Method and system for high-pressure reaction above 40MPa

Abstract

The invention discloses a method and a system for high-pressure polymerization reaction above 40MPa. The method provided by the invention comprises the following steps: arranging a first magnetic coupling piece in a first accommodating cavity, arranging a second magnetic coupling piece outside the first accommodating cavity, and arranging a stirring paddle in a second accommodating cavity; the first magnetic coupling piece is connected with the stirring paddle in the second containing cavity and drives the stirring paddle to rotate; controlling the pressure of the first accommodating cavity to be greater than or equal to 40MPa and the temperature to be less than or equal to 200 DEG C; reaction materials are introduced into the first accommodating cavity or the second accommodating cavity; the material pressure in the second containing cavity is larger than or equal to 40 MPa, and the reaction is carried out under the condition that the temperature is smaller than or equal to 800 DEG C. The invention also provides a high-pressure reaction device. The magnetic coupling technology is applied to the high-pressure and high-temperature reaction of 40 MPa or above, and operation and maintenance are easy.

Description

Technical Field

[0001] The present invention relates to the field of high-pressure and high-temperature reactions, and more particularly to a method and system for high-pressure reactions above 40 MPa. Background Art

[0002] During high-pressure, high-temperature reactions, the reactor temperature and pressure are very high. Typical high-temperature, high-pressure reactions include submarine thermochemical reactions, underground thermochemical reactions, high-pressure ethylene homopolymerization, and high-pressure ethylene and vinyl acetate copolymerization.

[0003] It is well known in the art that continuous reactions typically require high stirring speeds to achieve good mixing of materials within the reactor, which can easily damage moving parts of the stirred tank, typically seals. In particular, seals in stirred tank reactors are particularly susceptible to damage under high-pressure and high-temperature reaction conditions, leading to high maintenance costs.

[0004] In order to ensure the smooth and safe operation of the continuous reaction process under the harsh conditions of high temperature and high pressure, a more wear-resistant sealing material can be used for dynamic sealing or the drive motor can be built into the reactor. Typically, in industry, a reactor with a built-in motor is used, that is, the drive motor is placed inside the reactor. Since the motor is in direct contact with the reaction materials, in industrial practice, the device often stops due to motor failure. In the laboratory, dynamic sealing can be used to deal with the problem of stirring, but as the stirring speed increases, the life of the dynamic sealing material is very short. In addition, the frequent failure of the dynamic sealing structure leads to the inevitable leakage of reaction materials in the continuous reaction process, which poses a great safety risk. Summary of the Invention

[0005] The purpose of the present invention is to address the problems of short seal life and difficult maintenance in high-temperature reactions under high-pressure and ultra-high-pressure conditions. A method and system for high-pressure polymerization reactions above 40 MPa are proposed. By adopting magnetic coupling technology, the operating cycle of the high-pressure reaction device is improved.

[0006] The present invention solves the technical problem by adopting the following technical solutions:

[0007] The present invention first provides a method for high-pressure polymerization reaction above 40 MPa, the proposed method comprising the following steps:

[0008] 1) A first magnetic coupling member is disposed within the first cavity, a second magnetic coupling member is disposed outside the first cavity, and a stirring paddle is disposed in the second cavity; a sealing member having a central opening is disposed between the first cavity and the second cavity, and a stirring shaft is disposed in the central opening; the first magnetic coupling member is connected to the stirring paddle in the second cavity via the stirring shaft, driving the stirring paddle to rotate;

[0009] 2) According to the requirements of the polymerization process, all the polymerization reaction materials are directly introduced into the second cavity; or part of the polymerization reaction materials are directly introduced into the second cavity, and the other part is first introduced into the first cavity and then into the second cavity through the first cavity;

[0010] 3) controlling the pressure of the first chamber to be 40 MPa to 400 MPa and the temperature to be less than or equal to 200° C.; and controlling the pressure of the material in the second chamber to be 40 MPa to 400 MPa and the temperature to be less than or equal to 800° C. to carry out the reaction;

[0011] The pressure of the first chamber is 0.001 to 10 MPa higher than the pressure of the second chamber;

[0012] The high-pressure polymerization reaction is a continuous polymerization. During the polymerization process, the ratio of the pressure pulse amplitude to the average pressure in the second chamber is 0.0025 to 0.15, preferably 0.01 to 0.12.

[0013] In one embodiment of the present invention, the first cavity is provided with a first heat exchange structure to control the maximum temperature of the first cavity to be less than or equal to 200°C, preferably less than or equal to 150°C. The second cavity is provided with a second heat exchange structure to control the temperature of the second cavity to be 800°C or less, preferably 600°C or less, and more preferably 400°C or less.

[0014] In one embodiment of the present invention, the temperature of the first cavity is controlled by the first material and / or the temperature of the first cavity is controlled by the heat exchange structure provided in the first cavity. The temperature of the first cavity is less than or equal to 200°C, preferably less than or equal to 150°C.

[0015] In one embodiment of the present invention, the second cavity is provided with at least one temperature measurement opening and at least one feed port, and the feed port is used to introduce the polymerization reaction material into the second cavity.

[0016] In one embodiment of the present invention, when the polymerization reaction material in step 2) is fed in two parts, the first material enters the first cavity, enters the second cavity via the first cavity, and the second material directly enters the second cavity. The first material and the second material may contain the same components or different components. The temperature of the first material when entering the first cavity is less than or equal to 200°C.

[0017] In one embodiment of the present invention, when the polymerization reaction material is fed in two parts in step 2), the first material enters the second cavity through the gap between the stirring shaft and the sealing member; or the stirring shaft is a hollow structure, and the first material enters the second cavity through the hollow structure of the stirring shaft.

[0018] In one embodiment of the present invention, the second magnetic coupling member drives the first magnetic coupling member to rotate, and the first magnetic coupling member drives the stirring paddle to rotate, and the stirring speed of the stirring paddle is 10 to 3000 rpm, preferably 100 to 2000 rpm.

[0019] In one embodiment of the present invention, the second cavity is provided with at least one pressure measurement opening, and the second cavity is installed with at least one pressure relief structure, and the pressure relief structure is one or a combination of a bursting disc or a safety valve.

[0020] In one embodiment of the present invention, the second cavity is provided with at least one discharge port, and the reaction material enters the third cavity after being decompressed through the discharge port. The pressure of the third cavity is 0.1MPa to 40MPa, and the temperature of the third cavity is 0°C to 300°C.

[0021] The present invention also provides a high-pressure polymerization system for above 40 MPa, comprising:

[0022] A high-pressure feed pump for compressing the polymerization reaction material to a set pressure, a heat exchanger for changing the temperature of the polymerization reaction material, and a high-pressure reaction device;

[0023] The high-pressure reaction device comprises at least a first chamber, a second chamber, a third chamber, a stirring paddle, a first magnetic coupling member and a second magnetic coupling member; wherein the first chamber and the second chamber are both provided with a feed port;

[0024] The first magnetic coupling member is disposed inside the first cavity, and the second magnetic coupling member is disposed outside the first cavity. A sealing member with a central opening is disposed between the first cavity and the second cavity, and a stirring shaft is disposed in the central opening. The material in the first cavity can enter the second cavity through a gap between the sealing member and the stirring shaft or a hollow structure of the stirring shaft (in this embodiment, the stirring shaft has a hollow structure, the upper end of the hollow structure is connected to the first cavity, and the lower end is connected to the second cavity);

[0025] The first magnetic coupling member is an annular structure, the first magnetic coupling member is connected to the stirring paddle via the stirring shaft, and the central axes of the first magnetic coupling member, the stirring shaft, and the stirring paddle are on the same straight line;

[0026] The second magnetic coupling member is an annular structure, and the central axes of the second magnetic coupling member and the first magnetic coupling member are on the same straight line;

[0027] The second chamber is connected to the third chamber via a first pressure reducing valve.

[0028] In one embodiment of the present invention, the second cavity is preferably a cylindrical cavity with a height-to-diameter ratio of 2:1 to 1:20. The height-to-diameter ratio of the second cavity is the ratio of the internal height of the second cavity to the internal diameter of the second cavity. Preferably, the length-to-diameter ratio of the second cavity is 1:1 to 1:10. The inner diameter of the second cavity is 0.005m to 0.4m, preferably 0.01m to 0.2m.

[0029] In one embodiment of the present invention, the second coupling member comprises a structure including a permanent magnet and is connected to the motor via gears or belts; or the second coupling member comprises a structure including a coil and generates an alternating magnetic field via an alternating electric field. Preferably, in environments requiring high explosion-proof performance, the second coupling member comprises a structure including a permanent magnet.

[0030] In one embodiment of the present invention, the first coupling member is a combined structure including a permanent magnet, and the first coupling member and the stirring paddle are connected by either a direct connection or a reducer connection.

[0031] In one embodiment of the present invention, the second chamber and the third chamber are further provided with bursting discs and / or safety valves, which can quickly reduce the pressure of the reaction system.

[0032] Compared with the existing technology, the present invention has the following advantages:

[0033] 1. The present invention proposes a high-pressure polymerization reaction system comprising a high-pressure feed pump, a heat exchanger and a magnetic coupling stirrer. The test process is a continuous reaction. The test pressure of the high-pressure reaction device is 40MPa to 400MPa, the temperature can reach up to 800°C, and the process operation range is wide.

[0034] 2. During the polymerization process of the present invention, the ratio of the pressure pulse amplitude to the average pressure in the second cavity can be controlled to be 0.0025 to 0.15. On the one hand, the material flow rate in the first cavity and the second cavity fluctuates, which can improve the flushing effect of the reaction material on the wall surface and reduce the problems of poor wall heat transfer effect, difficult to control reaction conditions, and easy decomposition accidents of the reaction material caused by wall scaling; on the other hand, it avoids the problem of excessive pressure fluctuations in the first cavity and the second cavity causing the life of the first cavity and the second cavity to be shortened under the action of alternating loads.

[0035] 3. The proposed method avoids the high maintenance costs and short operating cycles of traditional dynamic seals and motor-internal seals. The present invention is particularly suitable for low-viscosity reaction systems and can more effectively guide the research and application of low-viscosity reaction processes under high-pressure and high-temperature conditions. BRIEF DESCRIPTION OF THE DRAWINGS

[0036] Figure 1 Schematic diagram of a high-pressure reaction device in one embodiment of the present invention. DETAILED DESCRIPTION

[0037] The following is a detailed description of an embodiment of the present invention. This embodiment is implemented based on the technical solution of the present invention, and provides a detailed implementation method and specific operation process. However, the protection scope of the present invention is not limited to the following embodiment.

[0038] like Figure 1 Figure 1 shows a schematic diagram of a high-pressure reaction system in one embodiment, comprising feed pumps 1a / 1b, heat exchangers 2a / 2b, first shut-off valves 3a / 3b, a first chamber 4, a second chamber 5, a first magnetic coupling 6a, a second magnetic coupling 6b, a first pressure-reducing valve 7, a third chamber 8, second and third pressure-reducing valves 9 and 10, and a safety valve 11. Feed pump 1a is connected to the inlet of heat exchanger 2a, and the reactants at the outlet of heat exchanger 2a enter the first chamber 4 through the first shut-off valve 3a. Feed pump 1b is connected to the inlet of heat exchanger 2b, and the reactants at the outlet of heat exchanger 2b enter the second chamber 5 through the first shut-off valve 3b. Both the first chamber 4 and the second chamber 5 are equipped with heat exchange structures to control the temperature of the first chamber 4 to ≤200°C and the temperature of the second chamber to a range of values, such as 100°C, 200°C, 400°C, 600°C, and 800°C. The heat exchange structures can be either thermal oil or water-cooled.

[0039] A first magnetic coupling member 6a is disposed within the first chamber 4, and a second magnetic coupling member 6b is disposed outside the first chamber 4. Both the first magnetic coupling member 6a and the second magnetic coupling member 6b are cylindrical structures composed of permanent magnets. A stirring paddle is disposed in the second chamber 5 and is directly connected to the first magnetic coupling member 6a in the first chamber 4. A motor is used to directly drive the second magnetic coupling member to rotate, further driving the rotation of the first magnetic coupling member. In some embodiments, various types of stirring paddles can be used in the second chamber 5, such as a turbine paddle, a ribbon paddle, a propeller paddle, etc.

[0040] Preferably, the first chamber 4 and the second chamber 5 are arranged in an upper and lower position, that is, the first chamber 4 is located above the first chamber 5, and a seal with a central opening is provided between the first chamber and the second chamber, and a stirring shaft is provided in the central opening, so that the material in the first chamber can enter the second chamber. The material entering the first chamber can be used to cool the magnetic coupling in the first chamber to prevent the magnetic coupling from being too hot and causing a decrease in magnetism. It should be noted that the pressure in the first chamber is 40MPa to 400MPa, and the temperature is less than or equal to 200°C; the pressure of the material in the second chamber is 40MPa to 400MPa, and the reaction is carried out at a temperature less than or equal to 800°C; and the pressure in the first chamber is 0.001 to 10MPa higher than the pressure in the second chamber. In the pressure polymerization reaction of the present invention, which is a continuous polymerization, the ratio of the pressure pulse amplitude to the pressure average value in the second chamber during the polymerization process is 0.0025 to 0.15, preferably 0.01 to 0.12.

[0041] The present invention can select the feeding method of materials according to the needs of the polymerization reaction process. For example, all the polymerization reaction materials can be directly introduced into the second cavity; or part of the polymerization reaction materials can be directly introduced into the second cavity, and the other part is first introduced into the first cavity, and then enters the second cavity through the first cavity. These two feeding methods can be switched during the same polymerization reaction process. Among them, when feeding in two parts, the two parts of materials can contain the same components or different components.

[0042] In an optional embodiment of the present invention, there is a gap between the seal and the agitator shaft, and the material in the first chamber enters the second chamber through the gap. In another optional embodiment of the present invention, the agitator shaft has a hollow structure, the upper end of the hollow structure is connected to the first chamber, and the lower end is connected to the second chamber; the material in the first chamber enters the second chamber through the hollow structure. In another optional embodiment of the present invention, there is a gap between the seal and the agitator shaft, and the agitator shaft has the hollow structure of the aforementioned embodiment, and the material in the first chamber enters the second chamber through the gap and the hollow structure. In a typical, but non-limiting, embodiment, the apparatus of the present invention is used to produce polyethylene products. Ethylene, or a mixture of ethylene and propylene, enters the first chamber via feed pump 1a and its subsequent pipelines, and ethylene, organic peroxide, and / or solvent, etc., enter the second chamber via feed pump 1b and its subsequent pipelines. Free radical polymerization is carried out in the second chamber, and the polymerization pressure reaches as high as 100-300 MPa and the temperature reaches 150-320°C, which is a high-pressure and high-temperature reaction process. In the embodiments, the apparatus of the present invention is used to produce polyethylene products.

[0043] The reaction product in the second chamber 5 enters the third chamber 8 through the first pressure reducing valve 7. The third chamber 8 separates the product and collects the polyethylene product. In a typical but non-limiting embodiment, the third chamber 8 is provided with a second pressure reducing valve 9 as a valve for gas phase discharge, and a third pressure reducing valve 10 as a valve for liquid and solid phase discharge, wherein the polyethylene product is located in the liquid and solid phase discharge materials.

[0044] Example 1

[0045] The technical parameters of the high-pressure reaction test device in this embodiment are as follows: test pressure of the first chamber and the second chamber: 40MPa~400MPa; experimental temperature of the first chamber: 20℃~200℃; test temperature of the second chamber: 30℃~500℃; pressure of the third chamber: 0.1MPa~40MPa; temperature of the third chamber: 0℃~300℃.

[0046] The high-pressure reaction in this embodiment is high-pressure free radical ethylene polymerization, and the test method is as follows:

[0047] use Figure 1 The reaction apparatus described herein prepares an initiator solution (second material) comprising an organic peroxide, TBPEH, and a solvent, isododecane, in a 1:1 mass ratio. Ethylene and propylene are then mixed in a 1000:1 mass ratio to obtain a first material. The second material is then continuously fed into the second chamber via a high-pressure feed pump 1b, a heat exchanger 2b, and a first shut-off valve 3b. The first material is continuously fed into the first chamber via a high-pressure feed pump 1a, a heat exchanger 1b, and a first shut-off valve 3a. The pressure in the second chamber is controlled by adjusting the opening of a first pressure reducing valve 7. When the pressure reaches a set value of 150 MPa, the pressure in the second chamber is 150 MPa, the pressure in the first chamber is 0.01 MPa higher than the pressure in the second chamber, and the pressure in the third chamber is 0.2 MPa. The ratio of the pressure pulse amplitude to the average pressure in the second chamber is 0.05.

[0048] Stirring was initiated in the second chamber at 500 rpm, and the heat exchange jacket temperature of the autoclave was maintained at 210°C. The polyethylene product was collected in the third chamber. The apparatus operated for 2000 hours without mechanical failure, and ethylene decomposition occurred twice within 1000 hours.

[0049] Example 2

[0050] This embodiment differs from Example 1 in that the pressure in the second chamber is controlled by controlling the opening of first pressure-reducing valve 7. When the pressure reaches the set value of 250 MPa, the pressure in the second chamber is 250 MPa, and the pressure in the first chamber is 0.1 MPa higher than the pressure in the second chamber. The ratio of the pressure pulse amplitude to the average pressure in the second chamber is 0.03. The device operated for 1800 hours without mechanical failure, and ethylene decomposition occurred three times within 1000 hours.

[0051] Example 3

[0052] The technical parameters of the high-pressure reaction test device in this embodiment are as follows: test pressure of the first chamber and the second chamber: 40MPa~90MPa; experimental temperature of the first chamber: 20℃~200℃; test temperature of the second chamber: 30℃~200℃; pressure of the third chamber: 0.1MPa~5MPa; temperature of the third chamber: 0℃~200℃.

[0053] The high-pressure reaction in this embodiment is the copolymerization of ethylene and vinyl acetate, and the test method is as follows: Figure 1 The reaction apparatus described above prepares an initiator solution (second material) composed of organic peroxide AIBN, vinyl acetate, and methanol in a mass ratio of 1:1000:1000, with ethylene and vinyl acetate serving as the first materials. The second material is then continuously fed into the second chamber via a high-pressure feed pump 1b, a heat exchanger 2b, and a first shut-off valve 3b. The first material is continuously fed into the first chamber via a high-pressure feed pump 1a, a heat exchanger 1a, and a first shut-off valve 3a. The mass flow rate ratio of the first and second materials is 2:1. The pressure in the second chamber is controlled by controlling the opening of the first pressure reducing valve 7. When the pressure reaches the set value of 50 MPa, the pressure in the second chamber is 50 MPa, which is 0.1 MPa higher than the pressure in the second chamber. The ratio of the pressure pulse amplitude to the average pressure in the second chamber is 0.05.

[0054] Stop the high-pressure feed pump 1a. Start stirring in the second chamber at 500 rpm, and maintain the heat exchange jacket temperature of the autoclave at 160°C. Collect the ethylene-vinyl acetate copolymer product in the third chamber. The apparatus operated for 2400 hours without mechanical failure, and ethylene decomposition occurred zero times during the 2400 hours.

[0055] Example 4

[0056] The difference between this embodiment and embodiment 1 is that the ratio of the pressure pulse amplitude to the average pressure in the second chamber is 0.16. The device ran for 1750 hours without mechanical failure, and ethylene decomposition occurred 4 times within 1000 hours.

[0057] Comparative Example 1

[0058] Comparative Example 1 differs from Example 1 in that it lacks a first chamber. All materials are introduced into the second chamber via a high-pressure feed pump 1b. The drive mechanism is an external motor connected to the agitator in the second chamber via a stirring shaft. A traditional dynamic seal ensures a seal between the stirring shaft and the second chamber. The device operated for 200 hours without mechanical failure, and ethylene decomposition occurred eight times within 1000 hours.

[0059] Comparative Example 2

[0060] Comparative Example 2 differs from Example 1 in that the motor in Comparative Example 2 is installed in the first chamber and connected to the agitator in the second chamber via a stirring shaft. The device operated for 900 hours without mechanical failure, and ethylene decomposition occurred five times within 1000 hours.

[0061] The above-described embodiments merely represent several implementation methods of the present invention. While the descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the present invention. It should be noted that a person skilled in the art would be able to make various modifications and improvements without departing from the spirit of the present invention, all of which fall within the scope of protection of the present invention. Therefore, the scope of protection of the present invention shall be determined by the appended claims.

Claims

1. A method for high-pressure polymerization reaction at a pressure of 40 MPa or above, characterized in that: The method comprises the following steps: 1) A first magnetic coupling member is disposed within the first cavity, a second magnetic coupling member is disposed outside the first cavity, and a stirring paddle is disposed in the second cavity; a sealing member having a central opening is disposed between the first cavity and the second cavity, and a stirring shaft is disposed in the central opening; the first magnetic coupling member is connected to the stirring paddle in the second cavity via the stirring shaft, driving the stirring paddle to rotate; 2) According to the requirements of the polymerization process, all the polymerization reaction materials are directly introduced into the second cavity; or part of the polymerization reaction materials are directly introduced into the second cavity, and the other part is first introduced into the first cavity and then into the second cavity through the first cavity; 3) controlling the pressure of the first chamber to be 40 MPa to 400 MPa and the temperature to be less than or equal to 200° C.; and controlling the pressure of the material in the second chamber to be 40 MPa to 400 MPa and the temperature to be less than or equal to 800° C. to carry out the reaction; The pressure of the first chamber is 0.001 to 10 MPa higher than the pressure of the second chamber; The high-pressure polymerization reaction is continuous polymerization, and during the polymerization process, the ratio of the pressure pulse amplitude to the average pressure in the second chamber is 0.0025 to 0.

15.

2. The method according to claim 1, characterized in that Both the first cavity and the second cavity are provided with a heat exchange structure, and the maximum temperature of the first cavity is controlled to be less than or equal to 200°C by the heat exchange structure or the material flow or temperature entering the first cavity; the temperature of the second cavity is controlled to be less than or equal to 800°C by the heat exchange structure.

3. The method according to claim 1, characterized in that The second cavity is provided with at least one temperature measurement opening and at least one feed port, and the feed port is used to introduce polymerization reaction materials into the second cavity.

4. The method according to claim 1, wherein When the polymerization reaction material is fed in two parts in step 2), the first material enters the first cavity, then enters the second cavity via the first cavity, and the second material directly enters the second cavity. The first material and the second material may contain the same components or different components. The temperature of the first material when entering the first cavity is less than or equal to 200° C.; the first material enters the second cavity through the gap between the stirring shaft and the sealing member. Alternatively, the stirring shaft is a hollow structure, and the first material enters the second cavity through the hollow structure of the stirring shaft.

5. The method according to claim 1, characterized in that The second magnetic coupling member drives the first magnetic coupling member to rotate, and the first magnetic coupling member drives the stirring paddle to rotate. The stirring speed of the stirring paddle is 10 to 3000 revolutions per minute, preferably 100 to 2000 revolutions per minute.

6. The method according to claim 1, characterized in that The second chamber is provided with at least one pressure measurement opening, and the second chamber is installed with at least one pressure relief structure, wherein the pressure relief structure is one of a bursting disc and a safety valve or a combination thereof.

7. The method according to claim 1, characterized in that The second cavity is provided with at least one discharge port, and the reaction material enters the third cavity after being decompressed through the discharge port. The pressure of the third cavity is 0.1MPa to 40MPa, and the temperature of the third cavity is 0°C to 300°C.

8. A high-pressure polymerization reaction system of 40 MPa or above for implementing the method according to any one of claims 1 to 7, characterized in that: include: A high-pressure feed pump for compressing the polymerization reaction material to a set pressure, a heat exchanger for changing the temperature of the polymerization reaction material, and a high-pressure reaction device; The high-pressure reaction device comprises at least a first chamber, a second chamber, a third chamber, a stirring paddle, a first magnetic coupling member and a second magnetic coupling member; wherein the first chamber and the second chamber are both provided with a feed port; The first magnetic coupling member is disposed inside the first cavity, and the second magnetic coupling member is disposed outside the first cavity. A sealing member with a central opening is disposed between the first cavity and the second cavity, and a stirring shaft is disposed in the central opening. The material in the first cavity can enter the second cavity through the gap between the sealing member and the stirring shaft or the hollow structure of the stirring shaft. The first magnetic coupling member is an annular structure, and the first magnetic coupling member is connected to the stirring paddle via the stirring shaft, and the central axes of the first magnetic coupling member, the stirring shaft, and the stirring paddle are all on the same straight line; The second magnetic coupling member is an annular structure, and the central axes of the second magnetic coupling member and the first magnetic coupling member are on the same straight line; The second chamber is connected to the third chamber via a first pressure reducing valve.

9. The high-pressure reaction system according to claim 8, characterized in that: The second coupling member is a combination structure including a permanent magnet, and is connected to the motor through gears and belts; or the second coupling member is a combination structure including a coil, which generates an alternating magnetic field through an alternating electric field.

10. The high-pressure reaction system according to claim 8, characterized in that: The first coupling member is a combined structure including a permanent magnet, and the first coupling member and the stirring paddle are connected by a direct connection or a reducer connection.

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