Continuous gas-liquid two-phase or gas-liquid-solid three-phase total conversion reaction system

Abstract

The invention discloses a continuous gas-liquid two-phase or gas-liquid-solid three-phase complete conversion reaction system which comprises a reaction kettle, a reactor, a heat exchanger, a large micro-nano bubble generating device and a small micro-nano bubble generating device, and the reaction kettle is provided with a feeding port, a gas-liquid inlet, a gas-phase outlet and a liquid-phase product outlet. A gas-liquid inlet of the reaction kettle is connected with an outlet of the large micro-nano bubble reaction device, a liquid-phase product outlet of the reaction kettle is connected with an inlet of the heat exchanger and the extraction valve, an outlet of the heat exchanger is connected with an inlet of the large micro-nano bubble reaction device, and an outlet of the extraction valve is connected with an inlet of the small micro-nano bubble generation device. An outlet of the small micro-nano bubble generating device is connected with the bottom end of the reactor, the reactor is provided with a product outlet, and the product outlet is connected with the product valve. According to the invention, continuous chemical reaction can be ensured, gas-liquid-solid three-phase dispersion is uniform, the gas-liquid two-phase reaction conversion rate reaches 100%, a solid catalyst is prevented from entering a circulating pump, and the reaction activity of the catalyst is ensured.

Description

Technical Field

[0001] The invention relates to the field of chemical production, and in particular to a continuous gas-liquid two-phase or gas-liquid-solid three-phase full-conversion reaction system. Background Art

[0002] Gas-liquid-solid three-phase reaction is a common reaction in the chemical industry. There are many types. In most cases, solids are catalysts, and gases and liquids are reactants and products. Back-mixing reactors such as loop reactors have the advantages of good mass transfer effect, large heat exchange area outside the kettle, and good sealing of the device. They are widely used in gas-liquid two-phase reactions. Common loop reactors are composed of reactors, heat exchangers, venturi ejectors, loop circulation pumps and circulation pipelines. The principle is to use high-speed mobile phases to entrain other phases, so that each phase is in close contact, and then evenly dispersed or suspended in the reactor to complete the reaction. When the loop reactor is working, the reaction liquid is sent into the venturi ejector by the circulation pump, and a fast jet flow is formed through the nozzle. The gas in the gas chamber is ejected out, and the liquid hits the tube wall and is fully mixed and reacted. In this area, the fierce turbulence enables the gas and liquid to complete the initial main mass transfer function, and then the gas-liquid two-phase mixture is ejected into the reactor. Secondary mixing and reaction continue in the reactor. It is difficult for a back-mixing reactor to achieve a continuous reaction with full conversion of the reaction product. In addition, the solid catalyst has poor dispersion effect in the reactor, is easily mixed into the circulation pump and easily broken and deactivated under the high shear effect of the circulation pump, which limits the application of gas-liquid-solid three-phase reaction in traditional loop reactors. In addition, fixed bed reactors have disadvantages such as poor gas-liquid mixing effect and poor mass transfer and heat transfer rate, which limits the application of continuous gas-liquid-solid three-phase full conversion reaction. Summary of the invention

[0003] In view of the deficiencies and defects in the prior art, the present invention provides a continuous gas-liquid two-phase or gas-liquid-solid three-phase full conversion reaction system. The reaction system can ensure the continuous progress of the chemical reaction, uniform dispersion of the gas-liquid-solid three-phases, a gas-liquid two-phase reaction conversion rate of 100%, avoid solid catalysts from entering the circulation pump, and ensure the reaction activity of the catalyst.

[0004] To achieve the above object, the technical solution adopted by the present invention is: A continuous gas-liquid two-phase or gas-liquid-solid three-phase full conversion reaction system comprises a reactor, a reactor, a heat exchanger, a large micro-nano bubble generating device and a small micro-nano bubble generating device. A feeding port and a gas-liquid inlet are respectively arranged at the top and the bottom of the reactor. A gas phase outlet and a liquid phase product outlet are arranged between the feeding port and the gas-liquid inlet, and the gas phase outlet is located above the liquid phase product outlet. The gas-liquid inlet of the reactor is connected to the outlet of the large micro-nano bubble reaction device, the liquid phase product outlet of the reactor is connected to the inlet of the heat exchanger and an extraction valve, the outlet of the heat exchanger is connected to the inlet of the large micro-nano bubble reaction device, the outlet of the extraction valve is connected to the inlet of the small micro-nano bubble generating device, the outlet of the small micro-nano bubble generating device is connected to the bottom end of the reactor, a product outlet is arranged at the middle and upper part of the reactor, and the product outlet is connected to the product valve.

[0005] Furthermore, the gas-liquid inlet of the reactor is connected to the outlet end of the first check valve, and the inlet end of the first check valve is connected to the outlet of the raw material inlet valve and the large micro-nano bubble generating device.

[0006] Furthermore, the gas phase outlet of the reactor is connected to the inlet of the second check valve, the top gas phase outlet of the heat exchanger is connected to the inlet of the third check valve, the top gas phase outlet of the reactor is connected to the fourth check valve, and the outlets of the second check valve, the third check valve and the fourth check valve are respectively connected to the gas supply pipeline.

[0007] Furthermore, the large micro-nano bubble generating device includes a circulation pump A, a micro-nano bubble generator A and an air intake pipeline A, and the small micro-nano bubble generating device includes a circulation pump B, a micro-nano bubble generator B and an air intake pipeline B. The air intake pipeline A and the air intake pipeline B are respectively connected to the air circuit valves, and the air circuit valves are connected to the air supply equipment.

[0008] Furthermore, the micro-nano bubble generator A and the micro-nano bubble generator B both include a shell and a generating column installed in the shell, the shell has a gas-liquid inlet and a gas-liquid outlet, the gas-liquid mixture entering from the gas-liquid inlet flows through the generating column and then flows out from the gas-liquid outlet, the generating column includes a plurality of bubble cutting units, a flow channel is provided on the surface of the bubble cutting unit, and a pressure reduction groove is provided between the bubble cutting units.

[0009] Preferably, the flow channel is a spiral flow channel.

[0010] Preferably, the inflow end of the bubble cutting unit is provided with a serrated surface.

[0011] Preferably, a collision platform is provided at the front end of the bubble cutting unit at the gas-liquid inlet end.

[0012] Preferably, the collision platform is a multi-stage frustum, and the collision platform, the bubble cutting unit and the gas-liquid inlet are coaxially arranged.

[0013] Preferably, the shell includes an outer shell and an inner shell, the generating column is arranged in the inner shell cavity, a gas-liquid inlet and a gas-liquid outlet are respectively provided at both ends of the inner shell, an air chamber is provided in the outer shell cavity, the air inlet of the air chamber is arranged on the outer shell, and the air outlet of the air chamber is communicated with the inner shell cavity.

[0014] Preferably, the air inlet of the air chamber is located at the upper middle part of the shell, and the air outlet of the air chamber is located at the gas-liquid outlet.

[0015] Preferably, the gas-liquid inlet comprises a bell-mouth section and a cylindrical section with gradually decreasing volumes, and the diameter of the generating column is larger than the diameter of the cylindrical section but smaller than the maximum diameter of the bell-mouth section.

[0016] Preferably, the gas-liquid outlet is in the shape of a gradually expanding trumpet, and the end of the generating column has a truncated cone section with a gradually increasing diameter, and the diameter of the truncated cone section is smaller than the diameter of the bubble cutting unit.

[0017] Furthermore, a feed valve is provided between the large micro-nano bubble generating device and the reaction kettle.

[0018] Furthermore, the reactor is a tubular reactor, and a jacket for heat exchange is provided on the outside of the reactor.

[0019] Furthermore, during the continuous operation of the reaction system, the feed rate of the feed valve, the output rate of the output valve and the output rate of the product valve should be the same.

[0020] Furthermore, the reaction kettle and the reactor are respectively provided with loaded catalysts inside, and the loaded catalysts are arranged inside the reaction kettle in a vertical, horizontal or spiral manner.

[0021] The beneficial effects of the present invention are as follows: (1) the reaction kettle, the heat exchanger, the large micro-nano bubble reaction device, the small micro-nano bubble reaction device and the reactor are connected to form a circulation loop, which is conducive to gas-liquid two-phase or gas-liquid-solid three-phase reaction. During the reaction, the flow rates of the feed valve, the extraction valve and the product valve are controlled to be the same, so as to realize continuous reaction; (2) the gas and liquid components enter the reaction kettle through the large micro-nano bubble reaction device and enter the reactor through the small micro-nano bubble reaction device. Compared with macro bubbles, the micro-nano bubbles generated by the micro-nano bubble generator have the advantages of large specific surface area, high activity, fast mass transfer rate and long residence time, which can promote uniform dispersion and efficient reaction of gas-liquid two-phase or gas-liquid-solid three-phase; the coupling of the reaction kettle and the reactor can improve the reaction conversion rate; (3) during the gas-liquid-solid three-phase reaction, the catalyst is loaded inside the reaction kettle and the reactor respectively, the solid-phase catalyst is fully in contact with the incoming gas-liquid reactants, the catalytic effect is good, and the catalyst is not easy to enter the circulation pump, so the reaction activity of the catalyst can be guaranteed. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present application. For those skilled in the art, other drawings can be obtained based on these drawings without paying any creative labor.

[0023] Figure 1 It is a structural schematic diagram of the present invention.

[0024] Figure 2 It is a structural schematic diagram of an optimal micro-nano bubble generator.

[0025] Figure 3 yes Figure 2 A partial enlarged view of point A in the middle.

[0026] Figure 4 It is a schematic diagram of the generating column structure.

[0027] Figure 5 It is a schematic diagram of the shell structure.

[0028] Figure 6 This is a comparison chart of mass transfer effects of different bubbles.

[0029] Figure 7 This is a schematic diagram of a full conversion reaction system using an optimized micro-nano bubble generator.

[0030] In the figure: 1 reactor, 11 loaded catalyst, 12 gas-liquid inlet, 13 liquid product outlet, 14 gas outlet, 15 feed port, 21 first check valve, 22 second check valve, 23 third check valve, 24 fourth check valve, 3 feed valve, 41 large micro-nano bubble generator, 411 circulation pump A, 412 micro-nano bubble generator A, 413 air intake pipeline A, 42 small micro-nano bubble generator, 421 circulation pump B, 422 micro-nano bubble generator B, 423 air intake pipeline B, 431 generating column, 4311 bubble cutting unit, 4312 flow channel, 4313 serrated surface, 4314 pressure reducing groove, 4315 collision table, 4316 frustum section, 432 shell, 4321 outer shell, 4322 inner shell, 4323 gas-liquid inlet, 43231 bell mouth section, 43232 cylindrical section, 4324 gas-liquid outlet, 433 gas chamber, 4331 air inlet, 4332 air outlet, 5 production valve, 6 gas path valve, 7 heat exchanger, 71 gas phase outlet, 8 reactor, 81 loaded catalyst, 82 gas phase outlet, 83 feeding port, 9 product valve, 10 gas supply pipeline. DETAILED DESCRIPTION

[0031] In order to make the purpose, technical solution and advantages of the embodiments of the present application clearer, the technical solution in the embodiments of the present application will be clearly and completely described below in conjunction with the drawings in the embodiments of the present application. Obviously, the described embodiments are part of the embodiments of the present application, rather than all the embodiments. The components of the embodiments of the present application described and shown in the drawings here can be arranged and designed in various different configurations.

[0032] In the description of this application, it should also be noted that, unless otherwise clearly specified and limited, the terms "set", "install", "connect", and "connect" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal connection of two components. For ordinary technicians in this field, the specific meanings of the above terms in this application can be understood according to specific circumstances.

[0033] Example 1 A continuous gas-liquid two-phase or gas-liquid-solid three-phase full conversion reaction system of the present invention comprises a reactor 1, a reactor 8, a heat exchanger 7, a large micro-nano bubble generating device 41 and a small micro-nano bubble generating device 42, wherein a feed port 15 and a gas-liquid inlet 12 are respectively provided at the top and the bottom of the reactor 1, a gas phase outlet 14 and a liquid phase product outlet 13 are provided between the feed port 15 and the gas-liquid inlet 12, and the gas phase outlet 14 is located above the liquid phase product outlet 13, the gas-liquid inlet 12 of the reactor 1 is connected to the outlet of the large micro-nano bubble reaction device, the liquid phase product outlet 13 of the reactor 1 is connected to the inlet of the heat exchanger 7 and the extraction valve 5, the outlet of the heat exchanger 7 is connected to the inlet of the large micro-nano bubble reaction device, the outlet of the extraction valve 5 is connected to the inlet of the small micro-nano bubble generating device 42, the outlet of the small micro-nano bubble generating device 42 is connected to the bottom end of the reactor 8, a product outlet is provided at the middle and upper part of the reactor 8, and the product outlet is connected to the product valve 9. The reaction kettle 1 is used in combination with the reactor 8. After the reactants have initially reacted in the reaction kettle 1 and reached the expected conversion rate, the extraction valve 5 is opened and the materials enter the reactor 8 for further reaction. When the conversion is complete, the product valve 9 is opened to discharge the product.

[0034] The gas-liquid inlet 12 of the reactor 1 is connected to the outlet of the first check valve 21, and the inlet of the first check valve 21 is connected to the outlet of the raw material inlet valve and the large micro-nano bubble generator 41. The first check valve 21 ensures that the material flows in one direction at the gas-liquid inlet 12 of the reactor 1 to prevent backflow.

[0035] The gas phase outlet 14 of the reactor 1 is connected to the inlet of the second check valve 22, the top gas phase outlet 71 of the heat exchanger 7 is connected to the inlet of the third check valve 23, the top gas phase outlet 82 of the reactor 8 is connected to the fourth check valve 24, and the outlets of the second check valve 22, the third check valve 23 and the fourth check valve 24 are respectively connected to the gas supply pipeline 10. The gas discharged through the second check valve 22, the third check valve 23 and the fourth check valve 24 enters the large micro-nano bubble generating device 41 or the small micro-nano bubble generating device 42 again through the gas supply pipeline, and then enters the reactor 1 or the reactor 8 to continue the reaction, thereby improving the conversion rate of the gas.

[0036] The large micro-nano bubble generating device 41 includes a circulation pump A411, a micro-nano bubble generator A412 and an air intake pipeline A413, wherein the air intake pipeline A413 is connected to the air circuit valve 6, and the small micro-nano bubble generating device 42 includes a circulation pump B421, a micro-nano bubble generator B422 and an air intake pipeline B423, wherein the air intake pipeline B423 is connected to the air circuit valve 6, and the air circuit valve 6 is connected to the gas supply equipment. The circulation pump A411 and the circulation pump B421 provide power for the micro-nano bubble generator A412, the micro-nano bubble generator B422 and the gas-liquid circulation. The gas supply equipment provides gas raw materials for the reactor 1 and the reactor 8.

[0037] The liquid phase circulation volume of the large micro-nano bubble generator 41 is different from that of the small micro-nano bubble generator 42. The liquid phase circulation volume of the large micro-nano bubble generator 41 is several to dozens of times that of the small micro-nano bubble generator 42. The air intake volume of the large micro-nano bubble generator 41 is the maximum air intake volume that the reaction system can withstand; the air intake volume of the small micro-nano bubble generator 42 is related to the liquid phase circulation volume and the conversion rate set by the extraction valve 5. The higher the conversion rate, the smaller the air intake volume and liquid phase circulation volume of the small micro-nano bubble generator 42.

[0038] A feed valve 3 is provided between the large micro-nano bubble generating device 41 and the reactor 1. The feed valve 3 can add liquid reactants to the reaction system.

[0039] The reactor 8 is a tubular reactor, and a jacket for heat exchange is provided on the outside thereof. A heat exchange fluid is introduced into the jacket to exchange heat with the material in the reactor 8. A feed port 83 is also provided on the top of the reactor 8 for adding material to the reactor 8.

[0040] During the continuous operation of the reaction system, the feed rate of the feed valve 3, the output rate of the output valve 5 and the output rate of the product valve 9 should be the same.

[0041] In addition, the reaction kettle 1 and the reactor 8 should at least be provided with a pressure gauge and a safety valve setting port.

[0042] Example 2 The difference between Example 2 and Example 1 is that: the reactor 1 is provided with a loaded catalyst 11, which is arranged vertically, horizontally or spirally inside the reactor 1. The reactor 8 is provided with a loaded catalyst 81, which is arranged vertically, horizontally or spirally inside the reactor 8. Example 1 is suitable for gas-liquid two-phase reaction, and Example 2 is suitable for gas-liquid-solid three-phase reaction by arranging the loaded catalyst in the reactor 1 and the reactor 8. The use of the loaded catalyst can increase the contact area between the catalyst and the reactant, improve the catalytic efficiency, and at the same time, the catalyst is not easy to enter the circulation pump, thereby ensuring the reaction activity of the catalyst.

[0043] During use of the reaction system of the present invention, the feed valve 3 is opened and / or liquid raw materials are added into the reactor 1 and the heat exchanger 7 through the feed port 15. The liquid level of the liquid raw materials should cover the loaded catalyst 11 in the reactor 1 and leave a part of the gas phase space; the feed valve 3 and the feed port 15 are closed, and the large micro-nano bubble generating device 41 is opened to allow the gas-liquid two-phase or the gas-liquid-solid three-phase to fully react in the reactor 1 until the conversion rate of the raw materials reaches the conversion rate requirement set by the extraction valve 5 (the conversion rate of the product of the extraction valve 5 is generally set to be above 80%); the feed valve 3, the extraction valve 5, the product valve 9 and the small micro-nano bubble generating device 42 are opened, and the gas-liquid two-phase or the gas-liquid-solid three-phase is fully reacted in the reactor 8 until the conversion rate reaches the conversion rate requirement set by the product valve 9 (the conversion rate of the product valve 9 can be set to 100%), and the product flows out from the product valve 9, and at this time, a continuous reaction of full conversion of the gas-liquid-solid three-phase is realized.

[0044] Example 3 The structures of the micro-nano bubble generator A412 and the micro-nano bubble generator B422 in the large micro-nano bubble generating device 41 and the small micro-nano bubble generating device 42 can be as follows: Figure 2 The micro-nano bubble generator, the full conversion reaction system using the preferred micro-nano bubble generator is as follows Figure 7 As shown. The micro-nano bubble generator includes a shell 432 and a generating column 431 installed in the shell 432. The shell 432 has a gas-liquid inlet 4323 and a gas-liquid outlet 4324. The gas-liquid mixture entering from the gas-liquid inlet 4323 flows through the generating column 431 and then flows out from the gas-liquid outlet 4324. The generating column 431 includes a plurality of bubble cutting units 4311. The surface of the bubble cutting unit 4311 is provided with a flow channel 4312. There are pressure-reducing grooves 4314 between the bubble cutting units 4311. The gas-liquid mixture is sheared, stirred and dispersed under the action of the bubble cutting unit 4311, and enters the annular pressure-reducing groove 4314. Because the cross-sectional area of ​​the cavity for accommodating the fluid passing through the pressure-reducing groove 4314 increases, the pressure is reduced, the gas dissolved in the liquid is released, and micro-nano bubbles are continuously generated.

[0045] In this embodiment, the flow channel 4312 adopts a spiral flow channel 4312. When the fluid flows through the spiral flow channel 4312, the spiral structure causes the gas-liquid two-phase fluid to produce a rotational motion, and the gas and liquid are continuously sheared, stirred and dispersed in the flow channel 4312. Compared with a straight channel, the spiral flow channel can significantly improve the uniformity of gas-liquid mixing.

[0046] The inflow end of the bubble cutting unit 4311 is provided with a serrated surface 4313, see Figure 2 and Figure 3 . The serrated surface increases impact and convection effects.

[0047] A collision platform 4315 is provided at the front end of the bubble cutting unit 4311 at the end of the gas-liquid inlet 4323. The collision platform 4315 is a multi-step truncated cone, and the collision platform 4315, the bubble cutting unit 4311 and the gas-liquid inlet 4323 are coaxially arranged. The collision platform 4315 impacts and collides the fluid entering from the gas-liquid inlet 4323 to generate convection, thereby enhancing the gas-liquid mixing effect; under the action of the impact force, the bubble will split into multiple smaller bubbles.

[0048] See also Figure 2 and Figure 5 The shell 432 includes an outer shell 4321 and an inner shell 4322. The generating column 431 is arranged in the cavity of the inner shell 4322. The two ends of the inner shell 4322 are respectively provided with a gas-liquid inlet 4323 and a gas-liquid outlet 4324. The cavity of the outer shell 4321 is provided with an air chamber 433. The air inlet 4331 of the air chamber 433 is arranged on the outer shell 4321, and the air outlet 4332 of the air chamber 433 is communicated with the cavity of the inner shell 4322. The air inlet 4331 of the air chamber 433 is located in the middle and upper part of the outer shell 4321, and the air outlet 4332 of the air chamber 433 is located at the gas-liquid outlet 4324. The air outlet 4332 is arranged at the gas-liquid outlet 4324, and more gas phase medium is brought in under the action of the high-speed gas-liquid mixed fluid. The air inlet 4331 of the air chamber is connected to the gas phase outlet 14 of the reactor 1, the gas phase outlet 71 of the heat exchanger 7, and the gas phase outlet 82 of the reactor 8. The discharged gas phase medium is reintroduced into the reaction system through the air chamber 433, which can improve the reaction conversion rate.

[0049] The gas-liquid inlet 4323 includes a gradually decreasing volume bell section 43231 and a cylindrical section 43232, and the diameter of the generating column 431 is larger than the diameter of the cylindrical section 43232 but smaller than the maximum diameter of the bell section 43231. The gradually decreasing volume bell section 43231 and the cylindrical section 43232 structure increases the fluid entry velocity and enhances the impact effect.

[0050] The gas-liquid outlet 4324 is in the shape of a gradually expanding trumpet, and the end of the generating column 431 has a gradually increasing diameter truncated cone section 4316, and the diameter of the truncated cone section 4316 is smaller than the diameter of the bubble cutting unit 4311. A channel is formed between the truncated cone section 4316 and the gas-liquid outlet 4324, and high-concentration micro-nano bubbles are discharged from the gas-liquid outlet 4324.

[0051] The number of bubble cutting units 4311 is not less than 3. The generating column 431 of this embodiment has 10 bubble cutting units 4311 and 9 pressure reducing grooves 4314. The pressure in the generating column is measured, and the pressure magnitudes at various locations are shown in Table 1. When the gas-liquid mixed fluid enters the cylindrical section 43232 of the gas-liquid inlet 4323, the pressure is 0.4-1.0Mpa, and the cross-sectional area at the collision platform 4315 and the pressure reducing groove 4314 increases, and the pressure is reduced to produce micro-nano bubbles. After 10 times of increasing the cross-sectional area and reducing the pressure, the pressure is 0.14-0.3Mpa.

[0052] Table 1 Pressure values ​​at the point where the cross-sectional area increases The higher the pressure, the higher the gas solubility. Reducing the pressure can gradually release the dissolved gas (turning into bubbles), and the gas will produce micro-nano bubbles through impact and collision. The bubble size and proportion can be controlled by increasing or decreasing the number of pressure reductions.

[0053] The mass transfer effects of bubbles of different sizes were compared, and the results are as follows: Figure 6 As shown, Stratified Flow, Translent Flow, and Mist Flow refer to laminar flow, transmission flow, and mist flow, respectively. The mist flow has a large proportion and a good mass transfer effect. a, b, c, and d are respectively large bubble mass transfer effect, medium bubble mass transfer effect, small bubble mass transfer effect, and micro-nano bubble mass transfer effect, wherein the bubbles in c are generated by a venturi ejector, and the micro-nano bubbles in d are generated by the micro-nano bubble generator of the present invention. The micro-nano bubble generator can reduce laminar flow, increase mist flow, and improve mass transfer efficiency by more than 30%. Compared with ordinary bubbles generated by a venturi ejector, the mass transfer effect of micro-nano bubbles can be improved by 4 times.

[0054] The above description is only the preferred embodiment of the present application and is not intended to limit the present application. For those skilled in the art, the present application may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application shall be included in the protection scope of the present application.

Claims

1. A continuous gas-liquid two-phase or gas-liquid-solid three-phase full conversion reaction system, characterized in that: The invention comprises a reaction kettle, a reactor, a heat exchanger, a large micro-nano bubble generating device and a small micro-nano bubble generating device. A feeding port and a gas-liquid inlet are respectively arranged on the top and the bottom of the reaction kettle. A gas phase outlet and a liquid phase product outlet are arranged between the feeding port and the gas-liquid inlet, and the gas phase outlet is located above the liquid phase product outlet. The gas-liquid inlet of the reaction kettle is connected to the outlet of the large micro-nano bubble reaction device, the liquid phase product outlet of the reaction kettle is connected to the inlet of the heat exchanger and the extraction valve, the outlet of the heat exchanger is connected to the inlet of the large micro-nano bubble reaction device, the outlet of the extraction valve is connected to the inlet of the small micro-nano bubble generating device, the outlet of the small micro-nano bubble generating device is connected to the bottom end of the reactor, a product outlet is arranged in the middle and upper part of the reactor, and the product outlet is connected to the product valve.

2. A continuous gas-liquid two-phase or gas-liquid-solid three-phase full conversion reaction system according to claim 1, characterized in that: The gas-liquid inlet of the reaction kettle is connected to the outlet end of the first check valve, and the inlet end of the first check valve is connected to the outlet of the raw material inlet valve and the large micro-nano bubble generating device.

3. A continuous gas-liquid two-phase or gas-liquid-solid three-phase full conversion reaction system according to claim 1, characterized in that: The gas phase outlet of the reactor is connected to the inlet of the second check valve, the top gas phase outlet of the heat exchanger is connected to the inlet of the third check valve, the top gas phase outlet of the reactor is connected to the fourth check valve, and the outlets of the second check valve, the third check valve and the fourth check valve are respectively connected to the gas supply pipeline.

4. A continuous gas-liquid two-phase or gas-liquid-solid three-phase full conversion reaction system according to claim 1, characterized in that: The large micro-nano bubble generating device includes a circulation pump A, a micro-nano bubble generator A and an air intake pipeline A, and the small micro-nano bubble generating device includes a circulation pump B, a micro-nano bubble generator B and an air intake pipeline B. The air intake pipeline A and the air intake pipeline B are respectively connected to the air circuit valve, and the air circuit valve is connected to the air supply equipment.

5. A continuous gas-liquid two-phase or gas-liquid-solid three-phase full conversion reaction system according to claim 4, characterized in that: The micro-nano bubble generator A and the micro-nano bubble generator B both include a shell and a generating column installed in the shell, the shell has a gas-liquid inlet and a gas-liquid outlet, the gas-liquid mixture entering from the gas-liquid inlet flows through the generating column and then flows out from the gas-liquid outlet, the generating column includes a plurality of bubble cutting units, a flow channel is provided on the surface of the bubble cutting unit, and a pressure reduction groove is provided between the bubble cutting units.

6. A continuous gas-liquid two-phase or gas-liquid-solid three-phase full conversion reaction system according to claim 5, characterized in that: The flow channel is a spiral flow channel; the inflow end of the bubble cutting unit is provided with a serrated surface; and the front end of the bubble cutting unit at the gas-liquid inlet end is provided with a collision platform.

7. A continuous gas-liquid two-phase or gas-liquid-solid three-phase full conversion reaction system according to claim 5, characterized in that: The shell comprises an outer shell and an inner shell, the generating column is arranged in the inner shell cavity, the two ends of the inner shell are respectively provided with a gas-liquid inlet and a gas-liquid outlet, an air chamber is arranged in the outer shell cavity, the air inlet of the air chamber is arranged on the outer shell, and the air outlet of the air chamber is communicated with the inner shell cavity.

8. A continuous gas-liquid two-phase or gas-liquid-solid three-phase full conversion reaction system according to claim 5, characterized in that: The air inlet of the air chamber is located in the upper middle part of the shell, and the air outlet of the air chamber is located at the gas-liquid outlet; the gas-liquid inlet includes a gradually decreasing bell-mouth section and a cylindrical section, and the diameter of the generating column is larger than the diameter of the cylindrical section but smaller than the maximum diameter of the bell-mouth section; the gas-liquid outlet is a gradually expanding bell-mouth shape, and the end of the generating column has a truncated cone section with a gradually increasing diameter, and the diameter of the truncated cone section is smaller than the diameter of the bubble cutting unit.

9. A continuous gas-liquid two-phase or gas-liquid-solid three-phase full conversion reaction system according to claim 1, characterized in that: A feed valve is arranged between the large micro-nano bubble generating device and the reaction kettle.

10. A continuous gas-liquid two-phase or gas-liquid-solid three-phase full conversion reaction system according to any one of claims 1 to 9, characterized in that: The reaction kettle and the reactor are respectively provided with loaded catalysts, and the loaded catalysts are arranged inside the reaction kettle in a vertical, horizontal or spiral manner.

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