Gas-liquid distribution plate and gas-liquid reactor

Abstract

This utility model relates to the field of gas-liquid reaction technology, specifically to a gas-liquid distribution plate and a gas-liquid reactor, comprising an outer plate, a sieve plate, and an inner plate arranged sequentially from the outside to the inside; a first flow channel is formed between the outer plate and the sieve plate, and the first flow channel has multiple first flow channel outlets with diameters in the micrometer and / or nanometer ranges; multiple baffles are installed at intervals between the sieve plate and the inner plate to form multiple breaking flow channels; bubbles accumulated in the first flow channel enter the breaking flow channels through the holes in the sieve plate and are broken into micrometer-sized and / or nanometer-sized bubbles by a turbulence-inducing component, and the micrometer-sized and / or nanometer-sized bubbles flow out from the breaking flow channel outlets; a second flow channel is formed inside the inner plate, and a second flow channel outlet is provided above the second flow channel with a diameter in the millimeter range. This utility model generates a gas-liquid mixed flow composed of a large number of micro- and nanometer-sized bubbles and a small number of millimeter-sized bubbles, referred to as a multi-scale gas-liquid mixed flow.

Description

Technical Field

[0001] This utility model relates to the field of gas-liquid reaction technology, specifically to a gas-liquid distribution plate and a gas-liquid reactor. Background Technology

[0002] A gas-liquid mixture is a multiphase reaction process involving both gas and liquid phases. Typically, gaseous reactants dissolve in the liquid phase before reacting with other reactants in the liquid phase; alternatively, all reactants may be in the gas phase, dissolved in a solution containing a catalyst before reacting. In the chemical and environmental protection fields, there are numerous instances of gas-liquid mixing, such as gas-liquid reactions and wastewater treatment. In these situations, gas-liquid mixing often has a significant impact on the reaction efficiency and wastewater treatment effectiveness.

[0003] Miniaturization of bubbles is a key technology in the chemical industry for promoting mass transfer and accelerating chemical reactions. In the prior art, disclosed in publication number WO2025091314A1, entitled "A Synthesis System and Method for Lithium Hexafluorophosphate," the synthesis system includes a gas-liquid reactor and a built-in microbubble generator unit disposed inside the reactor. The side wall of the gas-liquid reactor has a material inlet and a gas inlet. The built-in microbubble generator unit includes a first microbubble generator and a second microbubble generator. The first microbubble generator is located below the liquid level in the gas-liquid reactor and connected to the material inlet, while the second microbubble generator is located at the bottom of the reactor and connected to the gas inlet. Multiple layers of perforated plates are arranged sequentially from top to bottom inside the gas-liquid reactor, with the through holes of the multiple layers of perforated plates staggered and positioned between the first and second microbubble generators. This increases the mass transfer area between the lithium fluoride liquid and the phosphorus pentafluorophosphate gas in the above synthesis system, improves the reaction rate, and reduces energy consumption.

[0004] However, the slow flow rate of micron- and nano-sized bubbles is not conducive to further promoting gas-liquid reactions. Utility Model Content

[0005] To address the problem that a large number of micro- and nano-sized bubbles in the gas-liquid reaction in the prior art are not conducive to further promoting the gas-liquid reaction, the purpose of this invention is to provide a gas-liquid distribution plate and a gas-liquid reactor.

[0006] The technical solution provided by this utility model is as follows:

[0007] In a first aspect, a gas-liquid distribution plate includes an outer plate, a sieve plate, and an inner plate arranged sequentially from the outside to the inside;

[0008] A first flow channel is formed between the outer plate and the sieve plate. The first flow channel has multiple first flow channel outlets with diameters in the micrometer and / or nanometer ranges. Under the action of pressure difference, millimeter-sized bubbles pass through the first flow channel outlets to form micrometer-sized bubbles and / or nanometer-sized bubbles.

[0009] Multiple crushing channels are formed between the screen plate and the inner plate by multiple partitions installed at intervals, and turbulence components are installed in the crushing channels; the inlet of each crushing channel is connected to the first channel through the screen plate hole provided by the screen plate.

[0010] The bubbles accumulated in the first flow channel enter the crushing flow channel through the sieve plate holes and are broken into micron-sized and / or nano-sized bubbles by the turbulence component. The micron-sized and / or nano-sized bubbles flow out from the outlet of the crushing flow channel.

[0011] A second flow channel is formed inside the inner plate, and a second flow channel outlet is set above the second flow channel. The diameter of the second flow channel outlet is on the order of millimeters.

[0012] As an optional technical solution in the first aspect, the second flow channel outlet is located in the middle of the upper part of the gas-liquid distribution plate, and the first flow channel outlet and the crushing flow channel outlet are both located on the side of the second flow channel outlet.

[0013] The flux at the outlet of the first flow channel is denoted as K1, the flux at the outlet of the second flow channel is denoted as K2, and the flux at the outlet of the crushing flow channel is denoted as K3; where K2 = 5% to 15% (K1 + K2 + K3).

[0014] As one of the optional technical solutions in the first aspect, the screen plate is provided with screen plate holes divided into multiple layers, and each layer of screen plate holes corresponds to each crushing flow channel; along the direction from the outlet of the first flow channel to the inlet of the first flow channel, the total throughput of each layer of screen plate holes gradually decreases.

[0015] Optionally, along the direction from the outlet of the first flow channel to the inlet of the first flow channel, the number of holes in each layer of sieve plate gradually decreases, and the diameter of the holes in each layer of sieve plate gradually increases.

[0016] Furthermore, the aperture of the sieve plate is 1 to 10 mm.

[0017] As an optional technical solution in the first aspect, the end of the partition plate near the outlet of the crushing channel and the end of the inner plate near the outlet of the second channel are both inclined toward the center line of the gas-liquid distribution plate; the inclination angle θ ranges from 5° to 60°.

[0018] As an optional technical solution in the first aspect, the turbulence component has multiple sets, and each set of turbulence components includes correspondingly installed concave and convex parts;

[0019] The concave and convex parts are respectively arranged on both sides of the crushing channel radially and are staggered along the axial direction of the crushing channel;

[0020] The distance between the concave and convex parts is denoted as d1; the radial dimension of the breaking flow channel is denoted as d2; the distance between two adjacent sets of turbulence components is denoted as d3.

[0021] The ratio of d1 to d2 ranges from 1 / 3 to 2 / 3; the ratio of d3 to d2 ranges from 1 to 3.

[0022] In a second aspect, a gas-liquid reactor includes a tank having a liquid inlet and a liquid outlet; a plurality of air inlet pipes are installed at intervals inside the tank; and a gas-liquid distribution plate, as in the first aspect or any of the optional technical solutions of the first aspect, is provided above the air inlet pipes.

[0023] As an optional technical solution in the second aspect, a fixing plate is installed above the air inlet pipe, and multiple gas-liquid distribution plates are installed on the fixing plate; several first air guide pipes are installed on the side edge of the fixing plate; an air guide plate is installed above the fixing plate, the air guide plate is provided with several through holes for liquid to pass through, and the air guide plate is also provided with second air guide pipes corresponding to the first air guide pipes; the top of the tank is also provided with an inert gas outlet.

[0024] Optionally, a stirring blade is provided between the air guide plate and the fixed plate. The stirring blade is connected to the drive mechanism, which is used to drive the stirring blade to rotate.

[0025] Compared with the prior art, the technical solution provided by this utility model has the following advantages:

[0026] This invention generates a gas-liquid mixture flow consisting of a large number of micro-nano-sized bubbles and a small number of millimeter-sized bubbles, referred to as a multi-scale gas-liquid mixture flow. The micro-nano bubbles provide a large gas-liquid contact area for gas-liquid mixing, improving the reaction effect and wastewater treatment effect. At the same time, the flexible stirring effect of the millimeter-sized bubbles can improve the surface renewal of the micro-nano bubbles, that is, improve the gas-liquid mass transfer coefficient, thereby further improving the reaction effect and wastewater treatment effect. Attached Figure Description

[0027] Figure 1 This is a schematic diagram of a gas-liquid distribution plate in one embodiment of this application;

[0028] Figure 2 This is a schematic diagram of the multi-layer sieve holes provided in the gas-liquid distribution plate in one embodiment of this application;

[0029] Figure 3 This is a schematic diagram of the partition and inner plate ends in an inclined state in one embodiment of this application;

[0030] Figure 4 This is a schematic diagram of the bubble flow direction in one embodiment of this application;

[0031] Figure 5A schematic diagram illustrating the agitation of micron-sized bubbles by millimeter-sized bubbles;

[0032] Figure 6 This is a schematic diagram of a mixture of millimeter-sized and micrometer-sized bubbles in one embodiment of this application;

[0033] Figure 7 This is a schematic diagram of a turbulence component in one embodiment of this application;

[0034] Figure 8 This is a schematic diagram of a gas-liquid reactor in one embodiment of this application;

[0035] Figure 9 for Figure 8 Enlarged view of point A in the middle;

[0036] Figure 10 This is a schematic diagram of the air guide plate in one embodiment of this application.

[0037] Explanation of the labels in the diagram:

[0038] Outer plate 101, sieve plate 102, sieve plate hole 103, partition plate 104, end plate 105, inner plate 106, first flow channel inlet 201, first flow channel 202, first flow channel outlet 203, crushing flow channel outlet 204, crushing flow channel 205, turbulence component 206, concave part 206-1, convex part 206-2, second flow channel inlet 301, second flow channel 302, second flow channel outlet 303, tank body 401, liquid inlet 402, liquid outlet 403, inert gas outlet 404, drive mechanism 405-1, stirring blade 405-2, fixed plate 406, first air guide pipe 407, air inlet pipe 408, air guide plate 409, second air guide pipe 410, through hole 411. Detailed Implementation

[0039] To further understand the content of this utility model, a detailed description of this utility model will be provided in conjunction with the accompanying drawings and embodiments.

[0040] The structures, proportions, and sizes illustrated in the accompanying drawings are solely for illustrative purposes and to aid those skilled in the art in understanding and reading the invention. They are not intended to limit the scope of the invention and therefore have no substantial technical significance. Any modifications to the structure, changes in proportions, or adjustments to size, provided they do not affect the effectiveness or purpose of the invention, should still fall within the scope of the technical content disclosed herein. Furthermore, terms such as "upper," "lower," "left," "right," and "middle" used in this specification are merely for clarity and not intended to limit the scope of implementation. Changes or adjustments to their relative relationships, without substantially altering the technical content, should also be considered within the scope of the invention's implementation.

[0041] In one embodiment, this application proposes a gas-liquid distribution plate, such as... Figure 1-3 As shown, the gas-liquid distribution plate includes an outer plate 101, a sieve plate 102, and an inner plate 106 arranged sequentially from the outside to the inside. The outer plate 101, sieve plate 102, and inner plate 106 can be generally cylindrical, thereby forming a first flow channel 202 between the outer plate 101 and the sieve plate 102.

[0042] The first flow channel 202 has a first flow channel inlet 201 at one end and multiple first flow channel outlets 203 at the other end. Specifically, an end plate 105 can be installed at one end of the first flow channel 202, and multiple first flow channel outlets 203 are provided on the end plate 105. The aperture of the first flow channel outlets 203 is in the micrometer and / or nanometer range. When a millimeter-sized large bubble enters the first flow channel 202 through the first flow channel inlet 201, it will flow towards the first flow channel outlet 203. Under the action of pressure difference, the millimeter-sized large bubble will pass through the first flow channel outlet 203, thereby being split into micrometer-sized and / or nanometer-sized small bubbles.

[0043] Since the inner plate 106 is roughly cylindrical, a second flow channel 302 is formed inside the inner plate 106. One end of the second flow channel 302 is provided with a second flow channel inlet 301, and the other end of the first flow channel 302 is provided with a second flow channel outlet 303. The diameter of the second flow channel outlet 303 is on the order of millimeters.

[0044] It should be noted that the first flow channel outlet 203 and the second flow channel outlet 303 are located at the same end of the gas-liquid distribution plate.

[0045] Most of the large millimeter-sized bubbles enter the first flow channel 202 and are broken down into micrometer-sized and / or nanometer-sized bubbles. The remaining small portion of the large millimeter-sized bubbles enters the second flow channel 302 and continues to flow out as large bubbles with a diameter of millimeters from the second flow channel outlet 303.

[0046] Because the first flow channel outlet 203 and the second flow channel outlet 303 are located at the same end of the gas-liquid distribution plate, a small portion of millimeter-sized large bubbles will be mixed in with the micron- and / or nano-sized small bubbles. For example... Figure 5-6 As shown, micron- and / or nano-sized bubbles provide sufficient interphase area to maintain concentration near the bubbles. Millimeter-sized large bubbles provide liquid-phase disturbance, promoting mass transfer at the gas-liquid film end. Both work together to ensure and enhance the reaction process.

[0047] Because the orifice diameter of the first flow channel outlet 203 is small and the throughput is limited, when a large number of millimeter-sized large bubbles enter the first flow channel 202, these large bubbles will accumulate along the direction from the first flow channel outlet 203 to the first flow channel inlet 201. In order to improve the production rate of micron-sized and / or nano-sized small bubbles, it is necessary to break up the accumulated millimeter-sized large bubbles into micron-sized and / or nano-sized small bubbles.

[0048] In this embodiment, multiple spaced-apart partitions 104 are installed between the sieve plate 102 and the inner plate 106, thereby forming multiple independent crushing channels 205 between the sieve plate 102 and the inner plate 106. The inlets of the multiple crushing channels 205 are arranged along the direction from the first channel outlet 203 to the first channel inlet 201. Specifically, the sieve plate 102 is provided with sieve plate holes 103 corresponding to the inlets of each crushing channel 205, and the crushing channels 205 communicate with the first channel 202 through the sieve plate holes 103. Millimeter-sized large bubbles accumulated in the first channel 202 will enter the crushing channels 205 through the sieve plate holes 103.

[0049] Large air bubbles entering the crushing channel 205 through the sieve plate holes 103 on the side of the sieve plate 102 need to pass through the turbulence component 206 to be broken into smaller micron- and / or nano-sized air bubbles.

[0050] like Figure 4 As shown, the bubbles accumulated in the first flow channel 202 enter the crushing flow channel 205 through the sieve plate hole 103 and are crushed into micron-sized bubbles and / or nano-sized bubbles by the turbulence component 206. The micron-sized bubbles and / or nano-sized bubbles flow out from the crushing flow channel outlet 204.

[0051] Micron- and / or nano-sized bubbles flowing out of the broken flow channel outlet 204 and micron- and / or nano-sized bubbles flowing out of the first flow channel outlet 203 together form small bubbles, while millimeter-sized large bubbles flowing out of the second flow channel outlet 303 will agitate the small bubbles.

[0052] As an optional embodiment, such as Figure 1-3 As shown, the second flow channel outlet 303 is located in the middle of the upper part of the gas-liquid distribution plate, while the first flow channel outlet 203 and the breaking flow channel outlet 204 are both located to the side of the second flow channel outlet 303. The large millimeter-sized bubbles generated at this time can agitate more small bubbles.

[0053] The flux at the outlet 203 of the first flow channel is denoted as K1, the flux at the outlet 303 of the second flow channel is denoted as K2, and the flux at the outlet 204 of the broken flow channel is denoted as K3; where K2 = 5% to 15% (K1 + K2 + K3). In other words, large bubbles only account for a small portion, and only a small number of large bubbles are needed to agitate the small bubbles.

[0054] Optionally, such as Figure 2 As shown, the sieve plate 102 is provided with sieve plate holes 103 divided into multiple layers, and each layer of sieve plate holes 103 corresponds to each crushing flow channel 205. Along the direction from the outlet 203 of the first flow channel to the inlet 201 of the first flow channel, the total throughput of each layer of sieve plate holes 103 gradually decreases.

[0055] Since the bubbles accumulate along the direction from the first flow channel outlet 203 to the first flow channel inlet 201, the closer to the first flow channel outlet 203, the more bubbles accumulate. Therefore, the total throughput of the sieve plate holes 103 corresponding to the crushing flow channel 205 that is closer to the first flow channel outlet 203 should be larger, so as to allow more large bubbles to enter the crushing flow channel 205 through the sieve plate holes 103.

[0056] Along the direction from the outlet 203 of the first flow channel to the inlet 201 of the first flow channel, the number of holes 103 in each layer of sieve plate gradually decreases, and the hole diameter of each layer of sieve plate holes 103 gradually increases.

[0057] Along the direction from the outlet 203 of the first flow channel to the inlet 201 of the first flow channel, there are fewer bubbles closer to the inlet 201 of the first flow channel. Moreover, bubbles closer to the inlet 201 of the first flow channel are less likely to enter the sieve plate hole 103. Therefore, the sieve plate hole 103 closer to the inlet 201 of the first flow channel has a larger hole diameter, which facilitates the bubbles to enter the crushing flow channel 205 through the sieve plate hole 103.

[0058] As an optional embodiment, the aperture of the sieve plate hole 103 is 1-10 mm, for example... Figure 2 The first layer of the sieve plate has holes 1mm in diameter, the second layer has holes 2mm in diameter, the third layer has holes 3mm in diameter, and the fourth layer has holes 4mm in diameter. The hole diameter of the sieve plate 103 should not be too small, as this will hinder the passage of air bubbles. Conversely, the hole diameter should not be too large, as this will prevent the sieve plate 103 from effectively pre-breaking up large air bubbles.

[0059] Preferably, the ends of the baffle 104 near the outlet 204 of the break-up channel and the ends of the inner plate 106 near the outlet 303 of the second channel are inclined toward the centerline of the gas-liquid distribution plate; the inclination angle θ ranges from 5° to 60°. In this case, the outlet 204 of the break-up channel can be oriented toward the centerline of the distribution plate, that is, approximately toward the outlet 303 of the second channel. The micron-sized and / or nano-sized bubbles flowing out of the outlet 204 of the break-up channel will flow toward the millimeter-sized bubbles, which is beneficial for the millimeter-sized bubbles to agitate the micron-sized and / or nano-sized bubbles, and also agitate the micron-sized and / or nano-sized bubbles flowing out of the outlet 203 of the first channel.

[0060] Regarding the structure of the aerodynamic component, in one embodiment, such as Figure 7 As shown, the turbulence-inducing components 206 are in multiple sets, each set including correspondingly installed concave members 206-1 and convex members 206-2. The concave members 206-1 and convex members 206-2 are respectively arranged on both radial sides of the breaking channel 205 and are staggered along the axial direction of the breaking channel 205. When the liquid flows, guided by the concave members 206-1 and convex members 206-2, turbulence is generated, thereby breaking large bubbles into smaller bubbles.

[0061] Preferably, the distance between the concave member 206-1 and the convex member 206-2 is denoted as d1; the radial dimension of the breaking flow channel 205 is denoted as d2; and the distance between two adjacent sets of turbulence-causing components 206 is denoted as d3; wherein the ratio of d1 to d2 ranges from 1 / 3 to 2 / 3; and the ratio of d3 to d2 ranges from 1 to 3. In this technical solution, turbulence is more easily formed, and large bubbles are more easily broken into smaller bubbles.

[0062] For the turbulence component 206, existing technologies for breaking large bubbles into micron- and / or nano-sized bubbles by hydraulic means can also be used, which will not be elaborated or limited here.

[0063] In one embodiment, this application also proposes a gas-liquid reactor, such as... Figure 8-9 As shown, the device includes a tank 401, which has a liquid inlet 402 and a liquid outlet 403. Preferably, the liquid inlet 402 is located at the upper part of the tank 401, and the liquid outlet 403 is located at the lower part of the tank 401, with the liquid flowing from top to bottom.

[0064] Multiple gas inlet pipes 408 are installed at intervals inside the tank 401. At this time, the gas phase used for reaction in the tank 401 is introduced in segments, and the input amount of each segment of gas phase can be controlled, thereby avoiding waste of reaction gas.

[0065] The aforementioned gas-liquid distribution plate is installed above the air inlet pipe 408. Millimeter-sized large bubbles in the liquid pass through the gas-liquid distribution plate to form a mixture of mostly small bubbles and a small portion of large bubbles, which is beneficial for gas-liquid reaction in the tank 401.

[0066] As an optional embodiment, a fixing plate 406 is installed above the air intake pipe 408, and multiple gas-liquid distribution plates are installed on the fixing plate 406.

[0067] Several first air guide pipes 407 are installed on the side edge of the fixed plate 406, and an air guide plate 409 is installed above the fixed plate 406. Figure 10 As shown, the air guide plate 409 is provided with a plurality of through holes 411 for liquid to pass through, and the air guide plate 409 is also provided with a second air guide pipe 410 corresponding to the first air guide pipe 407.

[0068] Some of the inert gas generated during the gas-liquid reaction needs to be guided out. Since the liquid in tank 401 flows from top to bottom, and the orifice 411 has a diameter of only 1-3 mm, inert gas bubbles have difficulty passing through it. Instead, they flow into the second gas guide pipe 410, which extends vertically. After flowing out of the second gas guide pipe 410, the inert gas bubbles continue to rise vertically, eventually flowing into the first gas guide pipe 407, which corresponds to the second gas guide pipe 410. Similarly, the first gas guide pipe 407 also extends vertically, allowing the inert gas bubbles in tank 401 to flow through the first gas guide pipe 407 and the second gas guide pipe 410 to the upper part of tank 401, and finally exit from the inert gas outlet 404 located at the top of tank 401.

[0069] As an optional technical solution, a stirring blade 405-2 is provided between the air guide plate 409 and the fixed plate 406. The stirring blade 405-2 is connected to the drive mechanism 405-1, which drives the stirring blade 405-2 to rotate, thereby accelerating the reaction and preventing stratification. The drive mechanism 405-1 is relatively mature in the prior art and will not be described or limited here.

[0070] The present invention and its embodiments have been described above illustratively. This description is not restrictive, and the figures shown are only one embodiment of the present invention; the actual structure is not limited thereto. Therefore, if those skilled in the art are inspired by this description and design similar structures and embodiments without departing from the inventive spirit of the present invention, such designs should fall within the protection scope of the present invention.

Claims

1. A gas-liquid distribution plate, characterized in that: It includes an outer plate (101), a sieve plate (102), and an inner plate (106) that are sequentially nested from the outside to the inside; A first flow channel (202) is formed between the outer plate (101) and the sieve plate (102). The first flow channel (202) is provided with multiple first flow channel outlets (203). The diameter of the first flow channel outlets (203) is in the micrometer and / or nanometer range. Multiple crushing channels (205) are formed between the sieve plate (102) and the inner plate (106) through multiple partitions (104) installed at intervals. A flow disturbance component (206) is installed in the crushing channel (205). The inlet of each crushing channel (205) is connected to the first channel (202) through the sieve plate hole (103) provided in the sieve plate (102). The bubbles accumulated in the first flow channel (202) enter the crushing flow channel (205) through the sieve plate holes (103) and are crushed into micron-sized bubbles and / or nano-sized bubbles by the turbulence component (206). The micron-sized bubbles and / or nano-sized bubbles flow out from the crushing flow channel outlet (204). A second flow channel (302) is formed inside the inner plate (106), and a second flow channel outlet (303) is provided above the second flow channel (302). The diameter of the second flow channel outlet (303) is on the order of millimeters.

2. The gas-liquid distribution plate according to claim 1, characterized in that: The second flow channel outlet (303) is located in the middle of the upper part of the gas-liquid distribution plate, and the first flow channel outlet (203) and the broken flow channel outlet (204) are both located to the side of the second flow channel outlet (303); The flux of the first flow channel outlet (203) is denoted as K1, the flux of the second flow channel outlet (303) is denoted as K2, and the flux of the crushing flow channel outlet (204) is denoted as K3; wherein, K2 = 5%~15% (K1+K2+K3).

3. The gas-liquid distribution plate according to claim 1, characterized in that: The sieve plate (102) is provided with sieve plate holes (103) divided into multiple layers, and each layer of sieve plate holes (103) corresponds to each crushing flow channel (205); Along the direction from the outlet (203) of the first flow channel to the inlet (201) of the first flow channel, the total throughput of each layer of sieve plate holes (103) gradually decreases.

4. The gas-liquid distribution plate according to claim 3, characterized in that: Along the direction from the outlet (203) of the first flow channel to the inlet (201) of the first flow channel, the number of holes (103) in each layer of sieve plate gradually decreases, and the aperture of the holes (103) in each layer of sieve plate gradually increases.

5. The gas-liquid distribution plate according to claim 4, characterized in that: The aperture of the sieve plate hole (103) is 1 to 10 mm.

6. The gas-liquid distribution plate according to claim 1, characterized in that: The end of the partition (104) near the outlet (204) of the crushing channel and the end of the inner plate (106) near the outlet (303) of the second channel are both inclined toward the center line of the gas-liquid distribution plate; the inclination angle θ ranges from 5° to 60°.

7. The gas-liquid distribution plate according to claim 1, characterized in that: The aerodynamic components (206) are in multiple sets, and each set of aerodynamic components (206) includes a concave member (206-1) and a convex member (206-2) that are installed accordingly; The concave part (206-1) and the convex part (206-2) are respectively arranged on both sides of the crushing channel (205) radially and are staggered along the axial direction of the crushing channel (205); The distance between the concave part (206-1) and the convex part (206-2) is denoted as d1; the radial dimension of the breaking flow channel (205) is denoted as d2; the distance between two adjacent sets of turbulence components (206) is denoted as d3; The ratio of d1 to d2 ranges from 1 / 3 to 2 / 3; the ratio of d3 to d2 ranges from 1 to 3.

8. A gas-liquid reactor, comprising a tank (401) having a liquid inlet (402) and a liquid outlet (403); characterized in that: Multiple air inlet pipes (408) are installed at intervals inside the tank body (401); A gas-liquid distribution plate as described in any one of claims 1-7 is provided above the air intake pipe (408).

9. The gas-liquid reactor according to claim 8, characterized in that: A fixing plate (406) is installed above the air intake pipe (408), and multiple gas-liquid distribution plates are installed on the fixing plate (406); Several first air guide tubes (407) are installed on the side edge of the fixed plate (406); A guide plate (409) is installed above the fixed plate (406). The guide plate (409) has several through holes (411) for liquid to pass through. The guide plate (409) is also provided with a second guide pipe (410) corresponding to the first guide pipe (407). The top of the tank (401) is also provided with an inert gas outlet (404).

10. The gas-liquid reactor according to claim 9, characterized in that: An agitator blade (405-2) is provided between the air guide plate (409) and the fixed plate (406). The agitator blade (405-2) is connected to the drive mechanism (405-1), which is used to drive the agitator blade (405-2) to rotate.

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