Gas-liquid mixing assembly and its use in cumene oxidation

Abstract

The application relates to the technical field of chemical equipment, and discloses a gas-liquid mixing assembly and application of the gas-liquid mixing assembly in cumene oxidation, wherein the gas-liquid mixing assembly comprises a spraying pipe and a porous material membrane pipe, the spraying pipe and the porous material membrane pipe are coaxially connected to form a continuous internal flow channel for liquid flow, the spraying pipe comprises, in sequence along the flow direction of the liquid, a liquid inlet section, a throttling section, a gas inlet section and a gas-liquid two-phase development section, the flow channel cross-sectional area of the liquid inlet section is equal to that of the gas inlet section and is larger than that of the throttling section, and the gas inlet section and the porous material membrane pipe are respectively provided with a pore structure for introducing gas into the internal flow channel; the application realizes efficient mixing of gas-liquid two phases under the conditions of high flux and high gas-liquid ratio by setting two gas-liquid mixing zones and gradually mixing gas-liquid two phases by the spraying pipe and the porous material membrane pipe, and effectively overcomes the defect that the prior art cannot form a large number of micro-nano bubbles under the conditions of high flux and high gas-liquid ratio.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of chemical equipment, in particular to a gas-liquid mixing assembly and its application in cumene oxidation. BACKGROUND

[0002] Multiphase reactions such as hydrogenation and oxidation are widely used in process industry, such as benzene hydrogenation, PX air oxidation, diesel fixed bed hydrogenation, etc. These reaction processes are severely restricted by heat transfer rate and mass transfer rate, which in turn affects the overall efficiency of the reaction. The fundamental reason is that the interfacial area between gas and liquid, gas and liquid solid is too small. Taking the traditional bubble type air oxidation reactor as an example, due to the bubble diameter generally between 5-30mm, under normal pressure conditions, the interfacial area between gas and liquid is usually 20-300m 2 ·m -3 , and in most cases less than 100m 2 ·m -3 . Therefore, in industrial practice, people usually use methods such as increasing gas circulation or adding internal components to the reactor to strengthen mass transfer and improve reaction, but the effect is very limited.

[0003] The principle of micro-interface enhanced reaction technology (MIR) is to efficiently control the geometric scale of gas-liquid, gas-liquid-liquid, and gas-liquid-solid interface from millimeter to micron, which greatly increases the interfacial area. When the bubble is gradually reduced from several millimeters to micron level, the gas-liquid mass transfer rate and reaction rate will be significantly enhanced, thereby doubling the efficiency of chemical production process, greatly reducing energy and material consumption, and improving safety and environmental protection performance. The key to micro-interface enhanced reaction technology is the enhanced mixing of multiple phases, such as gas-liquid two-phase enhanced mixing, so the preparation of micro-bubbles is particularly important. Existing technologies have gradually developed micro-bubble preparation methods suitable for different occasions. Specifically, according to the generation method of micro-bubbles, it can be divided into the following types: (1) shear breaking into bubbles, such as Venturi type micro-bubble generator; (2) pressure reduction or temperature rise into bubbles, such as pressure dissolution type micro-bubble generator; (3) ultrasonic wave into bubbles; (4) micro-pore into bubbles, such as micro-porous plastic, rubber and ceramic tubes, etc.

[0004] In the prior art, gas-liquid two-phase enhanced mixing technology is mainly applied to water treatment, breeding and medicine, and less applied to chemical production. The main reason is that there are difficulties in scaling up the micro-mixer, one of the core problems is how to prepare micro-bubbles on a large scale and high throughput, and the other problem is that there are certain technical limitations in the preparation of micro-bubbles under high gas-liquid ratio conditions. SUMMARY

[0005] The application aims to overcome the problem of poor mixing efficiency of gas-liquid two-phase under high flux and high gas-liquid ratio in the prior art, and provide a gas-liquid mixing assembly and its application in cumene oxidation, which can effectively improve the mixing efficiency of gas-liquid two-phase under high flux and high gas-liquid ratio.

[0006] To achieve the above-mentioned purpose, the application provides a gas-liquid mixing assembly in the first aspect, comprising a spray pipe and a porous material membrane pipe, the spray pipe and the porous material membrane pipe are coaxially connected to form a continuous internal flow channel for liquid flow, the spray pipe comprises a liquid inlet section, a throttling section, a gas inlet section and a gas-liquid two-phase development section arranged in sequence along the flow direction of the liquid, the flow channel cross-sectional area of the liquid inlet section is equal to that of the gas inlet section and larger than that of the throttling section, and the gas inlet section and the porous material membrane pipe are respectively provided with a pore structure for introducing gas into the internal flow channel.

[0007] Preferably, the liquid flux of the gas-liquid mixing assembly is 30-1000 L / h, preferably 60-300 L / h.

[0008] The gas flux of the gas-liquid mixing assembly is 30-10000 L / h, preferably 60-1200 L / h.

[0009] The gas-liquid volume ratio per unit length is 0.1-10 m -1 ; preferably 0.5-4 m -1 .

[0010] Preferably, a sieve plate is arranged at the throttling section, and a plurality of sieve holes are arranged on the sieve plate.

[0011] Preferably, the diameter of the sieve hole is 1-3 mm, and the number of the sieve hole is 1-30, preferably 4-12.

[0012] Preferably, the angle between the axial direction of the sieve hole and the cross section of the spray pipe perpendicular to the length direction is 90°.

[0013] Preferably, the angle between the axial direction of the sieve hole and the cross section of the spray pipe perpendicular to the length direction is 30°-60°.

[0014] Preferably, the end of the gas inlet section close to the throttling section is arranged to be spaced apart from the liquid outlet end of the throttling section.

[0015] Preferably, the distance between the end of the gas inlet section close to the throttling section and the liquid outlet end of the throttling section is 1-10 mm, preferably 2-5 mm.

[0016] Preferably, the pipe wall of the injection pipe is provided with a sintered film of metal material with a mean pore size of 1-50 μm, preferably 1-20 μm.

[0017] Preferably, the base material of the porous material film pipe is selected from one of stainless steel, quartz, alumina, polytetrafluoroethylene, polypropylene and polyethylene.

[0018] Preferably, the porous material film pipe has a pore size of 1-100 μm, preferably 3-10 μm.

[0019] Preferably, the porous material film pipe is provided with a plurality of channels extending along the axial direction thereof, and the plurality of channels combine to form the internal flow channel for the liquid to flow through the porous material film pipe.

[0020] Preferably, the number of channels is 9-60, preferably 18-40.

[0021] Preferably, the inner wall of each channel is provided with a porous structure coating.

[0022] Preferably, the porous structure coating has a pore size of 20-800 nm, preferably 150-600 nm.

[0023] Preferably, each channel has a constant diameter structure, and the inner diameter of the channel is 1-6 mm, preferably 2-4 mm.

[0024] Alternatively, each channel comprises an inner hole tapering section and an inner hole expanding section arranged in sequence along the flow direction of the liquid, and the length ratio of the inner hole expanding section to the inner hole tapering section is 1-5:1, preferably 1.5-2.5:1.

[0025] Preferably, the gas-liquid mixing assembly further comprises a packing pipe, which is arranged at the end of the porous material film pipe away from the injection pipe, and the packing pipe is filled with packing.

[0026] Preferably, the length of the packing pipe is 1-30% of the length of the porous material film pipe, preferably 5-10%.

[0027] Preferably, the size of the packing is 1-10 mm, preferably 2-5 mm.

[0028] The second aspect of the present application provides a use of the aforementioned gas-liquid mixing assembly in cumene oxidation, wherein the gas-liquid mixing assembly is built into a reactor for cumene oxidation, and a plurality of the gas-liquid mixing assemblies are arranged in parallel, and the plurality of gas-liquid mixing assemblies are used to mix the gas and the liquid participating in the cumene oxidation reaction to form a gas-liquid mixture; the gas is an oxygen-containing gas, and the liquid is a liquid containing cumene or an oxidation liquid containing cumene hydroperoxide.

[0029] Preferably, the catalyst active component is loaded in the internal flow channel at the tube of the porous material membrane; or

[0030] The outlet of the tube of the porous material membrane is provided with a filler, and the catalyst active component is loaded on the filler; or

[0031] The outlet of the tube of the porous material membrane is provided with a filler prepared from a material containing the catalyst active component.

[0032] Preferably, the catalyst active component is selected from oxides of at least one of copper, magnesium, cobalt, manganese, nickel, chromium, zinc, iron, silver, and gold.

[0033] Preferably, the loading amount of the catalyst active component is 0.01% to 10%, preferably 0.05% to 5%, of the weight of the tube of the porous material membrane or the filler.

[0034] Preferably, the loading method of the catalyst active component is impregnation, vacuum coating, chemical vapor deposition, or atomic layer deposition.

[0035] Compared with the prior art, the gas-liquid mixing assembly provided by the present application can, when used, cause the liquid to enter from the end of the injection tube away from the tube of the porous material membrane and sequentially pass through the internal flow channel of the injection tube and the tube of the porous material membrane, and the gas to enter the internal flow channel through the gas inlet section of the injection tube and the tube of the porous material membrane, and mix with the liquid to form a gas-liquid mixture.

[0036] The present application provides two gas-liquid mixing areas in the flow direction of the liquid, and gas can be introduced into the internal flow channel in both of the two gas-liquid mixing areas, thereby ensuring the mixing efficiency of the gas-liquid two-phase under the conditions of high flux and high gas-liquid ratio. Specifically, by arranging the injection tube as a liquid inlet section, a throttling section, a gas inlet section, and a gas-liquid two-phase development section connected in sequence, the liquid enters the throttling section from the liquid inlet section, and due to the decrease in the cross-sectional area of the flow channel, the flow rate of the liquid increases. When the liquid enters the gas inlet section, the pressure inside the liquid suddenly drops, causing the liquid to rapidly spread to the periphery and generate intense vortex and turbulent flow. This part of the liquid and the gas entering through the gas inlet section are subjected to intense mixing and friction, forming a primary gas-liquid mixture rich in small gas bubbles. The gas and the liquid continue to interact and mix during the flow through the gas-liquid two-phase development section, making the mixing of the gas-liquid two-phase more sufficient. Further, the primary gas-liquid mixture rich in small gas bubbles enters the internal flow channel of the tube of the porous material membrane, and the gas entering the internal flow channel through the tube wall of the tube of the porous material membrane mixes with the primary gas-liquid mixture again, which not only effectively increases the gas-liquid ratio of the gas-liquid mixture, but also increases the bubble density in the gas-liquid mixture, promoting the sufficient mixing of the gas-liquid two-phase.

[0037] The gas-liquid mixing assembly provided by the application realizes high-efficiency mixing of gas-liquid two phases under high flux and high gas-liquid ratio conditions by setting two gas-liquid mixing areas and gradually mixing gas-liquid two phases by cooperating with the injection pipe and the porous material membrane pipe, and effectively overcomes the defect that the prior art cannot form a large amount of micro-nano bubbles under high flux and high gas-liquid ratio conditions. BRIEF DESCRIPTION OF DRAWINGS

[0038] Figure 1 is a structural schematic diagram of a gas-liquid mixing assembly provided by the application;

[0039] Figure 2 is a structural schematic diagram of another gas-liquid mixing assembly provided by the application;

[0040] Figure 3 is a schematic diagram of application of a gas-liquid mixing assembly provided by the application in isopropyl benzene oxidation;

[0041] BRIEF DESCRIPTION OF DRAWINGS

[0042] 1, reactor; 10, injection pipe; 11, liquid inlet section; 12, throttling section; 13, gas inlet section; 14, gas-liquid two-phase development section; 15, sieve plate; 151, sieve hole; 20, porous material membrane pipe; 21, channel; 211, inner hole tapering section; 212, inner hole expanding section; 30, filler pipe; 31, filler. DETAILED DESCRIPTION

[0043] The specific embodiments of the application will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are only used to illustrate and explain the application, and are not used to limit the application.

[0044] In combination with Figure 1 and Figure 2 shown, the application provides a gas-liquid mixing assembly, which comprises an injection pipe 10 and a porous material membrane pipe 20, the injection pipe 10 and the porous material membrane pipe 20 are coaxially connected to form a continuous internal flow channel for liquid flow, the injection pipe 10 comprises a liquid inlet section 11, a throttling section 12, a gas inlet section 13 and a gas-liquid two-phase development section 14 arranged in sequence along the flow direction of the liquid, the flow channel cross-sectional area of the liquid inlet section 11 is equal to that of the gas inlet section 13 and is larger than that of the throttling section 12, and the gas inlet section 13 and the porous material membrane pipe 20 are respectively provided with a pore structure for introducing gas into the internal flow channel.

[0045] The gas-liquid mixing component provided by the present invention, when in use, the liquid enters from the end of the injection tube 10 away from the porous material membrane tube 20 and passes through the internal flow channels of the injection tube 10 and the porous material membrane tube 20 in sequence, and the gas enters the internal flow channel through the air inlet section 13 of the injection tube 10 and the porous material membrane tube 20, and mixes with the liquid to form a gas-liquid mixture.

[0046] The present invention provides two gas-liquid mixing areas in the flow direction of the liquid, and gas can be introduced into the internal flow channel in both gas-liquid mixing areas, thereby ensuring the mixing efficiency of the gas-liquid two phases under high flux and high gas-liquid ratio conditions. Specifically, by setting the injection pipe 10 as a liquid inlet section 11, a throttling section 12, an air inlet section 13 and a gas-liquid two-phase development section 14 connected in sequence, in the process of the liquid entering the throttling section 12 through the liquid inlet section 11, the cross-sectional area of ​​the flow channel becomes smaller and the flow rate of the liquid becomes faster. When entering the air inlet section 13, the pressure inside the liquid suddenly drops sharply, causing the liquid to quickly diffuse to the surrounding area, generating violent eddy currents and turbulence. This part of the liquid and the gas entering through the air inlet section 13 undergo violent mixing friction to form a primary gas-liquid mixture rich in small bubbles. The gas and the liquid continue to interact and mix in the process of flowing through the gas-liquid two-phase development section 14, so that the mixing of the gas-liquid two phases is more sufficient; further, the primary gas-liquid mixture rich in small bubbles enters the internal flow channel of the porous material membrane tube 20, and the gas entering the internal flow channel through the tube wall of the porous material membrane tube 20 is remixed with the primary gas-liquid mixture, which can not only effectively improve the gas-liquid ratio of the gas-liquid mixture, but also improve the bubble density in the gas-liquid mixture, thereby promoting sufficient mixing of the gas-liquid two phases.

[0047] In the gas-liquid mixing component provided by the present invention, by setting up two gas-liquid mixing zones and cooperating with the injection tube 10 and the porous material membrane tube 20 to gradually mix the gas-liquid two phases, efficient mixing of the gas-liquid two phases under high flux and high gas-liquid ratio conditions is achieved, effectively overcoming the defect of the existing technology that a large number of micro-nano bubbles cannot be formed under high flux and high gas-liquid ratio conditions.

[0048] In the present invention, the length of the gas-liquid mixing assembly is designed according to the required gas flux and gas-liquid ratio, and the number of the gas-liquid mixing assemblies in parallel is designed according to the required liquid phase flux to meet the needs of high flux and high gas-liquid ratio. In some embodiments, the liquid phase flux of the gas-liquid mixing assembly is 30-1000 L / h, preferably 60-300 L / h; the gas phase flux of the gas-liquid mixing assembly is 30-10000 L / h, preferably 60-1200 L / h; the gas-liquid volume ratio per unit length is 0.1-10m -1 ; preferably 0.5-4m -1 .

[0049] It can be understood that the outer diameter of the gas-liquid mixing assembly is adaptively selected according to actual application, and in some embodiments, the outer diameter of the gas-liquid mixing assembly is 10-50 mm, preferably 20-30 mm.

[0050] In the present application, the injection pipe 10 is based on the Venturi principle, and the throttling section 12 is used to generate intense vortex and turbulent flow in the liquid, and then the gas entering the internal flow passage through the inlet section 13 is mixed efficiently. In an embodiment of the present application, the throttling section 12 is provided with a sieve plate 15, and a plurality of sieve holes 151 are arranged on the sieve plate 15; by arranging the sieve plate 15 with a plurality of sieve holes 151 on the flow path of the liquid, the liquid passing through the throttling section 12 is sufficiently disturbed, and the efficient mixing between the liquid and the gas is promoted.

[0051] In the present application, the diameter and number of the sieve holes 151 can be adaptively selected according to the specific type of the liquid, so that the liquid can generate sufficient vortex and turbulent flow in the inlet section 13, and then the efficient mixing between the liquid and the gas is realized. In some embodiments of the present application, the diameter of the sieve hole 151 is 1-3 mm, and the number of the sieve hole 151 is 1-30, preferably 4-12.

[0052] In some embodiments, the axial direction of the sieve hole 151 is perpendicular to the cross section of the length direction of the injection pipe 10, and the included angle is 90°; at this time, the liquid flowing through the liquid inlet section 11 directly enters the plurality of sieve holes 151 of the sieve plate 15, and after being compressed and accelerated, it enters the inlet section 13 and is released.

[0053] In some embodiments, the axial direction of the sieve hole 151 is perpendicular to the cross section of the length direction of the injection pipe 10, and the included angle is 30°-60°. At this time, the liquid flowing through the liquid inlet section 11 changes direction when entering the plurality of sieve holes 151 of the sieve plate 15, further improving the degree of disturbance of the liquid after flowing through the throttling section 12, and promoting the liquid to mix more fully with the gas entering the internal flow passage through the inlet section 13.

[0054] In the present application, the end of the inlet section 13 close to the throttling section 12 is spaced apart from the liquid outlet end of the throttling section 12; after being compressed and accelerated by the throttling section 12, the liquid generates intense vortex and turbulent flow when leaving the throttling section 12, and the spacing provides a certain space for the vortex and turbulent flow of the liquid. As a preferred, the spacing between the end of the inlet section 13 close to the throttling section 12 and the liquid outlet end of the throttling section 12 is 1-10 mm, more preferably 2-5 mm.

[0055] The gas-liquid mixing assembly provided by the present application is used in the following way: a part of the gas enters the internal flow channel of the injection pipe 10 through the gas inlet section 13 of the injection pipe 10, mixes with the liquid in the internal flow channel to form a gas-liquid mixture. In some embodiments, the pipe wall of the injection pipe 10 at the gas inlet section 13 is provided with a sintered film of metal material, and the average pore size of the sintered film of metal material is 1-50 μm, preferably 1-20 μm. Specifically, the metal material used for preparing the sintered film of metal material is titanium, carbon steel, stainless steel or hastelloy, preferably stainless steel or hastelloy.

[0056] Further, in the present application, another part of the gas enters the internal flow channel through the porous material film pipe 20, and further mixes with the primary gas-liquid mixture formed by the injection pipe 10 to form a further refined gas-liquid mixture. In some embodiments, the base material of the porous material film pipe 20 is selected from one of stainless steel, quartz, alumina, polytetrafluoroethylene, polypropylene and polyethylene, preferably stainless steel or alumina. The pore size of the porous material film pipe 20 is 1-100 μm, preferably 3-10 μm.

[0057] It can be understood that the base material used for preparing the porous material film pipe 20 is pre-formed into a pipe shape, and is subjected to a sintering treatment, so that the porous material film pipe 20 with an internal flow channel and a porous structure of the pipe wall is obtained. In specific use, the liquid flows in the internal flow channel, and the gas penetrates into the internal flow channel through the porous structure on the pipe wall, and mixes with the liquid to form a gas-liquid mixture.

[0058] In some embodiments, a plurality of channels 21 extending along the axial direction of the porous material film pipe 20 are provided on the porous material film pipe 20, and the plurality of channels 21 are combined to form the internal flow channel for the liquid to flow through the porous material film pipe 20. By providing the plurality of channels 21, the contact area between the gas and the liquid is significantly increased, the aeration area is increased, and the gas flux and the gas-liquid ratio are improved.

[0059] In some embodiments, the number of the channels 21 is 9-60, preferably 18-40.

[0060] In some embodiments, a porous structure coating is provided on the inner wall of each of the channels 21; further preferably, the pore size of the porous structure coating is 20-800 nm, preferably 150-600 nm. By providing a nano-scale porous structure coating in the channel 21, the gas penetrates into the internal flow channel through the porous structure coating, so that more micro-bubbles are generated.

[0061] In a specific embodiment of the present application, the porous structure coating is formed by sintering a nano material, and the nano material is an oxide, preferably alumina, zirconia, silicon dioxide or titanium dioxide.

[0062] In the present application, the porous material membrane tube 20 serves as a secondary gas-liquid mixing site, and the gas is introduced into the internal flow channel through the porous structure of the porous material membrane tube 20, and is re-mixed with the primary gas-liquid mixture formed by the jet tube 10, thereby effectively improving the gas-liquid ratio in the gas-liquid mixture.

[0063] In an embodiment of the present application, each of the channels 21 is of an equal-diameter structure, that is, the inner diameter of the channel 21 is always equal from the liquid inlet end to the liquid outlet end of the porous material membrane tube 20. Further, the inner diameter of the channel 21 is 1-6 mm, preferably 2-4 mm.

[0064] In another embodiment of the present application, each of the channels 21 includes an inner hole gradually tapered section 211 and an inner hole gradually expanded section 212 arranged in sequence along the flow direction of the liquid. In some embodiments, the hole diameter of the large-diameter end of the inner hole gradually tapered section 211 is 2 mm, and the hole diameter of the small-diameter end is 1 mm; the hole diameter of the small-diameter end of the inner hole gradually expanded section 212 is 1 mm, and the hole diameter of the large-diameter end is 2 mm. Further, the length ratio of the inner hole gradually expanded section 212 to the inner hole gradually tapered section 211 is 1-5:1, preferably 1.5-2.5:1.

[0065] In some embodiments, the gas-liquid mixing assembly further includes a filler tube 30 arranged at one end of the porous material membrane tube 20 away from the jet tube 10, and the filler tube 30 is filled with filler 31. The gas-liquid mixture formed by the jet tube 10 and the porous material membrane tube 20 is introduced into the filler tube 30 filled with the filler 31, and the filler 31 is used to re-shear and divide the unstable large gas bubbles in the gas-liquid mixture, thereby further forming small gas bubbles.

[0066] It can be understood that the length of the filler tube 30 directly affects the degree of re-shearing and division of the filler 31 on the gas-liquid mixture, but the gas bubbles in the gas-liquid mixture will not be further refined as the length of the filler tube 30 is extended. In some embodiments, the length of the filler tube 30 is 1-30% of the length of the porous material membrane tube 20, preferably 5-10%.

[0067] In some embodiments, the size of the filler 31 is 1-10 mm, preferably 2-5 mm.

[0068] It should be noted that the type of the filler 31 can be known to those skilled in the art, as long as it can achieve the re-shearing and division of the large gas bubbles in the gas-liquid mixture. In some embodiments, the type of the filler 31 is a Pall ring, a Raschig ring, a corrugated mesh, or a hollow spherical shape, preferably a corrugated mesh or a hollow spherical shape.

[0069] The material of the filler 31 can be metal or metal oxide, wherein the metal can be titanium, carbon steel, stainless steel or hastelloy, preferably stainless steel or hastelloy; the metal oxide can be alumina, titanium dioxide, cerium oxide or zirconium oxide, preferably alumina or titanium dioxide.

[0070] The advantages of the gas-liquid mixing assembly provided by the present application are further illustrated by specific examples.

[0071] Example 1

[0072] The present example provides a gas-liquid mixing assembly, which comprises a spray pipe 10, a porous material membrane pipe 20 and a filler pipe 30 coaxially connected; the outer diameter of the spray pipe 10, the porous material membrane pipe 20 and the filler pipe 30 is 30 mm.

[0073] The spray pipe 10 comprises a liquid inlet section 11, a throttling section 12, a gas inlet section 13 and a gas-liquid two-phase development section 14 arranged in sequence along the flow direction of the liquid, and the throttling section 12 is provided with a sieve plate 15, and the sieve plate 15 is provided with 12 sieve holes 151, and the diameter of the sieve holes 151 is 1 mm; the axial direction of the sieve holes 151 and the cross section of the spray pipe 10 perpendicular to the length direction form an angle of 60°. The distance between the end of the gas inlet section 13 close to the throttling section 12 and the liquid outlet end of the throttling section 12 is 3 mm; the pipe wall of the gas inlet section 13 of the spray pipe 10 is provided with a porous stainless steel sintered membrane with an average pore diameter of 10 μm and a length of 2 mm; the length of the gas-liquid two-phase development section 14 is 5 mm; the material of the porous material membrane pipe 20 is alumina, and the base body pore diameter is 5 μm; the porous material membrane pipe 20 is provided with 19 channels 21 extending in the axial direction, and the inner wall of the channel 21 is provided with a porous structure coating, and the material of the porous structure coating is nano-alumina with a pore diameter of 200 nm. Each channel 21 comprises an inner hole gradually reducing section 211 and an inner hole gradually expanding section 212 arranged in sequence along the flow direction of the liquid, and the large pore diameter end of the inner hole gradually reducing section 211 has a pore diameter of 2 mm, and the small pore diameter end has a pore diameter of 1 mm; the small pore diameter end of the inner hole gradually expanding section 212 has a pore diameter of 1 mm, and the large pore diameter end has a pore diameter of 2 mm. The overall length of the porous material membrane pipe 20 is 750 mm, the length of the pore diameter gradually reducing section 211 is 250 mm, and the length of the pore diameter gradually expanding section 212 is 500 mm; the length of the filler pipe 30 is 10 mm, and the filler 31 filled in the filler pipe 30 is a Rasching ring filler with a size of 2 mm.

[0074] Three above-mentioned gas-liquid mixing assemblies are used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 9 L / min.

[0075] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by a bubble imaging monitoring system, and the average bubble size was 70 μm.

[0076] Example 2

[0077] The gas-liquid mixing assembly provided in Example 1 was used to mix benzene and air, wherein the feed flow rate of benzene was 3 L / min, and the feed flow rate of air was 9 L / min.

[0078] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by a bubble imaging monitoring system, and the average bubble size was 150 μm.

[0079] Example 3

[0080] The gas-liquid mixing assembly provided in Example 1 was used to mix ethanol and air, wherein the feed flow rate of ethanol was 9 L / min, and the feed flow rate of air was 9 L / min.

[0081] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by a bubble imaging monitoring system, and the average bubble size was 45 μm.

[0082] Example 4

[0083] The gas-liquid mixing assembly provided in Example 1 was used to mix ethanol and air, wherein the feed flow rate of ethanol was 1.5 L / min, and the feed flow rate of air was 9 L / min.

[0084] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by a bubble imaging monitoring system, and the average bubble size was 180 μm.

[0085] Example 5

[0086] The gas-liquid mixing assembly provided in Example 1 was used to mix ethanol and air, wherein the feed flow rate of ethanol was 15 L / min, and the feed flow rate of air was 60 L / min.

[0087] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by a bubble imaging monitoring system, and the average bubble size was 125 μm.

[0088] Example 6

[0089] The gas-liquid mixing assembly provided in Example 1 was used to mix ethanol and air, wherein the feed flow rate of ethanol was 30 L / min, and the feed flow rate of air was 120 L / min.

[0090] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by a bubble imaging monitoring system, and the average bubble size was 600 μm.

[0091] Example 7

[0092] The gas-liquid mixing assembly used in this example was basically the same as the gas-liquid mixing assembly in Example 1, except that the number of sieve holes 151 on the sieve plate 15 was 30; the rest of the structure was unchanged.

[0093] The gas-liquid mixing assembly was used to mix ethanol and air, wherein the feed flow rate of ethanol was 3 L / min, and the feed flow rate of air was 9 L / min.

[0094] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by a bubble imaging monitoring system, and the average bubble size was 117 μm.

[0095] Example 8

[0096] The gas-liquid mixing assembly used in this example was basically the same as the gas-liquid mixing assembly in Example 1, except that the number of sieve holes 151 on the sieve plate 15 was 1; the rest of the structure was unchanged.

[0097] The gas-liquid mixing assembly was used to mix ethanol and air, wherein the feed flow rate of ethanol was 3 L / min, and the feed flow rate of air was 9 L / min.

[0098] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by a bubble imaging monitoring system, and the average bubble size was 132 μm.

[0099] Example 9

[0100] The gas-liquid mixing assembly used in this example was basically the same as the gas-liquid mixing assembly in Example 1, except that the number of sieve holes 151 on the sieve plate 15 was 1; the rest of the structure was unchanged.

[0101] The gas-liquid mixing assembly was used to mix ethanol and air, wherein the feed flow rate of ethanol was 3 L / min, and the feed flow rate of air was 9 L / min.

[0102] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by a bubble imaging monitoring system, and the average bubble size was 300 μm.

[0103] Example 10

[0104] The gas-liquid mixing assembly used in this embodiment is basically the same as the gas-liquid mixing assembly in Example 1, except that the angle between the axial direction of the sieve hole 151 and the cross section of the injection pipe 10 perpendicular to the length direction is 90°; the rest of the structure remains unchanged.

[0105] The gas-liquid mixing assembly is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min and the feed flow rate of air is 9 L / min.

[0106] The bubble imaging monitoring system was used to statistically analyze the bubble sizes in the gas-liquid mixture flowing out of the end of the filling tube 30 , and the average bubble size was found to be 84 μm.

[0107] Example 11

[0108] The gas-liquid mixing assembly used in this embodiment is basically the same as the gas-liquid mixing assembly in Example 1, except that the length of the air inlet section 13 is 6 mm; the rest of the structure remains unchanged.

[0109] The gas-liquid mixing assembly is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min and the feed flow rate of air is 9 L / min.

[0110] The bubble imaging monitoring system was used to statistically analyze the bubble sizes in the gas-liquid mixture flowing out of the end of the filling tube 30 , and the average bubble size was found to be 122 μm.

[0111] Example 12

[0112] The gas-liquid mixing assembly used in this embodiment is basically the same as the gas-liquid mixing assembly in Example 1, except that the distance between the end of the air inlet section 13 close to the throttling section 12 and the liquid outlet end of the throttling section 12 is 10 mm; the rest of the structure remains unchanged.

[0113] The gas-liquid mixing assembly is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min and the feed flow rate of air is 9 L / min.

[0114] The bubble imaging monitoring system was used to statistically analyze the bubble sizes in the gas-liquid mixture flowing out of the end of the filling tube 30 , and the average bubble size was found to be 153 μm.

[0115] Example 13

[0116] The gas-liquid mixing assembly used in this embodiment is basically the same as the gas-liquid mixing assembly in Example 1, except that the distance between the end of the air inlet section 13 close to the throttling section 12 and the liquid outlet end of the throttling section 12 is 1 mm; the rest of the structure remains unchanged.

[0117] The gas-liquid mixing assembly was used for mixing ethanol and air, wherein the feed flow rate of ethanol was 3 L / min, and the feed flow rate of air was 9 L / min.

[0118] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by the bubble imaging monitoring system, and the average bubble size was 124 μm.

[0119] Example 14

[0120] The gas-liquid mixing assembly used in the example was basically the same as the gas-liquid mixing assembly in Example 1, except that the length of the gas-liquid two-phase development section 14 was 1 mm; the rest of the structure was unchanged.

[0121] The gas-liquid mixing assembly was used for mixing ethanol and air, wherein the feed flow rate of ethanol was 3 L / min, and the feed flow rate of air was 9 L / min.

[0122] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by the bubble imaging monitoring system, and the average bubble size was 85 μm.

[0123] Example 15

[0124] The gas-liquid mixing assembly used in the example was basically the same as the gas-liquid mixing assembly in Example 1, except that the pore size of the porous structure coating on the inner wall of the channel 21 was 500 nm; the rest of the structure was unchanged.

[0125] The gas-liquid mixing assembly was used for mixing ethanol and air, wherein the feed flow rate of ethanol was 3 L / min, and the feed flow rate of air was 9 L / min.

[0126] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by the bubble imaging monitoring system, and the average bubble size was 114 μm.

[0127] Example 16

[0128] The gas-liquid mixing assembly used in the example was basically the same as the gas-liquid mixing assembly in Example 1, except that 12 channels 21 extending in the axial direction were provided on the porous material film tube 20; the rest of the structure was unchanged.

[0129] The gas-liquid mixing assembly was used for mixing ethanol and air, wherein the feed flow rate of ethanol was 3 L / min, and the feed flow rate of air was 9 L / min.

[0130] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by the bubble imaging monitoring system, and the average bubble size was 95 μm.

[0131] Example 17

[0132] The gas-liquid mixing assembly used in this example is basically the same as that in Example 1, except that the large-diameter end of the inner hole tapering section 211 has a hole diameter of 4 mm, and the small-diameter end has a hole diameter of 1 mm; the small-diameter end of the inner hole expanding section 212 has a hole diameter of 1 mm, and the large-diameter end has a hole diameter of 4 mm; the rest of the structure remains unchanged.

[0133] The gas-liquid mixing assembly was used to mix ethanol and air, with the ethanol feed flow rate being 3 L / min and the air feed flow rate being 9 L / min.

[0134] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by the bubble imaging monitoring system, and the average bubble size was 85 μm.

[0135] Example 18

[0136] The gas-liquid mixing assembly used in this example is basically the same as that in Example 1, except that each channel 21 is of an equal-diameter structure with an inner diameter of 1 mm; the rest of the structure remains unchanged.

[0137] The gas-liquid mixing assembly was used to mix ethanol and air, with the ethanol feed flow rate being 3 L / min and the air feed flow rate being 9 L / min.

[0138] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by the bubble imaging monitoring system, and the average bubble size was 90 μm.

[0139] Example 19

[0140] The gas-liquid mixing assembly used in this example is basically the same as that in Example 1, except that the large-diameter end of the inner hole tapering section 211 has a hole diameter of 2 mm, and the small-diameter end has a hole diameter of 0.5 mm; the small-diameter end of the inner hole expanding section 212 has a hole diameter of 0.5 mm, and the large-diameter end has a hole diameter of 2 mm; the rest of the structure remains unchanged.

[0141] The gas-liquid mixing assembly was used to mix ethanol and air, with the ethanol feed flow rate being 3 L / min and the air feed flow rate being 9 L / min.

[0142] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 was statistically analyzed by the bubble imaging monitoring system, and the average bubble size was 121 μm.

[0143] Example 20

[0144] The gas-liquid mixing assembly used in the embodiment is basically the same as the gas-liquid mixing assembly in Embodiment 1, except that the length of the hole-diameter-tapered section 211 is 150 mm, and the length of the hole-diameter-tapered section 212 is 600 mm; the rest of the structure is unchanged.

[0145] The gas-liquid mixing assembly is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 9 L / min.

[0146] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 is statistically analyzed by the bubble imaging monitoring system, and the average bubble size is 156 μm.

[0147] Embodiment 21

[0148] The gas-liquid mixing assembly used in the embodiment is basically the same as the gas-liquid mixing assembly in Embodiment 1, except that the length of the hole-diameter-tapered section 211 is 500 mm, and the length of the hole-diameter-tapered section 212 is 250 mm; the rest of the structure is unchanged.

[0149] The gas-liquid mixing assembly is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 9 L / min.

[0150] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 is statistically analyzed by the bubble imaging monitoring system, and the average bubble size is 184 μm.

[0151] Embodiment 22

[0152] The gas-liquid mixing assembly used in the embodiment is basically the same as the gas-liquid mixing assembly in Embodiment 1, except that the size of the packing 31 in the packing tube 30 is 5 mm; the rest of the structure is unchanged.

[0153] The gas-liquid mixing assembly is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 9 L / min.

[0154] The bubble size in the gas-liquid mixture flowing out of the end of the packing tube 30 is statistically analyzed by the bubble imaging monitoring system, and the average bubble size is 125 μm.

[0155] Embodiment 23

[0156] The gas-liquid mixing assembly used in the embodiment is basically the same as the gas-liquid mixing assembly in Embodiment 1, except that the length of the packing tube 30 is 150 mm; the rest of the structure is unchanged.

[0157] The gas-liquid mixing assembly is used for mixing ethanol and air, wherein the feeding flow rate of ethanol is 3 L / min, and the feeding flow rate of air is 9 L / min.

[0158] The bubble size in the gas-liquid mixture flowing out of the end of the packing pipe 30 is statistically analyzed by a bubble imaging monitoring system, and the average bubble size is 216 μm.

[0159] It can be seen from the above example data that the gas-liquid mixing assembly provided by the present application has excellent gas-liquid mixing effect on different gas-liquid components, and the average size of the gas bubbles after gas-liquid mixing can be controlled to be below 200 μm. It can be seen from the data of examples 1, 3, 4, and 5 that as the ratio of the gas feed amount to the liquid feed amount gradually decreases, the average size of the gas bubbles gradually decreases; it can be seen from the data of examples 5 and 6 that when the remaining structural conditions are unchanged, the overall increase of the gas-liquid two-phase feed amount will cause the average size of the gas bubbles to increase; it can be seen from the data of examples 1, 7, 8, and 9 that increasing the pore size of the sieve hole 151 will cause the average size of the gas bubbles to increase, and increasing or decreasing the number of the sieve hole 151 will cause the average size of the gas bubbles to increase; it can be seen from the data of examples 1 and 10 that setting the included angle between the axial direction of the sieve hole 151 and the cross section of the injection pipe 10 perpendicular to the length direction to be 60° is more conducive to reducing the average size of the gas bubbles than setting it to be 90°; it can be seen from the data of examples 1 and 11 that increasing the length of the gas inlet section 13 is not conducive to reducing the average size of the gas bubbles; it can be seen from the data of examples 1, 12, and 13 that the spacing between the end of the gas inlet section 13 close to the throttling section 12 and the liquid outlet end of the throttling section 12 is too large or too small, which is not conducive to reducing the average size of the gas bubbles; it can be seen from the data of examples 1 and 14 that maintaining a certain length of the gas-liquid two-phase development section 14 is conducive to reducing the average size of the gas bubbles; it can be seen from the data of examples 1 and 15 that the average pore size of the porous structure coating arranged on the inner wall of the channel 21 has a great influence on the average size of the gas bubbles, and when the average pore size of the porous structure coating is large, it is not conducive to reducing the average size of the gas bubbles; it can be seen from the data of examples 1 and 16 that reducing the number of the channel 21 will increase the average size of the gas bubbles; it can be seen from the data of examples 1, 17, 18, and 19 that when the channel 21 is arranged to include the inner hole tapering section 211 and the inner hole expanding section 212, it is conducive to reducing the average size of the gas bubbles to a certain extent, but when the tapering and expanding degree of the inner hole is large, it will instead cause the average size of the gas bubbles to increase; it can be seen from the data of examples 1, 20, and 21 that when the length ratio of the inner hole expanding section to the inner hole tapering section is too large or too small, it is not conducive to reducing the average size of the gas bubbles. The average size of the gas bubbles of example 1 (2:1) is 70 μm, the average size of the gas bubbles of example 20 (4:1) is 156 μm, and the average size of the gas bubbles of example 21 (0.5:1) is 184 μm; it can be seen from the data of examples 1, 22, and 23 that too large size of the filler 31 and too long length of the filler pipe 30 are also not conducive to reducing the average size of the gas bubbles.

[0160] In combination Figure 3As shown, the second aspect of the application provides an application of the aforementioned gas-liquid mixing assembly in cumene oxidation, the gas-liquid mixing assembly is built-in in a reactor 1 for cumene oxidation, a plurality of the gas-liquid mixing assemblies are arranged in parallel, and the plurality of the gas-liquid mixing assemblies are used to mix gas and liquid participating in the cumene oxidation reaction to form a gas-liquid mixture; the gas is oxygen-containing gas, and the liquid is liquid containing cumene or oxidation liquid containing cumene hydroperoxide.

[0161] In some embodiments, the catalyst active component is loaded in the internal flow channel at the porous material membrane tube 20; or a filler 31 is arranged at the outlet of the porous material membrane tube 20, and the catalyst active component is loaded on the filler 31; or a filler 31 made of a material containing the catalyst active component is arranged at the outlet of the porous material membrane tube 20.

[0162] By arranging the catalyst active component, the gas raw material and the liquid raw material can be reacted in the process of forming the gas-liquid mixture, and the reaction efficiency of the gas-liquid two phases is further improved.

[0163] Further, the catalyst active component is selected from oxides of at least one of copper, magnesium, cobalt, manganese, nickel, chromium, zinc, iron, silver and gold; it can be understood that the loading amount of the catalyst active component is arranged according to the requirements of specific reactions, and in some embodiments, the loading amount of the catalyst active component is 0.01%-10% of the weight of the porous material membrane tube 20 or the filler 31, preferably 0.05%-5%.

[0164] In the application, the catalyst active component can be loaded in any appropriate form, for example, the loading mode of the catalyst active component is impregnation, vacuum coating, chemical vapor deposition or atomic layer deposition.

[0165] The application of the gas-liquid mixing assembly provided by the application in cumene oxidation is further described below through a specific application example.

[0166] Application Example 1

[0167] Three gas-liquid mixing assemblies provided by the aforementioned embodiment 1 are built-in in a reactor 1 for cumene oxidation, and the three gas-liquid mixing assemblies are used to mix gas and liquid participating in the cumene oxidation reaction to form a gas-liquid mixture.

[0168] On each gas-liquid mixing assembly, the CuO active component is loaded on the porous material membrane tube 20 and the filler 31. The loading amount of the catalyst active component on the porous material membrane tube 20 is 1% of the mass of the porous material membrane tube 20, and the loading amount of the catalyst active component on the filler 31 is 1% of the mass of the filler 31.

[0169] The gas is air (oxygen concentration 21% (by volume percentage)) and the liquid is cumene hydrogen peroxide with a concentration of 14wt%; after 6h, the sample is analyzed by iodometric method to analyze the concentration of cumene hydrogen peroxide, and other by-products such as acetophenone and dimethyl benzyl alcohol are analyzed by liquid chromatography. The analysis results are summarized in Table 1.

[0170] Application Example 2

[0171] This application example is basically the same as the implementation of application example 1, except that the gas is replaced by oxygen-enriched air (oxygen concentration 50% (by volume percentage)); the rest is unchanged, and the final analysis results are summarized in Table 1.

[0172] Application Example 3

[0173] This application example is basically the same as the implementation of application example 1, except that the liquid feed rate is controlled to be 9L / min; the rest is unchanged, and the final analysis results are summarized in Table 1.

[0174] Application Example 4

[0175] This application example is basically the same as the implementation of application example 1, except that the liquid feed rate is controlled to be 1.5L / min; the rest is unchanged, and the final analysis results are summarized in Table 1.

[0176] Application Example 5

[0177] This application example is basically the same as the implementation of application example 1, except that the active component of the catalyst on the porous material membrane tube 20 is loaded with Cu, and the loading amount is 3% of the mass of the porous material membrane tube 20; the active component of the catalyst on the filler 31 is loaded with Cu metal, and the loading amount is 3% of the mass of the filler 31; the rest is unchanged, and the final analysis results are summarized in Table 1.

[0178] Application Example 6

[0179] This application example is basically the same as the implementation of application example 1, except that the active component of the catalyst is replaced by MgO; the rest is unchanged, and the final analysis results are summarized in Table 1.

[0180] Comparative Example 1

[0181] This comparative example is basically the same as the implementation of application example 1, except that no active component of the catalyst is loaded on the porous material membrane tube 20 and the filler 31; the rest is unchanged, and the final analysis results are summarized in Table 1.

[0182] Comparative Example 2

[0183] This comparative example uses a traditional aeration method, and the final analysis results are summarized in Table 1.

[0184] Table 1:

[0185] CHP production rate / (% / h) CHP selectivity / % Acetophenone selectivity / % Dimethyl benzyl alcohol / % Example 1 4.6 95.8 3.4 0.8 Example 2 5.8 90.4 6.5 3.1 Example 3 4.9 96.2 2.3 1.5 Example 4 4.3 94.1 4.2 1.7 Example 5 6.2 92.2 5.6 2.2 Example 6 5.5 93.5 4.7 1.8 Comparative Example 1 3.7 98.5 1.1 0.4 Comparative Example 2 2.1 92.1 4.8 3.1

[0186] It can be seen from the above test data that the reaction rate can be improved and the selectivity of CHP can be improved by the gas-liquid mixing assembly. The rich oxygen condition can improve the reaction rate, but is not conducive to the selectivity of CHP. The mixing effect is good when the gas-liquid ratio is reduced, which can improve the reaction rate and is conducive to improving the selectivity of CHP; the oxidation rate is reduced and the selectivity of CHP is not conducive when the gas-liquid ratio is increased.

[0187] The preferred embodiments of the present application are described in detail above in combination with the drawings, but the present application is not limited thereto. Within the technical concept of the present application, various simple modifications can be made to the technical solutions of the present application. In order to avoid unnecessary repetition, various possible combination modes are not described again in the present application. However, these simple modifications and combinations should also be regarded as the disclosed content of the present application and belong to the protection scope of the present application.

Claims

1. A gas-liquid mixing component, characterized in that: The invention comprises an injection pipe (10) and a porous material membrane tube (20), wherein the injection pipe (10) and the porous material membrane tube (20) are coaxially connected to form a continuous internal flow channel for liquid to flow through, and the injection pipe (10) comprises a liquid inlet section (11), a throttling section (12), an air inlet section (13) and a gas-liquid two-phase development section (14) arranged in sequence along the flow direction of the liquid, the flow channel cross-sectional area of ​​the liquid inlet section (11) is equal to that of the air inlet section (13) and is larger than the flow channel cross-sectional area of ​​the throttling section (12), and the air inlet section (13) and the porous material membrane tube (20) are respectively provided with a pore structure for introducing gas into the internal flow channel.

2. The gas-liquid mixing assembly according to claim 1, characterized in that: The liquid phase flux of the gas-liquid mixing component is 30-1000 L / h; The gas phase flux of the gas-liquid mixing component is 30-10000 L / h; The gas-liquid volume ratio per unit length is 0.1-10m -1 .

3. The gas-liquid mixing assembly according to claim 1, characterized in that: A sieve plate (15) is provided at the throttling section (12), and a plurality of sieve holes (151) are provided on the sieve plate (15).

4. The gas-liquid mixing assembly according to claim 1, characterized in that: One end of the air inlet section (13) close to the throttling section (12) is arranged to be spaced apart from the liquid outlet end of the throttling section (12).

5. The gas-liquid mixing assembly according to claim 1, characterized in that: The tube wall of the injection tube (10) located in the air inlet section (13) is configured as a porous metal sintered film.

6. The gas-liquid mixing assembly according to claim 1, characterized in that: The base material of the porous material membrane tube (20) is selected from one of stainless steel, quartz, alumina, polytetrafluoroethylene, polypropylene, and polyethylene.

7. The gas-liquid mixing assembly according to claim 1, characterized in that: The porous material membrane tube (20) is provided with a plurality of channels (21) extending along its axial direction, and the plurality of channels (21) are combined to form the internal flow channel for the liquid to flow through the porous material membrane tube (20).

8. The gas-liquid mixing assembly according to claim 7, characterized in that: A porous structure coating is provided on the inner wall of each channel (21).

9. The gas-liquid mixing assembly according to claim 7, characterized in that: Each of the channels (21) is of a constant diameter structure, and the inner diameter of the channel (21) is 1-6 mm; Alternatively, each of the channels (21) comprises an inner bore tapered section (211) and an inner bore gradually expanding section (212) sequentially arranged along the flow direction of the liquid, and the length ratio of the inner bore gradually expanding section (212) to the inner bore tapered section (211) is 1-5:

1.

10. The gas-liquid mixing assembly according to any one of claims 1 to 9, characterized in that: The gas-liquid mixing assembly further comprises a filling tube (30), wherein the filling tube (30) is arranged at one end of the porous material membrane tube (20) away from the injection tube (10), and the filling tube (30) is filled with a filler (31).

11. The gas-liquid mixing assembly according to claim 10, characterized in that: The length of the filling tube (30) is 1-30% of the length of the porous material membrane tube (20).

12. The gas-liquid mixing assembly according to claim 10, characterized in that: The size of the filler (31) is 1-10 mm.

13. Use of the gas-liquid mixing assembly according to any one of claims 1 to 12 in cumene oxidation, characterized in that: The gas-liquid mixing assembly is built into the cumene oxidation reactor (1), and a plurality of the gas-liquid mixing assemblies are arranged in parallel. The plurality of gas-liquid mixing assemblies are used to mix the gas and liquid participating in the cumene oxidation reaction to form a gas-liquid mixture; The gas is an oxygen-containing gas, and the liquid is a liquid containing cumene or an oxidizing liquid containing cumene hydroperoxide.

14. Use of the gas-liquid mixing assembly according to claim 13 in cumene oxidation, characterized in that: The internal flow channel located at the porous material membrane tube (20) is loaded with catalyst active components; or A filler (31) is provided at the outlet of the porous material membrane tube (20), and the filler (31) is loaded with catalyst active components; or A filler (31) made of a material containing catalyst active components is provided at the outlet of the porous material membrane tube (20).

15. Use of the gas-liquid mixing assembly according to claim 14 in cumene oxidation, characterized in that: The catalyst active component is selected from at least one oxide of copper, magnesium, cobalt, manganese, nickel, chromium, zinc, iron, silver and gold.

16. Use of the gas-liquid mixing assembly according to claim 15 in cumene oxidation, characterized in that: The loading amount of the catalyst active component is 0.01%-10% of the weight of the porous material membrane tube (20) or the filler (31).

17. Use of the gas-liquid mixing assembly according to claim 15 in cumene oxidation, characterized in that: The catalyst active components are loaded in a manner of impregnation, vacuum coating, chemical vapor deposition or atomic layer deposition.

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