduce the pressure to negative compression polycondensation operation until the viscosity required by the process is reached, and then start the pelletizer 6 to start pelletizing.

[0089] Production of the second polymer: add the succinic acid diacid solution and the butanediol raw material into the reactor 1 for stirring and mixing, perform program heating and heat preservation, and after the reactor 1 is heated to the set temperature, react at normal pressure for a certain period of time. The first separation device and the second separation device can be operated simultaneously, and vacuum is initially evacuated through the vacuum unit 14, and the vacuum degree in the reactor 1 is slowly established. During the concentration and pre-polycondensation, drainage is performed from the distillation tower 2 to retain the raw materials to the greatest extent. Open the hot oil component, and the heat-conducting oil in the interlayer set outside the reactor 1 is heated. The working pressure in the reactor 1 is below -0.090MPa, which can meet the requirements of different materials. After the reaction reaches the process value, open the cold oil component to cool down the reactor 1, and after reaching the temperature, keep it warm for polycondensation operation until the viscosity required by the process is reached, and then start the pelletizer 6 to start pelletizing.

[0090] Production of the third type of polymer: Add alkyd resin alcohol raw materials, stir and mix, heat and dissolve, add anhydride raw materials, continue to stir and mix, heat to a certain temperature, then add aromatic raw materials, program heating and insulation, when the reaction reaches the process conditions, start the cold oil circulation and start the cold oil component, quickly cool to the process conditions, add the kettle oil, and then carry out the discharge operation.

[0091] Production of the fourth type of polymer: Nylon 66 brine solution with a mass concentration of 30-80% enters reactor 1 for concentration and polycondensation, and the working pressure in reactor 1 is 3.0 MPa; it can meet the requirements of different materials to be reacted; the materials to be reacted complete temperature increase, pressure increase, constant pressure, and finally pressure reduction and polycondensation operations in reactor 1 until the process requirements are met, and pelletizer 6 is started to start pelletizing.

[0092] The above describes in detail a number of embodiments of the present invention, but the present invention is not limited to these specific embodiments. Those skilled in the art can make various variations and modifications to the embodiments based on the concept of the present invention, and these variations and modifications should all fall within the scope of protection claimed by the present invention.

Claims

1. A polymer production system, characterized in that include: A reaction device, which is used to stir the materials to be reacted so that the materials to be reacted can react in the reaction device to generate oil-water mixture materials and solid materials; A first separation device, which is connected to the top of the reaction device and is used to receive the oil-water mixture from the reaction device and separate the oil-water mixture to obtain a water phase output and an oil phase output with different boiling points; a second separation device, which is connected to the top of the reaction device, and is used to receive the oil-water mixture from the reaction device, and to perform rectification, condensation and separation treatment on the oil-water mixture to obtain an oil phase output and a water phase output; A solid material processing device, connected to the bottom of the reaction device, for pelletizing the solid material in the bottom of the reaction device to obtain polymer pellets; A heat transfer oil device is connected to the reaction device and is used to provide heat transfer oil for heating or cooling the reaction device.

2. The polymer production system according to claim 1, characterized in that The first separation device comprises a phase separator, an oil phase collection tank, a first heat exchanger, a water phase collection tank and a vacuum unit; The feed port of the phase separator is communicated with the top of the reaction device, and the first discharge port of the phase separator is connected to the oil phase collection tank, so as to transport the oil phase output separated by the phase separator to the oil phase collection tank; The second discharge port of the phase separator is connected to the first heat exchanger, and the vacuum unit is connected to the first heat exchanger through a vacuum pipeline, wherein the vacuum unit can enable the reaction device to maintain different vacuum degrees; The vacuum pipeline between the first heat exchanger and the vacuum unit is provided with the water phase collection tank for receiving the water phase output separated by the phase separator.

3. The polymer production system according to claim 2, characterized in that A vacuum regulating valve is provided on the vacuum pipeline between the phase separator and the reaction device, and the opening of the vacuum regulating valve can be adjusted according to the pressure in the reaction device, thereby adjusting the vacuum degree in the reaction device.

4. The polymer production system according to claim 2, characterized in that The first separation device further comprises a vacuum buffer tank, and the vacuum buffer tank is arranged on the vacuum pipeline between the water phase collection tank and the vacuum unit.

5. The polymer production system according to claim 2, characterized in that: The second separation device includes a distillation tower, a second heat exchanger and an oil-water separation tank; The distillation tower is connected to the top of the reaction device and is used to perform distillation treatment on the oil-water mixture from the reaction device; The feed port of the second heat exchanger is connected to the distillation tower and is used to perform heat exchange treatment on the oil-water mixture after distillation treatment by the distillation tower to separate the oil phase product and the water phase product; The oil-water separation tank is connected to the discharge port of the second heat exchanger to receive the oil phase product and the water phase product from the second heat exchanger. The oil-water separation tank is also connected to the top of the reaction device to transport the oil phase product back to the reaction device; the oil-water separation tank is also connected to the water phase collection tank to transport the water phase product to the water phase collection tank.

6. The polymer production system according to claim 5, characterized in that A pressure regulating valve is provided on the connecting pipeline connecting the distillation tower and the feed port of the second heat exchanger. The opening of the pressure regulating valve can be adjusted according to the pressure in the reaction device, thereby adjusting the pressure in the reaction device.

7. The polymer production system according to claim 5, characterized in that The discharge port of the second heat exchanger is connected to the oil-water separation tank through a first production pipeline, and a first switch valve is provided on the first production pipeline; The second separation device also includes a second production pipeline, one end of which is connected to the discharge port of the second heat exchanger, and the other end of which is connected to the feed port of the second heat exchanger. A second switch valve is provided on the second production pipeline. When the second switch valve is opened, at least part of the oil phase product and at least part of the water phase product discharged through the discharge port of the second heat exchanger are transported back to the second heat exchanger.

8. The polymer production system according to claim 1, characterized in that The thermal oil device comprises a thermal oil inlet three-way valve, a thermal oil outlet three-way valve, a hot oil delivery component and a cold oil delivery component; An interlayer is arranged outside the reaction device, and the interlayer has an oil inlet and an oil outlet; The hot oil delivery assembly includes a hot oil pump and a circulation heater connected to the outlet of the hot oil pump, the inlet of the hot oil pump is connected to the first valve port of the thermal oil inlet three-way valve, and the circulation heater is also connected to the first valve port of the thermal oil outlet three-way valve to heat the thermal oil and then transport it back to the oil inlet of the interlayer; The cold oil delivery assembly includes an oil cooler and a condenser connected to the oil cooler, the oil cooler is also connected to the second valve port of the thermal oil outlet three-way valve, and the condenser is also connected to the second valve port of the thermal oil inlet three-way valve, so as to cool the thermal oil and then deliver it back to the oil inlet of the interlayer; The third valve port of the thermal oil inlet three-way valve is connected to the oil outlet of the interlayer, and the third valve port of the thermal oil outlet three-way valve is connected to the oil inlet of the interlayer.

9. The polymer production system according to claim 5, characterized in that: The second separation device also includes a bypass pipeline and a tee pipe; One end of the bypass pipeline is connected to the reaction device, and the other end of the bypass pipeline is connected to the first pipe opening of the tee; the second pipe opening of the tee and the third pipe opening of the tee are respectively connected to the liquid inlets of the distillation tower and the second heat exchanger.

10. The polymer production system according to claim 1, characterized in that: The solid material processing device includes a bottom valve, a melt pump, a water tank, a blow dryer and a pelletizer; The reaction device comprises a reaction kettle, the bottom of which is detachably provided with the kettle bottom valve, the kettle bottom valve is connected to the melt pump, and the melt pump extracts the solid material in the bottom of the reaction kettle; The bottom outlet of the melt pump is detachably provided with a casting strip head, so that the solid material in the melt pump can be extruded in a strip shape through the casting strip head; The water tank is used to receive the extruded strip-shaped fixed material and cool the strip-shaped solid material; The blow dryer is used to blow dry the strip-shaped fixed material after being cooled in the water tank; The pelletizer is used to cut the strip-shaped solid material after the blow-drying process and obtain polymer pellets.

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