A gas-liquid mixing reactor

Abstract

The present invention relates to the technical field of chemical machinery and equipment, and specifically relates to a gas-liquid mixing reactor, which includes a swirl chamber, a gas nozzle, a rotating wheel and a swirl mixing chamber. After a liquid flow under a certain pressure enters the swirl chamber, it is forced to rotate through the action of the blades in the rotating wheel, and then flows out in a swirling state from the liquid outlet. Compressed gas is diffused and ejected through the gas nozzle. The ejected gas and the swirling liquid are cut and mixed with each other and then enter the swirl mixing chamber, and a shearing and dispersion effect is generated. At the same time, the corresponding pressure is adjusted by a valve installed at the front end of the swirl mixing chamber, so as to achieve the best gas dissolution effect. The present invention adopts a frustum-shaped rotating wheel to realize the forced rotation of the liquid, reduce the pressure drop of the liquid in the pipeline, and at the same time has no moving components, making it more reliable and energy-saving to use. At the same time, by adopting a gas nozzle, a shearing and dispersion effect occurs between the gas-liquid two phases, improving the mixing effect and facilitating use in industrial production.

Description

Technical Field

[0001] The invention relates to the technical field of chemical machinery and equipment, and in particular to a gas-liquid mixing reactor. Background Art

[0002] Gas-liquid mixing reactors are used in the process of industrial wastewater treatment in non-ferrous metals, rare earth alloy smelting, petrochemical industry, pharmaceutical industry, and environmental protection and pollution control. Gas-liquid mixing reactors, as the name suggests, are mainly used for mixing and reacting gases and compatible liquids. Expanding and ensuring the gas-liquid contact area is the core concept of the design of gas-liquid mixing reactors.

[0003] Traditional gas-liquid mixers mainly include Venturi mixers, static mixers, etc.; Venturi mixer is a device that integrates suction and mixing, with a unique mixing chamber design, strong water flow and air or liquid mixed injection, which improves the gas dissolution efficiency; static mixer is a high-efficiency mixing device without moving parts. Its basic working mechanism is to use the mixing unit fixed in the tube to change the flow state of the fluid in the tube, so as to achieve good dispersion and sufficient mixing between different fluids.

[0004] Static mixers are used to mix different fluids. During the mixing process, they have a large heat exchange coefficient, high dispersion efficiency, fast mixing speed, small pressure drop of materials in the mixer, small volume, low energy consumption, and pipelined operation. However, due to the internal structure of alternating forward and reverse rotating blades, they are not suitable for rapid mixing of high-speed fluids. Venturi mixers have the advantages of simple structure, easy operation, low investment cost and low operating cost. On the one hand, they have a good mixing effect on different fluids. On the other hand, they can directly mix fluids of different pressures and increase the pressure of fluids with lower pressures. However, there are certain defects in the process. When the fluid flow rate increases, it is easy for the fluid to have insufficient agitation intensity and insufficient mixing effect. Summary of the invention

[0005] The object of the present invention is to provide a gas-liquid mixing reactor to solve the problem that the existing gas-liquid mixer has insufficient mixing effect for large flow and high flow rate fluids during use.

[0006] To achieve the above-mentioned purpose, the present invention adopts the following technical scheme: a gas-liquid mixing reactor, comprising a cyclone chamber and a cyclone mixing chamber, one side of the cyclone chamber is a liquid inlet, a rotating wheel is arranged in the cyclone chamber, a liquid outlet is arranged at the center of the rotating wheel, blades are evenly distributed on the rotating wheel, an air inlet pipe is arranged on the cyclone chamber, the air inlet pipe extends to the inside of the cyclone chamber and extends out from the liquid outlet after being bent, the diameter of the air inlet pipe is smaller than the diameter of the liquid outlet, a gas nozzle is installed at the end of the air inlet pipe, the end of the cyclone chamber is connected with the cyclone mixing chamber, and the inner diameter of the cyclone mixing chamber is uniformly shrunk.

[0007] Furthermore, the rotary wheel is frustum-shaped, and the blades are evenly distributed inside the rotary wheel and extend inward to the top of the rotary wheel.

[0008] Furthermore, the blade radius of the blade is consistent with the inner diameter of the swirl chamber, the ratio of the liquid flow areas at both ends of the rotary wheel is 6-9, and the angle between the side surface of the rotary wheel and the tube wall of the swirl chamber is 30-40°.

[0009] Furthermore, the rear of the swirl mixing chamber is connected to a variable-diameter chamber, the variable-diameter chamber is connected to a pressure measurement chamber, the pressure measurement chamber is connected to an adjustment valve, and a pressure gauge is installed on the pressure measurement chamber.

[0010] Furthermore, corrosion-resistant linings are arranged on the inner sides of the swirl chamber, the swirl mixing chamber, the variable-diameter chamber, and the pressure measurement chamber.

[0011] Furthermore, the angle between the side surface of the swirl mixing chamber and the horizontal plane is 35-45°, and the ratio of the liquid flow areas at both ends of the swirl mixing chamber is 4-6.

[0012] The beneficial effects of the present invention: By adopting a frustum-shaped rotary wheel, forced rotation of the liquid is achieved, and the pressure drop of the liquid in the pipeline is reduced. At the same time, there are no moving components, making it more reliable and energy-saving in use. Meanwhile, by adopting a gas nozzle, shear dispersion of the gas-liquid two-phase occurs, improving the mixing effect and facilitating use in industrial production. Description of the Drawings

[0013] Figure 1 is a schematic diagram of the overall structure of the present invention;

[0014] Figure 2 is a schematic diagram of the internal structure of the swirl chamber of the present invention;

[0015] Figure 3 is a schematic diagram of the liquid flow direction at the rotary wheel of the present invention;

[0016] Figure 4 is a schematic diagram of the liquid flow force at the rotary wheel of the present invention;

[0017] Figure 5 is a schematic diagram of the liquid flow direction and the gas flow direction at the gas nozzle of the present invention;

[0018] Figure 6 is a schematic diagram of the liquid flow direction and the gas flow direction at the swirl mixing chamber of the present invention;

[0019] Figure 7 is a schematic diagram of the liquid flow direction and the gas flow direction at the variable-diameter chamber of the present invention.

[0020] The names corresponding to the marks in the figure:

[0021] 1. Swirl chamber; 11. Intake pipe; 111. Gas nozzle; 12. Liquid inlet; 13. Rotating wheel; 131. Blade; 132. Liquid outlet; 2. Swirl mixing chamber; 3. Reducing chamber; 4. Pressure measuring chamber; 41. Pressure gauge; 5. Control valve; 6. Corrosion-resistant lining; 7. Liquid flow direction; 8. Gas flow direction; f1. Liquid flow pressure; f2. Support force of the rotating wheel on the wall; f3. Support force of the lower blade; f4. Pressure of the upper blade. Detailed implementation mode

[0022] Next, the technical solutions in the embodiments of the present invention will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present invention.

[0023] Embodiment: As Figure 1 shown, a swirl chamber 1 is arranged in the reactor and connected to a swirl mixing chamber 2, the swirl mixing chamber 2 is connected to a reducing chamber 3, the reducing chamber 3 is connected to a pressure measuring chamber 4, the pressure measuring chamber 4 is connected to a control valve 5, and a corrosion-resistant lining 6 is arranged inside the gas-liquid swirl mixing reactor.

[0024] As Figure 1-2 shown, an intake pipe 11 is installed on the swirl chamber 1 of the gas-liquid swirl mixing reactor. The intake pipe 11 extends into the swirl chamber 1 and is arranged parallel to the swirl chamber 1 after being bent. A gas nozzle 111 is installed at the end of the intake pipe 11. A rotating wheel 13 is also arranged in the swirl chamber 1. The rotating wheel 13 is frustum-shaped and blades 131 are arranged around it. At the same time, a liquid outlet 132 is arranged at the end of the rotating wheel 13. The intake pipe 11 passes through the liquid outlet 132 and is connected to the gas nozzle 111.

[0025] As Figures 3-5 shown, at the rotating wheel 13 in the swirl chamber 1, when the pressurized liquid flows forward, due to the frustum shape of the rotating wheel 13, it will be subject to the support force f2 of the rotating wheel on the wall, the support force f3 of the lower blade, and the pressure f4 of the upper blade, and under the coercion of the liquid flow pressure f1, the flow direction will change, so that the liquid velocity has a tangential component, realizing a swirl flow state. After the liquid flows out from the liquid outlet 132, due to the expansion of the inner diameter of the swirl chamber 1, under the action of centrifugal force, the liquid flow direction 7 is in an outward diffusion state, and the gas flow direction 8, due to the action of the gas nozzle 8, is in a peripheral radiation state, and the gas flow direction 8 and the liquid flow direction 7 undergo a shearing action.

[0026] As Figures 6-7 shown, in the swirl mixing chamber 2, due to the reduction of the inner diameter of the swirl mixing chamber 2, the liquid flow direction 7 is in an inward contraction state, and the gas flow direction 8 is still in a peripheral radiation state and rotates and diffuses together with the liquid flow direction 7. In the reducing chamber 3, due to the expansion of the inner diameter of the reducing chamber 3, the liquid flow direction 7 is in an outward diffusion state (the velocity decreases), and at this time the gas has basically diffused into the liquid and is consistent with the liquid flow direction 7.

[0027] The principle of the present invention is as follows: Liquid enters the swirl chamber 1 from the liquid inlet 12 of the gas-liquid mixing reactor. At this time, the liquid has a certain pressure. Since there are no moving components in the entire gas-liquid mixing reactor, the liquid flows relying on the initial pressure, which also makes the entire gas-liquid mixing reactor more energy-efficient.

[0028] After the liquid with a certain pressure enters the swirl chamber 1, it is forced to rotate under the action of the blades 131 of the rotating wheel 13. During the process, due to the frustum-shaped setting of the rotating wheel 13, there is a certain buffering effect on the liquid in the flow direction, resulting in a small pressure drop. Furthermore, it can reduce the pressure at the liquid inlet 12, thereby reducing energy consumption. The change in liquid pressure is closely related to the liquid flow velocity u1, the angle θ between the side surface of the frustum of the rotating wheel 13 and the horizontal plane, the ratio k1 (k1>1) of the liquid flow area at the bottom and top of the frustum of the rotating wheel 13, and the blade radius r of the blade 131. The relevant exploration is as follows:

[0029] Take the diameter of the swirl chamber 1 as 500 mm, the diameter of the intake pipe 11 as 100 mm, the angle θ between the side surface of the frustum of the rotating wheel 13 and the inner wall of the swirl chamber 1 as 30°, the liquid flow area at the top surface of the frustum of the rotating wheel 13 as 23550 mm 2 , that is, k1 is 8.3, and the blade radius r of the blade 131 is 250 mm. Explore the relationship between the pressure drop ΔP and the liquid flow velocity u1. During the exploration process, the liquid medium is water, and a differential pressure gauge is installed between the liquid inlet 12 and the liquid outlet 132.

[0030] During the exploration process, the theoretical ΔP can be obtained according to Bernoulli's equation:

[0031]

[0032] In the formula: ρ is the density of water;

[0033] k1 is the ratio of the liquid flow area at the bottom and top of the frustum of the rotating wheel 13.

[0034] Thus, we can get:

[0035]

[0036] Table 1 Relationship table of pressure drop ΔP1 and liquid flow velocity u1

[0037] It can be seen that the actual pressure drop ΔP1 is greater than the theoretical pressure drop ΔP. This is because of the mutual friction between fluids and the mutual collision with the pipeline during the process, resulting in a certain amount of energy loss. As the liquid flow rate increases, the difference between the actual pressure drop ΔP and the theoretical pressure drop ΔP shows an increasing state, and as the liquid flow rate increases, this difference change becomes more and more obvious. It can be seen that when the liquid flow rate is less than 1.5 m / s, the pressure drop ΔP loss is less, so it is more energy-saving. When the flow rate is greater than 1.5 m / s, the pressure drop ΔP increases significantly, and a large amount of energy loss will be caused during the process, thereby increasing the equipment energy consumption and production cost. Compared with the existing static mixer, the fluid flow rate is generally less than 0.8 m / s, and the gas-liquid mixing reactor of the present invention has a significant improvement compared thereto.

[0038] The diameter of the swirl chamber 1 is taken as 500 mm, the diameter of the air inlet pipe 11 is 100 mm, the liquid flow rate u1 is 1 m / s, and the liquid flow-through area on the top surface of the frustum of the rotating wheel 13 is 23550 mm 2 , that is, k1 is 8.3, the blade radius r of the blade 131 is 250 mm, the relationship between the pressure drop ΔP1 and the angle θ between the side surface of the frustum of the rotating wheel 13 and the horizontal plane is explored. During the exploration process, the liquid medium is water, and a differential pressure gauge is installed between the liquid inlet 12 and the liquid outlet 132.

[0039] The calculation of the theoretical pressure drop ΔP is the same as the above Bernoulli equation, so we can get:

[0040]

[0041] Table 2 Relationship table of pressure drop ΔP1 and angle θ

[0042] It can be seen that when the angle θ is less than 40°, although there is a difference between the actual pressure drop ΔP1 and the theoretical pressure drop ΔP, the difference is not very large. However, when the angle θ is greater than 40°, the pressure loss increases significantly, indicating that as the angle θ increases, the obstruction intensity of the rotating wheel 13 on the liquid also increases, and it is particularly obvious when the angle is greater than 40°. Therefore, in actual production, the angle θ should be less than 40°. However, it should be noted that it is not the smaller the better. When the angle θ is too small, the corresponding length of the rotating wheel 13 will increase significantly, which will also increase the cost of the equipment. It is appropriate to select the angle θ between 30 and 40° in actual use.

[0043] The diameter of the swirl chamber 1 is taken as 500 mm, the diameter of the air inlet pipe 11 is 100 mm, the liquid flow rate u1 is 1 m / s, and the liquid flow-through area on the top surface of the frustum of the rotating wheel 13 is 23550 mm 2, that is, k1 is 8.3, the angle θ between the side of the frustum of the rotating wheel 13 and the horizontal plane is 30°. Explore the relationship between the pressure drop ΔP1 and the blade radius r of the blade 131. During the exploration process, the liquid medium is water, and a differential pressure gauge is installed between the liquid inlet 12 and the liquid outlet 132.

[0044] The calculation of the theoretical pressure drop ΔP is the same as the above Bernoulli equation, and it is only related to the flow area ratio k1 and the flow velocity u1. Thus, we can obtain:

[0045]

[0046] Table 3 Relationship table between pressure drop ΔP1 and blade radius r

[0047] It can be seen that as the blade radius r increases, the pressure drop ΔP1 decreases significantly. When the blade radius is greater than 200, the change in the actual pressure drop ΔP1 tends to be gentle. This indicates that when the blade radius r is small, the bending strength of the blade is large, and the forced swirling force on the liquid is strong, resulting in a large amount of energy loss of the liquid. When the blade radius r is large, the swirling of the liquid transitions smoothly, effectively reducing the energy loss, which is beneficial to reducing energy consumption. Therefore, in actual use, the blade radius r of the blade 131 can be greater than 200. At the same time, it can also be seen that the selection of the blade radius r has a great relationship with the radius of the rotating wheel 13, and the value is taken near the inner diameter of the rotating wheel 13.

[0048] For the flow area ratio k1 (k1 > 1) between the bottom and top of the frustum of the rotating wheel 13, take the diameter of the swirl chamber 1 as 500 mm, the diameter of the air inlet pipe 11 as 100 mm, the liquid flow velocity u1 as 1 m / s, the blade radius r of the blade 131 as 250 mm, and the angle θ between the side of the frustum of the rotating wheel 13 and the horizontal plane as 30°. Explore the relationship between the pressure drop ΔP1 and the flow area ratio k1 between the bottom and top of the frustum of the rotating wheel 13. During the exploration process, the liquid medium is water, and a differential pressure gauge is installed between the liquid inlet 12 and the liquid outlet 132.

[0049] The calculation of the theoretical pressure drop ΔP is the same as the above Bernoulli equation. Thus, we can obtain:

[0050]

[0051] Table 4 Relationship table between pressure drop ΔP1 and flow area ratio k1

[0052] It can be seen that with the increase of the flow area ratio k1, the actual pressure drop ΔP1 increases slowly at first and then sharply. This means that when the flow area at the liquid outlet 132 is too small, the liquid flow rate will increase sharply, resulting in a substantial energy loss in the process, thereby increasing energy consumption. However, when the flow area ratio is too small, the speed of the liquid passing through the liquid outlet 132 will decrease, resulting in insufficient contact with the gas and affecting the mixing effect. Therefore, the flow area ratio k1 is generally selected between 6 and 9 during actual use.

[0053] The liquid passing through the rotating wheel 13 flows out from the liquid outlet 12 in a swirling state, and the compressed gas is diffused and sprayed out through the gas nozzle 111. The sprayed gas and the swirling liquid are cut and mixed with each other and then enter the swirling mixing chamber 2, and a shearing dispersion effect is generated. The shearing dispersion effect in the process is closely related to the gas flow rate u2 and the liquid swirling speed u3. In actual operation, it is not easy to directly measure the effect of the shearing dispersion effect. However, when the liquid flow rate u1 and the gas flow rate u2 are constant, the shearing dispersion effect will be manifested through the change of pressure. Pressure gauges are installed at both ends of the swirling mixing chamber 2. Differential pressure gauge, when the shear dispersion effect is good, the pressure difference changes significantly, and when the effect is not good, the pressure difference change is not obvious, so the shear dispersion effect can be expressed by the reading of the differential pressure gauge, and the liquid swirl velocity u3 is closely related to the blade radius r and the liquid flow rate u1. In addition, the gas and liquid phases are fully mixed in the swirl mixing chamber. The mixing effect in the process is related to the length l and the change of the inner diameter of the swirl mixing chamber 2. The change of the inner diameter in the process can be expressed by the ratio k2 of the inlet and outlet inner diameters of the swirl mixing chamber 2. Therefore, the relevant research is as follows:

[0054] When the diameter of the swirl chamber 1 is 500mm, the diameter of the air inlet pipe 11 is 100mm, the liquid flow rate u1 is 1m / s, the blade radius r is 250mm, the length l of the swirl mixing chamber 2 is 0.5m, and the ratio k2 of the inlet and outlet areas of the swirl mixing chamber 2 is 5, the relationship between the differential pressure gauge reading ΔP2 and the gas flow rate u2 is explored.

[0055]

[0056] Table 5 Relationship between gas flow rate u2 and differential pressure gauge reading ΔP2

[0057] It can be seen that with the increase of gas flow rate u2, the differential pressure gauge reading ΔP2 first increases rapidly and then remains basically unchanged. When the differential pressure gauge reading ΔP2 increases rapidly, it means that the introduced gas is basically dissolved, but when the gas flow rate u2 increases to 25m / s, the differential pressure gauge reading ΔP2 remains basically unchanged, indicating that the gas is excessive and the gas-liquid two phases can no longer be well mixed. Therefore, for the gas flow rate u2, it is advisable to choose less than 20m / s in actual operation.

[0058] When the diameter of the swirl chamber 1 is 500 mm, the diameter of the intake pipe 11 is 100 mm, the gas flow velocity u2 is 20 m / s, and the blade radius r is 250 mm, the length l of the swirl mixing chamber 2 is 0.5 m, and the ratio k2 of the inlet area to the outlet area of the swirl mixing chamber 2 is 5, the relationship between the differential pressure gauge reading ΔP2 and the liquid flow velocity u1 is explored.

[0059]

[0060] Table 6 Relationship table between liquid flow velocity u1 and differential pressure gauge reading ΔP2

[0061] It can be seen that as the liquid flow velocity u1 increases, the differential pressure gauge reading ΔP2 first changes significantly and then the change trend becomes smaller. This indicates that when the liquid flow velocity u1 decreases, the gas is not well mixed. When the liquid flow velocity u1 increases, the liquid swirl intensity increases, making the mixing with the gas more sufficient. However, due to the increase in the liquid flow velocity u1, the pressure drop ΔP2 increases. Therefore, the pressure drop ΔP2 is still increasing, but the increase amplitude decreases.

[0062] When the diameter of the swirl chamber 1 is 500 mm, the diameter of the intake pipe 11 is 100 mm, the liquid flow velocity u1 is 1 m / s, the gas flow velocity u2 is 20 m / s, the length l of the swirl mixing chamber 2 is 0.5 m, and the ratio k2 of the inlet area to the outlet area of the swirl mixing chamber 2 is 5, the relationship between the differential pressure gauge reading ΔP2 and the blade radius r is explored.

[0063]

[0064] Table 7 Relationship table between blade radius r and differential pressure gauge reading ΔP2

[0065] It can be seen that as the blade radius r increases, the differential pressure gauge reading ΔP2 first remains basically unchanged and then decreases instead. During the process, as the blade radius r increases, the liquid swirl intensity decreases. Therefore, when the blade radius r is between 200 and 300, the liquid swirl intensity is sufficient, so it can be fully mixed with the gas. When the blade radius r exceeds 300, the liquid swirl intensity weakens, resulting in insufficient gas-liquid mixing and causing the decrease in the differential pressure gauge reading ΔP2. Therefore, combining the above exploration, it is appropriate to select the blade radius r of the rotating wheel 13 between 200 and 300.

[0066] When the diameter of the swirl chamber 1 is 500 mm, the diameter of the intake pipe 11 is 100 mm, the liquid flow velocity u1 is 1 m / s, the gas flow velocity u2 is 20 m / s, and the blade radius r is 250 mm, the length l of the swirl mixing chamber 2 is 0.5 m, and the relationship between the differential pressure gauge reading ΔP2 and the ratio k2 of the inlet area to the outlet area of the swirl mixing chamber 2 is explored.

[0067]

[0068] Table 8 Relationship Table between Area Ratio k2 and Differential Pressure Gauge Reading ΔP2

[0069] It can be seen that as the area ratio k2 increases, the differential pressure gauge reading ΔP2 shows an increasing trend. When the area ratio k2 is less than 4, the differential pressure gauge reading ΔP2 is relatively small, indicating that the gas-liquid mixing is not sufficient at this time. When the area ratio k2 is between 4 and 6, the differential pressure gauge reading ΔP2 is relatively stable, indicating that the gas-liquid mixing is sufficient at this time. When the area ratio k2 is greater than 6, the differential pressure gauge reading ΔP2 increases significantly at this time, indicating that due to the increase in the area ratio k2, the outlet of the swirl mixing chamber 2 decreases significantly, resulting in a large amount of energy loss during the process and increasing the energy consumption. Therefore, the area ratio k2 is preferably between 4 and 6.

[0070] Take the diameter of the swirl chamber 1 as 500 mm, the diameter of the inlet pipe 11 as 100 mm, the liquid velocity u1 as 1 m / s, the gas velocity u2 as 20 m / s, the blade radius r as 250 mm, and when the ratio k2 of the inlet and outlet areas of the swirl mixing chamber 2 is 5, explore the relationship between the differential pressure gauge reading ΔP2 and the length l of the swirl mixing chamber 2.

[0071]

[0072] Table 9 Relationship Table between the Length l of the Swirl Mixing Chamber and the Differential Pressure Gauge Reading ΔP2

[0073] It can be seen that as the swirl mixing chamber 2 increases, the differential pressure gauge reading ΔP2 shows a trend of increasing first and then tending to be stable, indicating that when the length l is small, the gas-liquid mixing time is short and the mixing process is not sufficient. When the length l is greater than 0.5 m, the gas-liquid is basically mixed sufficiently. Although the differential pressure gauge reading ΔP2 still has a small increase, considering the equipment cost, the length l of the swirl mixing chamber 2 is preferably between 0.5 and 0.8 m in the actual process. At this time, the angle between the side of the swirl mixing chamber 2 and the horizontal plane is between 32° and 45°.

[0074] The gas-liquid two-phase has been basically mixed completely after passing through the swirl mixing chamber 2. At this time, further mixing is carried out through the variable-diameter chamber 3. The variable-diameter chamber 3 diffuses the liquid, which can make the gas-liquid mixing more uniform. However, correspondingly, due to energy loss and the expansion of the inner diameter, the liquid velocity and the swirl velocity will both decrease. Another function of the variable-diameter chamber 3 is to connect instruments and valves, etc. with the swirl mixing chamber 2. During the process, the pressure of the overall mixing reactor can be adjusted by adjusting the opening degree of the valve 5, so as to achieve the best gas dissolution effect, realizing the adjustable function of the entire gas-liquid mixing reactor, which is convenient for reasonable adjustment and use according to needs during the production process.

[0075] The above exploration shows that the gas-liquid mixing reactor of the present invention can still achieve good mixing of gas-liquid two phases at large flow rates and large flow velocities, which is convenient for selection in the actual production process.

[0076] The present invention is not limited to the above best implementation mode. Anyone can obtain other various forms of products under the inspiration of the present invention. However, no matter what changes are made in its shape or structure, as long as it has the same or similar technical solutions as the present application, it falls within the protection scope of the present invention.

Claims

1. A gas-liquid mixing reactor, characterized in that: It includes a swirl chamber (1) and a swirl mixing chamber (2). One side of the swirl chamber (1) is a liquid inlet (12). A rotating wheel (13) is arranged in the swirl chamber (1). A liquid outlet (132) is arranged at the center of the rotating wheel (13). Blades (131) are evenly distributed on the rotating wheel (13). An air inlet pipe (11) is arranged on the swirl chamber (1). The air inlet pipe (11) extends into the interior of the swirl chamber (1), bends and extends out from the liquid outlet (132). The diameter of the air inlet pipe (11) is smaller than the diameter of the liquid outlet (132). A gas spray head (111) is installed at the end of the air inlet pipe (11). The end of the swirl chamber (1) is connected to the swirl mixing chamber (2), and the inner diameter of the swirl mixing chamber (2) uniformly contracts; the rotating wheel (13) is arranged in a frustum shape, and the blades (131) are evenly distributed on the inner side of the rotating wheel (13) and extend inward to the top of the rotating wheel (13); the blade radius of the blades (131) is consistent with the inner diameter of the swirl chamber (1), the ratio of the liquid flow areas at both ends of the rotating wheel (13) is 6 to 9, and the angle between the side surface of the rotating wheel (13) and the tube wall of the swirl chamber (1) is 30 to 40°.

2. The gas-liquid mixing reactor according to claim 1, wherein: The rear of the swirl mixing chamber (2) is connected to a variable-diameter chamber (3). The variable-diameter chamber (3) is connected to a pressure measurement chamber (4). The pressure measurement chamber (4) is connected to a regulating valve (5). A pressure gauge (41) is installed on the pressure measurement chamber (4).

3. The gas-liquid mixing reactor according to claim 2, wherein: Corrosion-resistant linings (6) are arranged on the inner sides of the swirl chamber (1), the swirl mixing chamber (2), the variable-diameter chamber (3), and the pressure measurement chamber (4).

4. A gas-liquid mixing reactor according to claim 1, wherein: The angle between the side surface of the swirl mixing chamber (2) and the horizontal plane is 35 to 45°, and the ratio of the liquid flow areas at both ends of the swirl mixing chamber (2) is 4 to 6.

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