Gas-liquid mixing assembly and application thereof in cumene oxidation

Abstract

The invention relates to the technical field of chemical equipment, and discloses a gas-liquid mixing assembly and application thereof in cumene oxidation, the gas-liquid mixing assembly comprises an injection pipe and a porous material membrane pipe, the injection pipe and the porous material membrane pipe are coaxially connected to form a continuous internal flow channel for liquid to flow through, the injection pipe comprises a liquid inlet section, a throttling section, a gas inlet section and a gas-liquid two-phase development section which are sequentially arranged in the flowing direction of liquid, the flow channel sectional area of the liquid inlet section and the flow channel sectional area of the gas inlet section are equal and larger than the flow channel sectional area of the throttling section, and pore structures are arranged on the gas inlet section and the porous material membrane pipe correspondingly and used for introducing gas into internal flow channels; according to the invention, two gas-liquid mixing areas are arranged and matched with the injection pipe and the porous material membrane pipe to gradually mix a gas phase and a liquid phase, so that efficient mixing of the gas phase and the liquid phase under the conditions of high flux and high gas-liquid ratio is realized, and the defect that a large number of micro-nano bubbles cannot be formed under the conditions of high flux and high gas-liquid ratio in the prior art is effectively overcome.

Description

Technical Field

[0001] The present invention relates to the technical field of chemical equipment, in particular to a gas-liquid mixing component and application thereof in cumene oxidation. Background Art

[0002] Multiphase reactions such as hydrogenation and oxidation are widely used in process industries, such as benzene hydrogenation, PX air oxidation, and diesel fixed-bed hydrogenation. 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 interphase area between gas and liquid, and between gas, liquid and solid is too small. Taking the traditional bubbling air oxidation reactor as an example, since the bubble diameter is generally between 5-30mm, under normal pressure conditions, the interphase area between gas and liquid phase is usually 20-300m 2 ·m -3 , and in most cases less than 100m 2 ·m -3 Therefore, in industrial practice, people usually adopt methods such as increasing the gas circulation volume or adding internal components of the reactor to enhance mass transfer and improve the reaction, but the effect is very limited.

[0003] The principle of microinterface enhanced reaction technology (MIR) is to efficiently control the geometric scale of gas-liquid, gas-liquid-liquid, and gas-liquid-solid interfaces from milli-centimeter level to micrometer level, which greatly increases the interfacial area by orders of magnitude. When the bubbles are gradually reduced from several millimeters to micrometer level, the gas-liquid mass transfer rate and reaction rate will be significantly enhanced, thereby doubling the efficiency of the chemical production process, significantly reducing energy consumption and material consumption, and improving safety and environmental protection performance. The key to microinterface enhanced reaction technology lies in the enhanced mixing between multiple phases, such as the enhanced mixing of gas and liquid phases. Therefore, the preparation of microbubbles is particularly important. Existing technologies have gradually developed microbubble preparation methods suitable for different occasions. Specifically, according to the generation method of microbubbles, they are mainly divided into the following types: (1) shearing and breaking bubbles, such as Venturi-type microbubble generators; (2) pressure reduction or temperature increase bubbles, such as pressure dissolution microbubble generators; (3) ultrasonic bubble formation; (4) microporous bubble formation, such as microporous plastics, rubber and ceramic tubes.

[0004] In the existing technology, gas-liquid two-phase enhanced mixing technology is mainly used in water treatment, aquaculture, and medicine, and is less used in chemical production. The reason is that it is difficult to scale up the micromixer. One of the core problems is how to prepare microbubbles on a large scale and with high throughput. Another problem is that the preparation of microbubbles under high gas-liquid ratio conditions has certain technical limitations. Summary of the Invention

[0005] The purpose of the present invention is to overcome the problem of poor gas-liquid two-phase mixing efficiency under high flux and high gas-liquid ratio conditions in the prior art, and to provide a gas-liquid mixing component and its application in isopropylbenzene oxidation, which can effectively improve the gas-liquid two-phase mixing efficiency under high flux and high gas-liquid ratio conditions.

[0006] In order to achieve the above-mentioned objectives, the first aspect of the present invention provides a gas-liquid mixing component, including an injection pipe and a porous material membrane tube, the injection pipe and the porous material membrane tube are coaxially connected to form a continuous internal flow channel for liquid to flow through, the injection pipe includes a liquid inlet section, a throttling section, an air 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 air inlet section and is larger than the flow channel cross-sectional area of ​​the throttling section, and the air inlet section and the porous material membrane tube are respectively provided with pore structures for introducing gas into the internal flow channel.

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

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

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

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

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

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

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

[0014] Preferably, one end of the air 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 air 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 tube wall of the injection tube located in the air inlet section is configured as a porous metal sintered film, and the average pore size of the metal sintered film is 1-50 μm, preferably 1-20 μm.

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

[0018] Preferably, the pore size of the porous material membrane tube is 1-100 μm, preferably 3-10 μm.

[0019] Preferably, the porous material membrane tube is provided with a plurality of channels extending along its axial direction, and the plurality of channels are combined to form the internal flow channel for the liquid to flow through the porous material membrane tube.

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

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

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

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

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

[0025] Preferably, the gas-liquid mixing assembly further comprises a filling tube, which is arranged at one end of the porous material membrane tube away from the injection tube, and is filled with a filler.

[0026] Preferably, the length of the filling tube is 1-30%, preferably 5-10%, of the length of the porous material membrane tube.

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

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

[0029] Preferably, the internal flow channel located at the porous material membrane tube is loaded with catalyst active components; or

[0030] A filler is provided at the outlet of the porous material membrane tube, and the filler is loaded with catalyst active components; or

[0031] A filler made of a material containing catalyst active components is arranged at the outlet of the porous material membrane tube.

[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%-10% of the weight of the porous material membrane tube or the filler, preferably 0.05%-5%.

[0034] Preferably, the catalyst active components are supported by impregnation, vacuum coating, chemical vapor deposition or atomic layer deposition.

[0035] Compared with the prior art, when the gas-liquid mixing component provided by the present invention is used, the liquid enters from the end of the injection tube away from the porous material membrane tube and passes through the internal flow channel of the injection tube and the porous material membrane tube in turn, and the gas enters the internal flow channel through the air inlet section of the injection tube and the porous material membrane tube, mixes with the liquid to form a gas-liquid mixture.

[0036] 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 to a liquid inlet section, a throttling section, an air inlet section and a gas-liquid two-phase development section connected in sequence, in the process of the liquid entering the throttling section through the liquid inlet section, 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, the pressure inside the liquid suddenly drops sharply, causing the liquid to quickly diffuse to the surrounding area, resulting in violent eddy currents and turbulence. This part of the liquid and the gas entering through the air inlet section 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, 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, and the gas entering the internal flow channel through the tube wall of the porous material membrane tube 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 increase the bubble density in the gas-liquid mixture, thereby promoting sufficient mixing of the gas-liquid two phases.

[0037] In the gas-liquid mixing component provided by the present invention, by setting up two gas-liquid mixing zones and coordinating the gradual mixing of the gas-liquid two phases with the injection tube and the porous material membrane tube, 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. BRIEF DESCRIPTION OF THE DRAWINGS

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

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

[0040] Figure 3 This is a schematic diagram of the application of a gas-liquid mixing assembly provided by the present invention in the oxidation of cumene;

[0041] Description of Reference Numerals

[0042] 1. Reactor; 10. Injection pipe; 11. Liquid inlet section; 12. Throttling section; 13. Air inlet section; 14. Gas-liquid two-phase development section; 15. Sieve plate; 151. Sieve hole; 20. Porous material membrane tube; 21. Channel; 211. Inner hole gradually contracting section; 212. Inner hole gradually expanding section; 30. Filling tube; 31. Filling. DETAILED DESCRIPTION

[0043] The following describes the specific embodiments of the present invention in detail with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are only used to illustrate and explain the present invention and are not intended to limit the present invention.

[0044] Combine Figure 1 and Figure 2 As shown, the present invention provides a gas-liquid mixing component, including an injection pipe 10 and a porous material membrane tube 20, 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, the injection pipe 10 includes 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.

[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 is understandable that the outer diameter of the gas-liquid mixing component is adaptively selected according to actual applications. In some embodiments, the outer diameter of the gas-liquid mixing component is 10-50 mm, preferably 20-30 mm.

[0050] In the present invention, the injection pipe 10 is based on the Venturi principle, utilizing the throttling section 12 to generate intense eddies and turbulence in the liquid, thereby achieving efficient mixing with the gas entering the internal flow channel through the air inlet section 13. In one embodiment of the present invention, a sieve plate 15 is provided at the throttling section 12, and the sieve plate 15 is provided with a plurality of sieve holes 151. By providing the sieve plate 15 with a plurality of sieve holes 151 in the liquid flow path, the liquid passing through the throttling section 12 is fully disturbed, thereby promoting efficient mixing between the liquid and the gas.

[0051] In the present invention, the diameter and number of the sieve holes 151 can be adaptively selected according to the specific type of the liquid, so as to enable the liquid to generate sufficient eddy currents and turbulence in the air inlet section 13, thereby achieving efficient mixing of the liquid and gas. In some embodiments of the present invention, the diameter of the sieve holes 151 is 1-3 mm, and the number of the sieve holes 151 is 1-30, preferably 4-12.

[0052] In some embodiments, 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°; at this time, the liquid flowing through the liquid inlet section 11 directly enters the multiple sieve holes 151 of the sieve plate 15, and after being compressed and accelerated, enters the air inlet section 13 for release.

[0053] In some embodiments, the angle between the axis of the sieve holes 151 and the cross-section of the injection pipe 10 perpendicular to its length is 30°-60°. In this case, the liquid flowing through the liquid inlet section 11 changes direction upon entering the multiple sieve holes 151 of the sieve plate 15, further increasing the turbulence of the liquid after passing through the throttling section 12 and promoting more complete mixing of the liquid with the gas entering the internal flow channel through the gas inlet section 13.

[0054] In the present invention, the end of the air inlet section 13 near the throttle section 12 is spaced apart from the liquid outlet end of the throttle section 12. Due to the compression and acceleration of the throttle section 12, the liquid generates intense eddy currents and turbulence upon leaving the throttle section 12. This spacing provides space for these eddy currents and turbulence. Preferably, the spacing between the end of the air inlet section 13 near the throttle section 12 and the liquid outlet end of the throttle section 12 is 1-10 mm, more preferably 2-5 mm.

[0055] When the gas-liquid mixing assembly provided by the present invention is in use, a portion of the gas enters the internal flow channel of the injection tube 10 through the air inlet section 13 of the injection tube 10, mixing with the liquid in the internal flow channel to form a gas-liquid mixture. In some embodiments, the tube wall of the injection tube 10 located at the air inlet section 13 is configured as a porous metal sintered membrane, and the average pore size of the metal sintered membrane is 1-50μm, preferably 1-20μm. Specifically, the metal material used to prepare the metal sintered membrane is titanium, carbon steel, stainless steel, or Hastelloy alloy, preferably stainless steel or Hastelloy alloy.

[0056] Furthermore, in the present invention, another portion of the gas enters the internal flow channel through the porous material membrane tube 20 and further mixes with the primary gas-liquid mixture formed by the injection tube 10 to form a further refined gas-liquid mixture. In some embodiments, the base material of the porous material membrane tube 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 membrane tube 20 is 1-100 μm, preferably 3-10 μm.

[0057] It can be understood that by preforming the base material used to prepare the porous material membrane tube 20 into a tube shape and combining it with a sintering treatment, a porous material membrane tube 20 with an internal flow channel and a porous tube wall structure can be obtained. During 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 tube wall, mixes with the liquid, and forms a gas-liquid mixture.

[0058] In some embodiments, 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; by providing the plurality of channels 21, the contact area between the gas and the liquid is significantly improved, 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 coating is provided on the inner wall of each channel 21. Further preferably, the porous coating has a pore size of 20-800 nm, preferably 150-600 nm. By providing a nanoscale porous coating in the channel 21, gas penetrates through the porous coating into the internal flow channel, promoting the generation of more tiny bubbles.

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

[0062] In the present invention, the porous material membrane tube 20 serves as a place for secondary gas-liquid mixing. Gas is introduced into the internal flow channel through the porous structure tube wall of the porous material membrane tube 20, and then mixed with the primary gas-liquid mixture formed by the injection tube 10, thereby effectively improving the gas-liquid ratio in the gas-liquid mixture.

[0063] In one embodiment of the present invention, each channel 21 is of a constant diameter structure, that is, the inner diameter of the channel 21 is always the same from the liquid inlet end to the liquid outlet end of the porous material membrane tube 20. Furthermore, the inner diameter of the channel 21 is 1-6 mm, preferably 2-4 mm.

[0064] In another embodiment of the present invention, each channel 21 includes a tapered inner section 211 and a widening inner section 212, arranged sequentially along the flow direction of the liquid. In some embodiments, the diameter of the large-diameter end of the tapered inner section 211 is 2 mm, and the diameter of the small-diameter end is 1 mm; the diameter of the small-diameter end of the widening inner section 212 is 1 mm, and the diameter of the large-diameter end is 2 mm. Furthermore, the length ratio of the widening inner section 212 to the tapered inner section 211 is 1-5:1, preferably 1.5-2.5:1.

[0065] In some embodiments, the gas-liquid mixing assembly further includes a filling tube 30, which is disposed at one end of the porous material membrane tube 20 away from the injection tube 10 and is filled with a filler 31. The gas-liquid mixture formed by the injection tube 10 and the porous material membrane tube 20 is introduced into the filling tube 30 filled with the filler 31, and the filler 31 is used to shear and split unstable large bubbles in the gas-liquid mixture again to further form tiny bubbles.

[0066] It is understood that the length of the filling tube 30 directly affects the degree to which the filler 31 re-shears and divides the gas-liquid mixture, but the bubbles in the gas-liquid mixture are not further refined as the length of the filling tube 30 increases. In some embodiments, the length of the filling 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 any type known to those skilled in the art, as long as it can achieve re-shearing and segmenting of large bubbles in the gas-liquid mixture. In some embodiments, the filler 31 is a Pall ring, a Raschig ring, a corrugated mesh, or a hollow sphere, preferably a corrugated mesh or a hollow sphere.

[0069] The filler 31 may be made of metal or metal oxide, wherein the metal may be titanium, carbon steel, stainless steel or Hastelloy, preferably stainless steel or Hastelloy; the metal oxide may be aluminum oxide, titanium dioxide, cerium oxide, zirconium oxide, preferably aluminum oxide or titanium dioxide.

[0070] The advantages of the gas-liquid mixing assembly provided by the present invention are further illustrated below through specific embodiments.

[0071] Example 1

[0072] This embodiment provides a gas-liquid mixing assembly, including a coaxially connected injection pipe 10, a porous material membrane tube 20 and a filling tube 30; the outer diameters of the injection pipe 10, the porous material membrane tube 20 and the filling tube 30 are 30 mm.

[0073] The injection pipe 10 includes a liquid inlet section 11, a throttling section 12, an air inlet section 13 and a gas-liquid two-phase development section 14, which are arranged in sequence along the flow direction of the liquid. A sieve plate 15 is provided at the throttling section 12, and 12 sieve holes 151 are provided on the sieve plate 15. The aperture of the sieve hole 151 is 1 mm; 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 60°. 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 3mm; the wall of the injection tube 10 located in the air inlet section 13 is set as a porous stainless steel sintered membrane with an average pore size of 10μm and a length of 2mm; the length of the gas-liquid two-phase development section 14 is 5mm; the material of the porous material membrane tube 20 is alumina, and the base pore size is 5μm; the porous material membrane tube 20 is provided with 19 channels 21 extending along the axial direction, and the inner wall of the channel 21 is provided with a porous structure coating made of nano-alumina with a pore size of 200nm. Each channel 21 includes an inner pore tapering section 211 and an inner pore expanding section 212 arranged in sequence along the flow direction of the liquid. The pore size of the large pore end of the inner pore tapering section 211 is 2mm, and the pore size of the small pore end is 1mm; the pore size of the small pore end of the inner pore expanding section 212 is 1mm, and the pore size of the large pore end is 2mm. The overall length of the porous material membrane tube 20 is 750 mm, the length of the aperture tapering section 211 is 250 mm, and the length of the aperture expanding section 212 is 500 mm; the length of the filling tube 30 is 10 mm, and the filler 31 filled in the filling tube 30 is a Raschig ring filler with a size of 2 mm.

[0074] Three parallel gas-liquid mixing assemblies were 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.

[0075] 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 70 μm.

[0076] Example 2

[0077] Benzene and air were mixed using the gas-liquid mixing assembly provided in Example 1, 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 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 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 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 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 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 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 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 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 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 600 μm.

[0091] Example 7

[0092] 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 aperture of the sieve hole 151 on the sieve plate 15 is 2 mm; the rest of the structure remains unchanged.

[0093] 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.

[0094] 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 117 μm.

[0095] Example 8

[0096] 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 number of sieve holes 151 on the sieve plate 15 is 30; the rest of the structure remains unchanged.

[0097] 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.

[0098] 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 132 μm.

[0099] Example 9

[0100] 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 number of sieve holes 151 on the sieve plate 15 is 1; the rest of the structure remains unchanged.

[0101] 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.

[0102] 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 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 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.

[0118] 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 124 μm.

[0119] Example 14

[0120] 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 gas-liquid two-phase development section 14 is 1 mm; the rest of the structure remains unchanged.

[0121] 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.

[0122] 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 85 μm.

[0123] Example 15

[0124] 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 pore size of the porous structure coating on the inner wall of the channel 21 is 500 nm; the rest of the structure remains unchanged.

[0125] 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.

[0126] 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 114 μm.

[0127] Example 16

[0128] The gas-liquid mixing assembly used in this embodiment is basically the same as the gas-liquid mixing assembly in Example 1, except that 12 channels 21 extending in the axial direction are provided on the porous material membrane tube 20; the rest of the structure remains unchanged.

[0129] 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.

[0130] 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 95 μm.

[0131] Example 17

[0132] 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 aperture of the large-aperture end of the inner hole tapering section 211 is 4 mm, and the aperture of the small-aperture end is 1 mm; the aperture of the small-aperture end of the inner hole expanding section 212 is 1 mm, and the aperture of the large-aperture end is 4 mm; the rest of the structure remains unchanged.

[0133] 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.

[0134] 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 85 μm.

[0135] Example 18

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

[0137] 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.

[0138] 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 90 μm.

[0139] Example 19

[0140] 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 aperture of the large-aperture end of the inner hole tapering section 211 is 2 mm, and the aperture of the small-aperture end is 0.5 mm; the aperture of the small-aperture end of the inner hole expanding section 212 is 0.5 mm, and the aperture of the large-aperture end is 2 mm; the rest of the structure remains unchanged.

[0141] 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.

[0142] 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 121 μm.

[0143] Example 20

[0144] 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 aperture tapering section 211 is 150 mm, and the length of the aperture expanding section 212 is 600 mm; the rest of the structure remains 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 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 156 μm.

[0147] Example 21

[0148] 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 aperture tapering section 211 is 500 mm, and the length of the aperture expanding section 212 is 250 mm; the rest of the structure remains 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 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 184 μm.

[0151] Example 22

[0152] 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 size of the filler 31 in the filler tube 30 is 5 mm; the rest of the structure remains 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 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 125 μm.

[0155] Example 23

[0156] 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 filling tube 30 is 150 mm; the rest of the structure remains unchanged.

[0157] 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.

[0158] 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 216 μm.

[0159] From the data of the above embodiments, it can be seen that the gas-liquid mixing assembly provided by the present invention has excellent gas-liquid mixing effect for different gas-liquid components, and specifically can control the average size of bubbles after gas-liquid mixing to be below 200 μm. Combined with the data of Examples 1, 3, 4, and 5, it can be seen that as the ratio of the gas feed amount to the liquid feed amount gradually decreases, the average size of the bubbles also gradually decreases; Combined with the data of Examples 5 and 6, it can be seen that when the other structural conditions remain unchanged, the overall increase in the gas-liquid two-phase feed amount will lead to an increase in the average size of the bubbles; Combined with the data of Examples 1, 7, 8, and 9, it can be seen that increasing the aperture of the sieve hole 151 will lead to an increase in the average size of the bubbles, and increasing and decreasing the number of sieve holes 151 will lead to an increase in the average size of the bubbles; Combined with the data of Examples 1 and 10, it can be seen that setting 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 to 60° is more conducive to reducing the average size of the bubbles than setting it to 90°; Combined with the data of Examples 1 and 11, it can be seen that increasing the length of the air inlet section 13 is not conducive to reducing the average size of the bubbles; Combined with the data of Examples 1, 12, and 13, it can be seen 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 too large. or too small, is not conducive to reducing the average size of bubbles; combined with the data of Examples 1 and 14, it can be seen that maintaining a certain length of the gas-liquid two-phase development section 14 is conducive to reducing the average size of bubbles; combined with the data of Examples 1 and 15, it can be seen that the average pore size of the porous structure coating provided on the inner wall of the channel 21 has a greater influence on the average size of bubbles, and when the average pore size of the porous structure coating is larger, it is not conducive to reducing the average size of bubbles; combined with the data of Examples 1 and 16, it can be seen that reducing the number of channels 21 will increase the average size of bubbles; combined with the data of Examples 1, 17, 18, and 19, it can be seen that when the channel 21 is set to include an inner pore tapering section 211 and an inner pore expanding section 212, it is conducive to reducing the average size of bubbles to a certain extent. However, when the degree of inner pore tapering and expanding is large, it will cause the average size of bubbles to increase; combined with the data of Examples 1, 20, and 21, it can be seen that the ratio of the length of the inner pore expansion section to the inner pore tapering section is too large or too small, which is not conducive to reducing the average size of bubbles. The average bubble size of Example 1 (2:1) is 70 μm, the average bubble size of Example 20 (4:1) is 156 μm, and the average bubble size of Example 21 (0.5:1) is 184 μm. Combining the data of Examples 1, 22, and 23, it can be seen that the size of the filler 31 is too large and the length of the filler tube 30 is too long, which is not conducive to reducing the average size of the bubbles.

[0160] Combine Figure 3As shown, the second aspect of the present invention provides an application of the aforementioned gas-liquid mixing component in the oxidation of isopropylbenzene, wherein the gas-liquid mixing component is built into the reactor 1 for the oxidation of isopropylbenzene, and a plurality of the gas-liquid mixing components are arranged in parallel, and the plurality of gas-liquid mixing components are used to mix the gas and liquid participating in the isopropylbenzene oxidation reaction to form a gas-liquid mixture; the gas is an oxygen-containing gas, and the liquid is a liquid containing isopropylbenzene or an oxidation liquid containing isopropylbenzene hydrogen peroxide.

[0161] In some embodiments, 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.

[0162] By providing the active components of the catalyst, the gas raw material and the liquid raw material can react in the process of forming the gas-liquid mixture, further improving the reaction efficiency of the gas-liquid two-phase.

[0163] Furthermore, the catalyst active component is selected from at least one oxide of copper, magnesium, cobalt, manganese, nickel, chromium, zinc, iron, silver, and gold; it is understandable that the loading amount of the catalyst active component is set according to the requirements of the specific reaction. 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 present invention, the catalyst active components can be supported in any appropriate form. For example, the catalyst active components can be supported by impregnation, vacuum coating, chemical vapor deposition or atomic layer deposition.

[0165] The application of the gas-liquid mixing assembly provided by the present invention in the oxidation of cumene is further illustrated below through specific application examples.

[0166] Application Example 1

[0167] The three gas-liquid mixing assemblies provided in the above-mentioned embodiment 1 are built into the reactor 1 for cumene oxidation, and the three gas-liquid mixing assemblies are used to mix the gas and liquid involved in the cumene oxidation reaction to form a gas-liquid mixture;

[0168] In each gas-liquid mixing assembly, the porous membrane tube 20 and the filler 31 are both loaded with CuO active components. The catalytic active component loading on the porous membrane tube 20, calculated as Cu, is 1% of the mass of the porous membrane tube 20; the catalytic active component loading on the filler 31, calculated as Cu, is 1% of the mass of the filler 31.

[0169] The gas was air (oxygen concentration 21% by volume), and the liquid was cumene hydroperoxide at a concentration of 14 wt%. After 6 hours, samples were taken for cumene hydroperoxide concentration analysis using iodine titration, and other byproducts, such as acetophenone and dimethylbenzyl alcohol, were analyzed by liquid chromatography. The results are summarized in Table 1.

[0170] Application Example 2

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

[0172] Application Example 3

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

[0174] Application Example 4

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

[0176] Application Example 5

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

[0178] Application Example 6

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

[0180] Comparative Example 1

[0181] The implementation of this comparative example is basically the same as that of Application Example 1, except that no catalyst active components are loaded on the porous material membrane tube 20 and the filler 31. The rest remains unchanged. The final analysis results are summarized in Table 1.

[0182] Comparative Example 2

[0183] This comparative example adopts the 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 / % Dimethylbenzyl alcohol / % Application Example 1 4.6 95.8 3.4 0.8 Application Example 2 5.8 90.4 6.5 3.1 Application Example 3 4.9 96.2 2.3 1.5 Application Example 4 4.3 94.1 4.2 1.7 Application Example 5 6.2 92.2 5.6 2.2 Application 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] Combined with the above experimental data, it can be seen that the gas-liquid mixing component can increase the reaction rate and enhance CHP selectivity. Oxygen-enriched conditions can increase the reaction rate but are detrimental to CHP selectivity. A lower gas-liquid ratio improves mixing, which can increase the reaction rate and improve CHP selectivity. An increased gas-liquid ratio reduces the oxidation rate and is detrimental to CHP selectivity.

[0187] While the preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings, the present invention is not limited thereto. Within the technical scope of the present invention, various simple variations of the technical solution of the present invention may be made. To avoid unnecessary repetition, the present invention will not further describe various possible combinations. However, these simple variations and combinations should also be considered as disclosed herein and fall within the scope of protection of the present invention.

Claims

1. A gas-liquid mixing component, characterized in that: The invention comprises an injection tube (10) and a porous material membrane tube (20), wherein the injection tube (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 tube (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) which are sequentially arranged along the flow direction of the liquid, and 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 pore structures 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, preferably 60-300 L / h; The gas phase flux of the gas-liquid mixing component 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 .

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); Preferably, the pore size of the sieve hole (151) is 1-3 mm, and the number of the sieve holes (151) is 1-30, preferably 4-12; Preferably, 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°; Preferably, 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 30°-60°.

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); Preferably, the distance between one end of the air inlet section (13) close to the throttling section (12) and the liquid outlet end of the throttling section (12) is 1-10 mm, preferably 2-5 mm.

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, and the average pore size of the metal sintered film is 1-50 μm, preferably 1-20 μm.

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; Preferably, the pore size of the porous material membrane tube (20) is 1-100 μm, preferably 3-10 μm.

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); Preferably, the number of the channels (21) is 9-60, preferably 18-40; Preferably, a porous structure coating is provided on the inner wall of each of the channels (21); Preferably, the pore size of the porous structure coating is 20-800 nm, preferably 150-600 nm.

8. The gas-liquid mixing assembly according to claim 7, characterized in that: Each of the channels (21) is of equal diameter structure, and the inner diameter of the channel (21) is 1-6 mm, preferably 2-4 mm; Alternatively, each of the channels (21) comprises an inner bore tapered section (211) and an inner bore gradually expanding section (212) arranged in sequence 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, preferably 1.5-2.5:

1.

9. The gas-liquid mixing assembly according to any one of claims 1 to 8, characterized in that: The gas-liquid mixing component 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 filling material (31).

10. The gas-liquid mixing assembly according to claim 9, characterized in that: The length of the filling tube (30) is 1-30%, preferably 5-10%, of the length of the porous material membrane tube (20).

11. The gas-liquid mixing assembly according to claim 9, characterized in that: The size of the filler (31) is 1-10 mm, preferably 2-5 mm.

12. Use of the gas-liquid mixing assembly according to any one of claims 1 to 11 in cumene oxidation, characterized in that: The gas-liquid mixing component is built into the reactor (1) for cumene oxidation, and a plurality of the gas-liquid mixing components are arranged in parallel. The plurality of gas-liquid mixing components are used to mix the gas and liquid involved 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.

13. Use of the gas-liquid mixing assembly according to claim 12 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 a catalyst active component is loaded on the filler (31); or A filler (31) made of a material containing catalyst active components is arranged at the outlet of the porous material membrane tube (20).

14. Use of the gas-liquid mixing assembly according to claim 13 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; Preferably, 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%; Preferably, the catalyst active components are loaded by impregnation, vacuum coating, chemical vapor deposition or atomic layer deposition.

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