Single-shaft horizontal reaction kettle for final polycondensation of polyethylene naphthalate

Abstract

The invention belongs to the technical field of high polymer material synthesis equipment, and relates to a single-shaft horizontal reaction kettle for final polycondensation of polyethylene naphthalate, which comprises a stirring paddle, a kneading claw and a kettle wall, the stirring paddle comprises a stirring shaft and stirring blades shaped like a Chinese character'yi ', and the kneading claws comprise kneading claws shaped like a Chinese character'yi'; the stirring blades shaped like the Chinese character'yi 'and the kneading claws shaped like the Chinese character'yi' are arranged at intervals in a staggered mode in the axial direction, and when the stirring paddle rotates in the kettle wall, the stirring blades shaped like the Chinese character'yi 'and the kneading claws shaped like the Chinese character'yi' rotate and knead with each other in the kettle wall; through the shape of the stirring blades, the included angle between the stirring blades and the stirring shaft and the shape and the distribution mode of the kneading claws, the kneading efficiency of materials in the reaction kettle is higher; according to the invention, the mass transfer area is increased, the interfacial mass transfer of ethylene glycol molecules is more effective, and the increase of the mass transfer area is beneficial to forward movement of reaction balance, so that synthesis of a high-molecular-weight polyethylene naphthalate (PEN) product is facilitated.

Description

Technical Field

[0001] The invention belongs to the technical field of polymer material synthesis equipment and relates to a uniaxial horizontal reactor used for final polycondensation of polyethylene naphthalate. Background Art

[0002] Polyethylene naphthalate (PEN) resin has excellent barrier properties, thermal stability and mechanical properties, and is an ideal material for electronic information, electronic packaging, optoelectronic devices and special engineering fields. PEN is usually bulk polymerized by ester exchange or direct esterification. The molecular chain of PEN is rigid and the chain motion energy barrier is high, which makes the melt viscosity increase sharply to 10-1000 Pa·s in the later stage of polycondensation. This seriously hinders the interfacial mass transfer process of ethylene glycol from the melt to the gas phase, resulting in difficulty in the forward movement of the polymerization reaction equilibrium and difficulty in synthesizing high molecular weight PEN resin. In order to solve the problem of mass transfer difficulties caused by the high final polycondensation viscosity, the final polycondensation of polyesters such as PEN is usually carried out in a horizontal disc reactor or a cage reactor. The disc reactor is a common type of reactor and plays a role in many polymerization reactions. The disc reactor has the characteristics of relatively simple structure and relatively stable operation.

[0003] However, the structural characteristics of the disc reactor determine that its mass transfer area has certain limitations. In the PEN synthesis process, the mass transfer process is of great significance for the mixing of raw materials and the diffusion of reaction products. The size of the mass transfer area will affect the progress and efficiency of the reaction. This characteristic limits the performance of the disc reactor in synthesizing high molecular weight PEN to a certain extent. The structure of the cage reactor is similar to the shape of a cage, with complex structural components inside. When processing some low-viscosity and fluid materials, the internal structure of the cage reactor can promote the mixing of materials in different directions. When processing high-viscosity materials, due to the complexity of its internal structure, the material is prone to form some areas with extremely low flow rate or even near stagnation during the flow process, which is the so-called large dead zone volume. For example, in the high-viscosity polyester synthesis reaction, the high viscosity characteristics of the material increase its flow resistance in the cage reactor, and dead zones are easily formed in some corners or areas with complex structures. In these dead zones, the material cannot fully participate in the reaction, resulting in incomplete reaction, affecting the quality and yield of the product.

[0004] Therefore, a device or method suitable for enhancing mass transfer of high-viscosity materials, having a small dead zone volume, and being conducive to the synthesis of high molecular weight PEN products is needed to solve the above technical problems. Summary of the invention

[0005] The present invention adopts a special single-axis structure and is equipped with a special kneading element on the axis, which can continuously shear, stretch and remix the materials during the reaction process. Compared with the disc reactor, its special structure increases the mass transfer area, making the contact between the reactants more sufficient; compared with the cage reactor, it can effectively avoid the problem of high-viscosity materials forming a large dead volume, thereby improving the reaction efficiency and product quality, which is of great significance in the field of chemical reaction engineering.

[0006] The technical solution adopted by the present invention to solve the technical problem is: a uniaxial horizontal reactor for final polycondensation of polyethylene naphthalate, comprising: a stirring paddle, a reactor wall, a left reactor cover, a right reactor cover, and a feeding port, wherein the reactor wall is cylindrical, and the left reactor cover and the right reactor cover are covered on the reactor wall from both ends of the cylinder of the reactor wall;

[0007] The stirring paddle comprises a stirring shaft, which extends axially from one end of the kettle wall into the kettle wall, and a stirring blade in the shape of an outward radial direction is provided on the cylindrical surface of the stirring shaft located in the kettle wall; a stirring blade cross bar is provided on the out-shaped stirring blade, and the stirring blade cross bar extends axially to both ends from the connection of the out-shaped stirring blade, and vertical bars extending radially inward are provided at both ends of the stirring blade cross bar;

[0008] The cylindrical inner wall of the kettle wall is provided with kneading claws, which include "out"-shaped kneading claws extending radially inward from the inner wall of the kettle wall; the "out"-shaped kneading claws are provided with kneading claw cross bars, which extend axially to both ends from the connection of the "out"-shaped kneading claws, and both ends of the kneading claw cross bars are provided with vertical bars extending radially outward;

[0009] The "out"-shaped stirring blades are arranged alternately with the "out"-shaped kneading claws along the axial direction, and the vertical rods of the "out"-shaped stirring blades extend radially inwardly into the inner side of the vertical rods of the adjacent "out"-shaped kneading claws; the vertical rods of the "out"-shaped kneading claws extend radially outwardly into the inner side of the vertical rods of the adjacent "out"-shaped stirring blades;

[0010] When the stirring paddle rotates in the kettle wall, the "out"-shaped stirring paddle and the "out"-shaped kneading claws rotate and knead with each other in the kettle wall.

[0011] Preferably, the stirring blade cross bar is provided with multiple layers radially on the "Out"-shaped stirring blade; the kneading claw cross bar is provided with multiple layers radially on the "Out"-shaped kneading claw; when the "Out"-shaped stirring blade and the "Out"-shaped kneading claw rotate and knead with each other in the kettle wall, the stirring blade cross bar and the axially adjacent multiple layers of kneading claw cross bars rotate and knead with each other.

[0012] More preferably, in two radially adjacent stirring blade cross bars, the vertical bars at both ends of the stirring blade cross bar close to the rotating shaft are vertical bars close to the stirring shaft, and the vertical bars at both ends of the stirring blade cross bar away from the rotating shaft are vertical bars away from the stirring shaft, and the length of the vertical bar close to the stirring shaft is one quarter to three quarters of the length of the vertical bar away from the stirring shaft:

[0013] Of the two radially adjacent kneading claw cross bars, the vertical bars at both ends of the kneading claw cross bar close to the kettle wall are vertical bars close to the kettle wall, and the vertical bars at both ends of the kneading claw cross bar away from the kettle wall are vertical bars away from the kettle wall. The length of the vertical bar away from the kettle wall is one quarter to three quarters of the length of the vertical bar close to the kettle wall.

[0014] Preferably, the kneading claws also include "half-out" type kneading claws extending radially inward from the inner wall of the kettle wall, and the "half-out" type kneading claws are arranged at both ends of the cylinder of the kettle wall, and the kneading claw cross bar of the "half-out" type kneading claws is arranged on one side along the axial direction, and the kneading claw cross bar of the "half-out" type kneading claws extends from the outside to the inside into the cylinder of the kettle wall.

[0015] Preferably, there are multiple "out"-shaped stirring blades, which are arranged around the stirring shaft; there are multiple "out"-shaped kneading claws, which are arranged around the cylindrical inner wall of the kettle wall.

[0016] More preferably, there are 2 to 12 "out" shaped stirring blades, which are evenly distributed around the stirring shaft; there are 2 to 6 "out" shaped kneading claws, which are evenly distributed around the cylindrical inner wall of the kettle wall.

[0017] Preferably, there are a plurality of “out”-shaped stirring blades, and the plurality of “out”-shaped stirring blades are arranged along the axial direction of the stirring shaft.

[0018] Preferably, the feed port is provided with a gas phase discharge port; the left kettle cover or the right kettle cover is provided with a nitrogen hole and a hole for monitoring the melt temperature in the kettle.

[0019] Preferably, the left kettle cover and the right kettle cover are respectively sealed to the kettle wall through flanges.

[0020] Preferably, the stirring paddle, kneading claws, kettle wall and stirring shaft rotate on the same axis, and two ends of the stirring shaft are rotatably connected to the left kettle cover and the right kettle cover respectively.

[0021] The beneficial effects of the present invention are:

[0022] 1. The present invention is conducive to the synthesis of high molecular weight PEN products; the special shape of the stirring blade ("out" shape or "half out" shape) and the specific angle between the stirring blade and the stirring shaft, as well as the special shape of the kneading claw ("out" shape or "half out" shape) and the unique distribution method make the kneading efficiency of the material in the reactor higher. This sufficient kneading action increases the mass transfer area, making the interfacial mass transfer of ethylene glycol molecules more effective. According to the principle of chemical equilibrium, increasing the mass transfer area helps the reaction equilibrium to move forward, which is conducive to the synthesis of high molecular weight polyethylene naphthalate (PEN) products.

[0023] 2. The present invention is suitable for enhancing mass transfer of high-viscosity materials; the two sets of vertical rods of the kneading claws (the length of the vertical rods close to the kettle wall is 1 / 2 of the length of the vertical rods away from the kettle wall) and the cross rods (the length of the cross rods of the "out"-shaped kneading claws is less than the distance between two adjacent kneading claws) further improve the processing capacity of the kneading claws for high-viscosity materials, can effectively break the viscous resistance of high-viscosity materials, and ensure that ethylene glycol can still be efficiently discharged from the melt under high viscosity conditions.

[0024] 3. The dead zone volume of the present invention is small; the special structural design of the kneading claws reduces the dead zone volume in the reactor, avoids the occurrence of side reactions such as high-temperature oxidation and etherification of PEN polyester, and can obtain a high molecular weight PEN product with uniform performance.

[0025] 4. The present invention promotes efficient discharge of ethylene glycol; the left kettle cover is provided with upper and lower holes, the upper hole is used to introduce nitrogen, the lower hole is used to monitor the melt temperature, and a gas phase outlet is provided on the side of the feed port. This design can ensure that the ethylene glycol molecules that escape from the PEN melt to the gas phase can be promptly taken out of the kettle by the nitrogen flow, further promoting the mass transfer process. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 It is a stereoscopic diagram of a uniaxial horizontal reactor for final polycondensation of polyethylene naphthalate according to the present invention;

[0027] Figure 2 It is a front view of the reaction kettle of the present invention;

[0028] Figure 3 It is a left view of the reaction kettle of the present invention;

[0029] Figure 4 This is a front view of the stirring paddle of the reactor of the present invention;

[0030] Figure 5 It is a front view of the reactor wall and kneading claws of the present invention;

[0031] Figure 6 It is a left view of the reactor wall and kneading claws of the present invention;

[0032] Figure 7 Schematic diagram of the kneading of the stirring paddle and kneading claws of the reactor of the present invention.

[0033] In the figure, 1 is the stirring paddle; 2 is the kneading claw; 3 is the kettle wall; 11 is the stirring shaft; 12 is the "out" shaped stirring paddle blade; 13 is the vertical rod close to the stirring shaft; 14 is the vertical rod far from the stirring shaft; 15 is the cross bar of the stirring paddle blade; 21 is the "out" shaped kneading claw; 22 is the "semi-out character" shaped kneading claw; 23 is the vertical rod close to the kettle wall; 24 is the vertical rod far from the kettle wall; 25 is the cross bar of the kneading claw; 31 is the left kettle cover; 32 is the right kettle cover; 33 is the feeding port; 34 is the gas-phase discharge port; 35 is the nitrogen hole; 36 is the monitoring hole for the melt temperature inside the kettle. Specific embodiments

[0034] Next, the relevant technologies in the present invention will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without making creative efforts belong to the scope of protection of the present invention.

[0035] Refer to Figures 1 to 7 As shown, a single-shaft horizontal reactor for the final polycondensation of polyethylene naphthalate in the present embodiment mainly consists of a stirring paddle 1, a kneading claw 2, a kettle wall 3, a left kettle cover 31, a right kettle cover 32 and a feeding port 33.

[0036] The "out" shaped stirring paddle blades 12 are evenly distributed on the stirring shaft 11 of the stirring paddle 1. A single set of stirring paddles 1 consists of four "out" shaped stirring paddle blades 12 evenly distributed along the axis on the stirring shaft 11. This distribution method helps to form a relatively uniform stirring field inside the reactor. The axial distribution angle between two adjacent sets of "out" shaped stirring paddle blades 12 in the radial direction is 30 - 60°, and the preferred angle is 45°. This angle setting can make the material continuously change the flow direction during the stirring process and enhance the stirring effect. A single set of stirring paddles 1 is located on the same rotation plane distributed in the radial direction. Two sets of vertical rods are arranged in the "out" shaped stirring paddle blade 12, namely the vertical rod 13 close to the stirring shaft and the vertical rod 14 far from the stirring shaft. The length of the vertical rod 13 close to the stirring shaft is 1 / 4 - 3 / 4 of the length of the vertical rod 14 far from the stirring shaft, and the preferred length is 1 / 2.

[0037] The kneading claws 3 are in the shape of "out" or "semi-out character" and are evenly distributed on the inner wall of the kettle. This special-shaped kneading claw 3 can cooperate better with the stirring paddle 1 to effectively knead the material. Two sets of vertical rods are arranged on the kneading claw 3, namely the vertical rod 23 close to the kettle wall and the vertical rod 24 far from the kettle wall. The length of the vertical rod 23 close to the kettle wall is 1 / 2 of the length of the vertical rod 24 far from the kettle wall.

[0038] The kneading claws 3 and the stirring paddle 1 are kneaded and distributed, the length of the stirring paddle cross bar 15 of the "out"-shaped stirring paddle 12 is less than the distance between two adjacent groups of "out"-shaped stirring paddles 12, and the length of the kneading claw cross bar 25 of the "out"-shaped kneading claw 21 is less than the distance between two adjacent kneading claws 2. This size relationship ensures that the stirring paddle 1 and the kneading claw 2 can cooperate with each other without interfering with each other during the working process, thereby ensuring the normal kneading and stirring process of the materials in the reactor.

[0039] The kettle wall 3 is a hollow cylinder connected to the left and right sides, and the kneading claws 2 are welded and distributed on the inner wall to ensure that the kneading of the materials can be effectively carried out in cooperation with the stirring paddle 1.

[0040] The left kettle cover 31 is sealed with the left end of the cylinder of the kettle wall 3 by a flange. The left kettle cover 31 has two upper and lower holes vertically distributed along the central axis. The upper hole is used to introduce nitrogen, which is the nitrogen hole 35. The introduction of nitrogen can protect the reaction system and adjust the reaction atmosphere. The lower hole is used to monitor the melt temperature in the kettle, which is the melt temperature monitoring hole 36 in the kettle to ensure the smooth progress of the reaction. The right kettle cover 32 is sealed with the right end of the cylinder of the kettle wall 3 by a flange, which also plays the role of sealing the reactor.

[0041] The feed port 33 is connected to the interior of the kettle body and the kettle cover is sealed with a flange. An opening is arranged on the side of the feed port 33 for discharging gaseous substances such as nitrogen, namely, a gas phase discharge port 34.

[0042] The uniaxial horizontal reactor of this specific embodiment is suitable for the final polycondensation process of PEN resin. The transesterification polymerization of PEN can be divided into three stages: transesterification, pre-polycondensation and final polycondensation. The viscosity of the material in the transesterification stage is relatively low, and it is usually completed in a vertical reactor. In the pre-polycondensation stage, a prepolymer with a molecular weight of 1000 to 5000 g / mol is usually synthesized. The viscosity of the material is relatively low, about 0.1 to 10 Pa·s, and it can be completed in a vertical reactor. With the increase of the degree of polymerization, the viscosity of the PEN melt rises sharply, and the mass transfer area of ​​the vertical reactor is small, making it difficult to effectively remove the ethylene glycol molecules in the system. The horizontal reactor of this specific embodiment is dedicated to the final polycondensation process of PEN. Specifically, the pre-polycondensation product is used as a raw material, and the polycondensation reaction is further carried out under high temperature and high vacuum conditions through the special kneading action of the horizontal reactor, and finally a high molecular weight PEN product with a degree of polymerization of 20,000 to 60,000 g / mol is obtained.

[0043] Example

[0044] Reactor processing and manufacturing

[0045] The stirring shaft 11 of the stirring paddle 1 is made of high-strength alloy steel. During the manufacturing process, the diameter tolerance of the shaft is ensured to be controlled within ±0.1 mm.

[0046] The "out" shaped stirring blade 12 is made of 316L stainless steel. During manufacturing, ensure that the curved surface accuracy of the blade reaches ±0.1mm. For the two groups of vertical rods in the blade, welding is used to connect them during the manufacturing process. The length of the vertical rod 13 close to the stirring shaft is 1 / 2 of the vertical rod 14 away from the stirring shaft. Its length tolerance is controlled within ±0.5mm. The "out" shaped stirring blade 12 is evenly welded to the stirring shaft 11, and the angle between two adjacent groups of "out" shaped stirring blades 12 along the axial distribution is 45°. The accuracy of the angle is ensured to be within ±2° through precise fixture positioning.

[0047] The kneading claws 3 are made of 316L stainless steel and welded to the inner wall of the reactor. The kneading claws 3 are installed at a specific position inside the reactor and are staggered with the stirring paddles 1. The two sets of vertical rods arranged for the kneading claws 3 have a length of the vertical rod 23 close to the reactor wall that is 1 / 2 of the length of the vertical rod 24 away from the reactor wall. The length tolerance is controlled within ±0.5mm. When the kneading claws 3 are welded and installed, the position accuracy of the kneading claws 3 is ensured to be within ±0.1mm to ensure the kneading effect with the stirring paddle 1.

[0048] The reactor wall 3 is a hollow cylinder connected to the left and right, and is made of a double-layer stainless steel structure. The outer stainless steel layer mainly plays a supporting and protective role, and the inner stainless steel layer is in direct contact with the reaction material, and is made of 316L stainless steel. The inner wall is welded with distributed kneading claws 3: including "out"-shaped kneading claws 21 and "half-out"-shaped kneading claws 22. The "out"-shaped kneading claws 21 are located in the middle of the hollow cylinder of the reactor wall 3, and the "half-out"-shaped kneading claws 22 are respectively located at the two ends of the hollow cylinder of the reactor wall 3.

[0049] The left kettle cover 31 has two holes vertically distributed along the central axis. The nitrogen hole 35 is used to introduce nitrogen, and its hole diameter is 6.35 mm. The hole diameter of the melt temperature monitoring hole 36 in the kettle is 12.7 mm, and a thermocouple is inserted for temperature monitoring. When installing the left kettle cover 31, a metal-wrapped graphite high-temperature resistant sealing gasket is used, and the kettle cover is tightly connected to the kettle wall 3 by bolts. The processing and sealing methods of the right kettle cover 32 are similar to those of the left kettle cover 31.

[0050] The feed port 33 is connected to the interior of the kettle body, and the pipe diameter is 5 cm. The kettle cover is sealed with a flange, and a gas phase discharge port 34 is arranged on the side of the feed port 33. The diameter of the gas phase discharge port 34 is 6.35 mm, which is used to discharge gas phase substances such as nitrogen and ethylene glycol.

[0051] PEN final polycondensation

[0052] Slowly add a certain amount of PEN oligomer into the kettle through the feed port 33, and introduce nitrogen to replace the air in the kettle. Raise the temperature to 280°C, control the system pressure to 100 Pa, and control the nitrogen inlet rate to 100 ml / min. Turn on the stirring and adjust the speed to 50 rpm. Under this condition, react for 30 minutes, open the kettle cover while hot, take out the PEN product, and the reaction is over.

[0053] In order to evaluate the devolatilization efficiency of the horizontal reactor, the reaction conditions were kept constant and only the reactor structure was adjusted to compare the changes in the intrinsic viscosity of the PEN prepolymer after polycondensation in reactors with different structures. The number average molecular weight of the oligomer and product was characterized by an Ubbelohde viscometer.

[0054] Example 1

[0055] The angle between two adjacent groups of "out" shaped stirring blades 12 of the horizontal single-axis reactor is 45 degrees. Two groups of vertical rods are arranged in the "out" shaped stirring blades 12, and the length of the vertical rod 13 close to the stirring shaft is 1 / 2 of the vertical rod 14 away from the stirring shaft.

[0056] 1 kg of PEN oligomer with an intrinsic viscosity of 0.48 dL / g was added into the kettle, and the air was replaced by nitrogen. The reaction was carried out for 30 minutes at 280°C, 100 Pa, a nitrogen flow rate of 100 ml / min, and a rotation speed of 50 rpm. The product was discharged while hot to obtain the PEN product, and the intrinsic viscosity was tested.

[0057] Example 2

[0058] The angle between two adjacent groups of "out" shaped stirring blades 12 of the horizontal single-axis reactor is 30 degrees. Two groups of vertical rods are arranged in the "out" shaped stirring blades 12, and the length of the vertical rod 13 close to the stirring shaft is 1 / 2 of the vertical rod 14 away from the stirring shaft.

[0059] The PEN polycondensation process and the product intrinsic viscosity test method are the same as those in Example 1.

[0060] Example 3

[0061] The angle between two adjacent groups of "out" shaped stirring blades 12 of the horizontal single-axis reactor is 60 degrees. Two groups of vertical rods are arranged in the "out" shaped stirring blades 12, and the length of the vertical rod 13 close to the stirring shaft is 1 / 2 of the vertical rod 14 away from the stirring shaft.

[0062] The PEN polycondensation process and the product intrinsic viscosity test method are the same as those in Example 1.

[0063] Example 4

[0064] The angle between two adjacent groups of "out" shaped stirring blades 12 of the horizontal single-axis reactor is 45 degrees. Two groups of vertical rods are arranged in the "out" shaped stirring blades 12, and the length of the vertical rod 13 close to the stirring shaft is 3 / 4 of the length of the vertical rod 14 away from the stirring shaft.

[0065] The PEN polycondensation process and the product intrinsic viscosity test method are the same as those in Example 1.

[0066] Example 5

[0067] The angle between two adjacent groups of "out" shaped stirring blades 12 of the horizontal single-axis reactor is 45 degrees. Two groups of vertical rods are arranged in the "out" shaped stirring blades 12, and the length of the vertical rod 13 close to the stirring shaft is 1 / 4 of the length of the vertical rod 14 away from the stirring shaft.

[0068] The PEN polycondensation process and the product intrinsic viscosity test method are the same as those in Example 1. Table 1 is a comparative table of intrinsic viscosities of PEN products obtained in the examples.

[0069]

[0070] According to Examples 1 to 5, the uniaxial horizontal reactor of the present invention is suitable for the final polycondensation process of PEN, and can obtain a PEN resin with an intrinsic viscosity of 0.90 to 1.05 dL / g, which meets the requirements of most application scenarios for PEN resin.

[0071] The uniaxial horizontal reactor of the present embodiment adopts an "out"-shaped stirring paddle 1, and an "out"-shaped or "half-out"-shaped kneading claw 2 is arranged on the reactor wall. The special kneading action of the two can effectively increase the surface area renewal rate of the PEN melt during the final polycondensation process, so that ethylene glycol can be quickly discharged from the system, promote the forward movement of the polymerization reaction equilibrium, accelerate the reaction rate, and obtain a high intrinsic viscosity PEN resin, which has great application value in the field of polymer material synthesis equipment technology.

[0072] In summary, the present invention makes the kneading efficiency of the material in the reactor higher through the special shape of the stirring blade and the specific angle between the stirring blade and the stirring shaft, as well as the special shape and unique distribution of the kneading claws. This sufficient kneading action increases the mass transfer area, making the interfacial mass transfer of ethylene glycol molecules more effective. Increasing the mass transfer area helps the reaction equilibrium to move forward, which is beneficial to the synthesis of high molecular weight polyethylene naphthalate (PEN) products.

[0073] It should be emphasized that the above are only preferred embodiments of the present invention and do not limit the present invention in any form. Any simple modifications, equivalent changes and modifications made to the above embodiments based on the technical essence of the present invention are still within the scope of the technical solution of the present invention.

Claims

1. A uniaxial horizontal reactor for final polycondensation of polyethylene naphthalate, comprising: A stirring blade (1), a kettle wall (3), a left kettle cover (31), a right kettle cover (32), and a feeding port (33), wherein the kettle wall (3) is cylindrical, and the left kettle cover (31) and the right kettle cover (32) are covered on the kettle wall (3) from both ends of the cylinder of the kettle wall (3), characterized in that: The stirring paddle (1) comprises a stirring shaft (11), the stirring shaft (11) extending axially from one end of the kettle wall (3) into the kettle wall (3), and a stirring blade (12) extending radially outwardly in the shape of an "out" is provided on a cylindrical surface of the stirring shaft (11) located inside the kettle wall (3); a stirring blade cross bar (15) is provided on the "out"-shaped stirring blade (12), the stirring blade cross bar (15) extending axially toward both ends from a connection point of the "out"-shaped stirring blade (12), and vertical bars extending radially inwardly are provided at both ends of the stirring blade cross bar (15); A kneading claw (2) is provided on the cylindrical inner wall of the kettle wall (3), and the kneading claw (2) comprises an "out"-shaped kneading claw (21) extending radially inward from the inner wall of the kettle wall (3); a kneading claw cross bar (25) is provided on the "out"-shaped kneading claw (21), and the kneading claw cross bar (25) extends axially toward both ends from the connection of the "out"-shaped kneading claw (21), and vertical bars extending radially outward are provided at both ends of the kneading claw cross bar (25); The "out"-shaped stirring blades (12) are arranged alternately with the "out"-shaped kneading claws (21) along the axial direction; the vertical rods of the "out"-shaped stirring blades (12) extend radially inwards into the inner side of the vertical rods of the adjacent "out"-shaped kneading claws (21); and the vertical rods of the "out"-shaped kneading claws (21) extend radially outwards into the inner side of the vertical rods of the adjacent "out"-shaped stirring blades (12); When the stirring paddle (1) rotates in the kettle wall (3), the "out"-shaped stirring paddle (12) and the "out"-shaped kneading claw (21) rotate and knead with each other in the kettle wall (3); The kneading claw (2) further comprises a "half-out" type kneading claw (22) extending radially inward from the inner wall of the kettle wall (3); the "half-out" type kneading claw (22) is arranged at both ends of the cylinder of the kettle wall (3); a kneading claw cross bar of the "half-out" type kneading claw (22) is arranged unilaterally along the axial direction; the kneading claw cross bar of the "half-out" type kneading claw (22) extends from the outside to the inside of the cylinder of the kettle wall (3).

2. A uniaxial horizontal reactor for final polycondensation of polyethylene naphthalate according to claim 1, characterized in that: The stirring blade cross bar (15) is provided with multiple layers along the radial direction on the "out"-shaped stirring blade (12); and the kneading claw cross bar (25) is provided with multiple layers along the radial direction on the "out"-shaped kneading claw (21).

3. A uniaxial horizontal reactor for final polycondensation of polyethylene naphthalate according to claim 2, characterized in that: In two radially adjacent stirring blade cross bars (15), the length of the vertical bar (13) close to the stirring shaft is one quarter to three quarters of the length of the vertical bar (14) away from the stirring shaft: In the two radially adjacent kneading claw cross bars (25), the length of the vertical bar (24) away from the kettle wall is one quarter to three quarters of the length of the vertical bar (23) close to the kettle wall.

4. A uniaxial horizontal reactor for final polycondensation of polyethylene naphthalate according to claim 1, characterized in that: The "out"-shaped stirring blades (12) are provided in plurality, and the plurality of the "out"-shaped stirring blades (12) are arranged around the stirring shaft (11); the "out"-shaped kneading claws (21) are provided in plurality, and the plurality of the "out"-shaped kneading claws (21) are arranged around the cylindrical inner wall of the kettle wall (3).

5. A uniaxial horizontal reactor for final polycondensation of polyethylene naphthalate according to claim 4, characterized in that: The "out"-shaped stirring blades (12) are provided in a number of 2 to 12, and the "out"-shaped stirring blades (12) are evenly distributed around the stirring shaft (11); the "out"-shaped kneading claws (21) are provided in a number of 2 to 6, and the "out"-shaped kneading claws (21) are evenly distributed around the cylindrical inner wall of the kettle wall (3).

6. A uniaxial horizontal reactor for final polycondensation of polyethylene naphthalate according to claim 1, characterized in that: A plurality of "out"-shaped stirring blades (12) are provided, and the plurality of "out"-shaped stirring blades (12) are arranged along the axial direction of the stirring shaft (11).

7. The uniaxial horizontal reactor for final polycondensation of polyethylene naphthalate according to claim 1, characterized in that: The feed port (33) is provided with a gas phase discharge port (34); the left kettle cover (31) or the right kettle cover (32) is provided with a nitrogen hole (35) and a melt temperature monitoring hole (36) in the kettle.

8. The uniaxial horizontal reactor for final polycondensation of polyethylene naphthalate according to claim 1, characterized in that: The left kettle cover (31) and the right kettle cover (32) are respectively sealed with the kettle wall (3) via flanges.

9. The uniaxial horizontal reactor for final polycondensation of polyethylene naphthalate according to claim 1, characterized in that: The stirring paddle (1), the kneading claws (2), the kettle wall (3) and the stirring shaft (11) rotate on the same axis, and the two ends of the stirring shaft (11) are rotatably connected to the left kettle cover (31) and the right kettle cover (32) respectively.

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