Gas-liquid mixer and its use in cumene oxidation

Abstract

The application relates to the technical field of chemical equipment, and discloses a gas-liquid mixer and application of the gas-liquid mixer in cumene oxidation, wherein the gas-liquid mixer comprises a mixer shell with a first pressure-bearing air charging area and a second pressure-bearing air charging area, a jet pipe is arranged in the first pressure-bearing air charging area, a porous material film pipe is arranged in the second pressure-bearing air charging area, the jet pipe is coaxially connected with the porous material film pipe to form a continuous internal flow channel for liquid flow, the jet 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 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 film pipe are respectively used for feeding gas into the internal flow channel; the gas-liquid mixer provided by the application realizes efficient mixing of gas-liquid two phases under the condition of high flux and high gas-liquid ratio, and effectively overcomes the defect that the prior art cannot form a large amount of micro-nano bubbles under the condition of high flux and high gas-liquid ratio.

Description

Technical Field

[0001] The present invention relates to the technical field of chemical equipment, in particular to a gas-liquid mixer 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 application is to overcome the problem of poor gas-liquid mixing efficiency under high flux and high gas-liquid ratio conditions in the prior art, and to provide a gas-liquid mixer 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 conditions.

[0006] In order to achieve the above-mentioned purpose, the present application provides a gas-liquid mixer, comprising a mixer shell with a first pressurized gas charging area and a second pressurized gas charging area, a spray pipe is arranged in the first pressurized gas charging area, and a porous material membrane pipe is arranged in the second pressurized gas charging area, 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 is larger than that of the throttling section, and the gas inlet section and the porous material membrane pipe are respectively used to introduce gas into the internal flow channel.

[0007] Preferably, a sieve plate is arranged at the throttling section of the spray pipe, and a plurality of sieve holes are arranged on the sieve plate.

[0008] Preferably, the diameter of the sieve hole is 1-3mm, and the number of the sieve hole is 1-30, preferably 4-12.

[0009] Preferably, the axial direction of the sieve hole is perpendicular to the cross section of the spray pipe perpendicular to the length direction, and the included angle is 90°.

[0010] Preferably, the axial direction of the sieve hole is perpendicular to the cross section of the spray pipe perpendicular to the length direction, and the included angle is 30°-60°.

[0011] Preferably, one 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.

[0012] Preferably, the spacing between one end of the gas inlet section close to the throttling section and the liquid outlet end of the throttling section is 1-10mm, preferably 2-5mm.

[0013] Preferably, the length ratio of the gas-liquid two-phase development section to the gas inlet section is 1-50:1, preferably 5-20:1.

[0014] Preferably, a plurality of spray pipes are arranged, a plurality of porous material membrane pipes are arranged, and a plurality of spray pipes and a plurality of porous material membrane pipes are coaxially connected one by one to form a plurality of continuous internal flow channels for liquid to pass through.

[0015] Preferably, one end of the mixer housing is provided with an inlet head for communicating a plurality of the sparging tubes away from one end of a plurality of the porous material membrane tubes, and the other end of the mixer housing is provided with an outlet head for communicating a plurality of the porous material membrane tubes away from one end of a plurality of the sparging tubes.

[0016] The inlet head is provided with a liquid inlet for liquid to enter, and the outlet head is provided with an outlet for gas-liquid mixture to flow out.

[0017] Preferably, a liquid distributor is provided in the inlet head for communicating the liquid inlet, and the liquid distributor is used to disperse the liquid into the internal flow channel.

[0018] Preferably, the outlet head is filled with a packing.

[0019] Preferably, the sparging tube is provided with a porous metal sintered membrane on the wall of the gas inlet section, and the average pore size of the metal sintered membrane is 1-50 μm, preferably 1-20 μm.

[0020] Preferably, the base material of the porous material membrane tube is selected from one of stainless steel, quartz, alumina, polytetrafluoroethylene, polypropylene, and polyethylene.

[0021] Preferably, the pore size of the porous material membrane tube is 1-100 μm, preferably 3-10 μm.

[0022] Preferably, a plurality of channels extending along the axial direction of the porous material membrane tube are provided on the porous material membrane tube, and the plurality of channels are combined to form the internal flow channel for the liquid to flow through the porous material membrane tube.

[0023] Preferably, the number of the channels is 9-60, preferably 18-40.

[0024] Preferably, a porous structure coating is provided on the inner wall of each channel.

[0025] Preferably, the pore size of the porous structure coating is 20-800 nm, preferably 150-600 nm.

[0026] Preferably, an intermediate seal is provided between the first pressurized gas charging zone and the second pressurized gas charging zone.

[0027] The mixer housing is provided with a first gas inlet for the gas to enter the first pressurized gas charging zone and a second gas inlet for the gas to enter the second pressurized gas charging zone.

[0028] Preferably, a plurality of the first gas inlets and a plurality of the second gas inlets are provided, respectively, and the plurality of the first gas inlets and the plurality of the second gas inlets are respectively arranged at intervals along the circumference of the mixer housing.

[0029] The second aspect of the present application provides an application of the aforementioned gas-liquid mixer in cumene oxidation, wherein a gas and a liquid for cumene oxidation reaction are mixed in the gas-liquid mixer to form a gas-liquid mixture, and the gas-liquid mixture is transported to a cumene oxidation reactor through a pipeline for reaction; the gas is an oxygen-containing gas, and the liquid is a liquid containing cumene or an oxidation liquid containing cumene hydroperoxide.

[0030] Preferably, the catalyst active component is loaded in the internal flow channel at the porous material membrane tube; or

[0031] The outlet of the porous material membrane tube is provided with a filler, and the filler is loaded with a catalyst active component; or

[0032] The outlet of the porous material membrane tube is provided with a filler prepared from a material containing a catalyst active component.

[0033] 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.

[0034] Preferably, the loading amount of the catalyst active component is 0.01% to 10%, preferably 0.05% to 5%, of the weight of the porous material membrane tube or the filler.

[0035] Preferably, the loading method of the catalyst active component is impregnation, vacuum coating, chemical vapor deposition, or atomic layer deposition.

[0036] Compared with the prior art, in the specific use of the gas-liquid mixer provided by the present application, the liquid enters from the end of the ejection tube away from the porous material membrane tube, sequentially passes through the ejection tube and the internal flow channel of the porous material membrane tube, and the pressurized gas is introduced into the first pressurized gas zone and the second pressurized gas zone, the pressurized gas enters the internal flow channel of the porous material membrane tube through the gas inlet section, mixes with the liquid, and forms a gas-liquid mixture.

[0037] 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 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 providing the injection pipe with 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 flow rate of the liquid becomes faster due to the smaller cross-sectional area; when entering the air inlet section, the pressure inside the liquid suddenly drops, causing the liquid to quickly diffuse to the surrounding area, generating violent eddy currents and turbulence phenomena, and this part of the liquid and the throttling section are mixed. The gas introduced through the air inlet section undergoes 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 complete; further, the primary gas-liquid mixture rich in small bubbles enters the internal flow channel of the porous material membrane tube, and the pressurized gas in the second pressurized inflation zone enters the internal flow channel through the porous material membrane tube and 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 the complete mixing of the gas-liquid two-phases.

[0038] The gas-liquid mixer provided by the present invention realizes efficient mixing of gas and liquid phases under high flux and high gas-liquid ratio conditions, 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

[0039] Figure 1 This is a structural schematic diagram of a gas-liquid mixer provided by the present invention;

[0040] Figure 2 This is a schematic structural diagram of a single injection pipe and a porous material membrane tube coaxially connected according to the present invention;

[0041] Figure 3 This is a schematic diagram of the application of a gas-liquid mixer provided by the present invention in the oxidation of cumene.

[0042] Description of Reference Numerals

[0043] 1. Isopropylbenzene oxidation reactor; 10. Mixer shell; 101. First pressurized aeration zone; 102. Second pressurized aeration zone; 11. Inlet head; 111. Liquid inlet; 12. Outlet head; 121. Outlet; 13. Liquid distributor; 14. Packing; 15. Intermediate seal; 16. First air inlet; 17. Second air inlet; 20. Injection pipe; 21. Liquid inlet section; 22. Throttling section; 23. Air inlet section; 24. Gas-liquid two-phase development section; 25. Sieve plate; 251. Sieve hole; 30. Porous material membrane tube; 31. Channel. DETAILED DESCRIPTION

[0044] 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.

[0045] As mentioned above, combined with Figure 1 、 2 As shown, the first aspect of the present invention provides a gas-liquid mixer for improving the mixing efficiency of gas and liquid under high flux and high gas-liquid ratio conditions.

[0046] The gas-liquid mixer includes a mixer shell 10 having a first pressurized inflation zone 101 and a second pressurized inflation zone 102, wherein an injection pipe 20 is provided in the first pressurized inflation zone 101, and a porous material membrane tube 30 is provided in the second pressurized inflation zone 102, and the injection pipe 20 is coaxially connected to the porous material membrane tube 30 to form a continuous internal flow channel for liquid to flow through; the injection pipe 20 includes a liquid inlet section 21, a throttling section 22, an air inlet section 23 and a gas-liquid two-phase development section 24 arranged in sequence along the flow direction of the liquid, the flow channel cross-sectional area of ​​the liquid inlet section 21 is equal to that of the air inlet section 23 and is larger than the flow channel cross-sectional area of ​​the throttling section 22, and the air inlet section 23 and the porous material membrane tube 30 are respectively used to introduce gas into the internal flow channel.

[0047] The gas-liquid mixer provided by the present invention, when in use, enters from the end of the injection tube 20 away from the porous material membrane tube 30, passes through the internal flow channels of the injection tube 20 and the porous material membrane tube 30 in turn, and pressurized gas is introduced into the first pressurized inflation zone 101 and the second pressurized inflation zone 102. The pressurized gas enters the internal flow channel through the air inlet section 23 and the porous material membrane tube 30, mixes with the liquid, and forms a gas-liquid mixture.

[0048] The present application ensures the mixing efficiency of gas-liquid two-phase under the condition of high flux and high gas-liquid ratio by arranging two gas-liquid mixing areas in the flow direction of the liquid, and gas can be introduced into the internal flow channel in the two gas-liquid mixing areas. Specifically, by arranging the injection pipe 20 as a liquid inlet section 21, a throttling section 22, a gas inlet section 23 and a gas-liquid two-phase development section 24 connected in sequence, the flow rate of the liquid increases due to the decrease of the flow channel cross-sectional area during the process of the liquid entering the throttling section 22 from the liquid inlet section 21, and the liquid rapidly spreads to the periphery due to the sudden drop of the internal pressure of the liquid when entering the gas inlet section 23, which generates intense vortex and turbulent flow phenomena. The part of the liquid and the gas introduced through the gas inlet section 23 generate intense mixing and friction to form a primary gas-liquid mixture rich in small gas bubbles. The gas and the liquid continue to interact and mix during the process of flowing through the gas-liquid two-phase development section 24, which makes the mixing of gas-liquid two-phase more sufficient. Further, the primary gas-liquid mixture rich in small gas bubbles enters the internal flow channel of the porous material membrane pipe 30, and the pressurized gas in the second pressurized gas charging area 102 enters the internal flow channel through the porous material membrane pipe 30 and mixes with the primary gas-liquid mixture again, which not only can effectively improve the gas-liquid ratio of the gas-liquid mixture, but also can improve the bubble density in the gas-liquid mixture and promote the sufficient mixing of gas-liquid two-phase.

[0049] In the gas-liquid mixer provided by the present application, by arranging two gas-liquid mixing areas and gradually mixing gas-liquid two-phase by the injection pipe 20 and the porous material membrane pipe 30, the efficient mixing of gas-liquid two-phase under the condition of high flux and high gas-liquid ratio is realized, and the defect that a large number of micro-nano gas bubbles cannot be formed under the condition of high flux and high gas-liquid ratio in the prior art is overcome.

[0050] In the present application, the injection pipe 20 is based on the Venturi principle, and the throttling section 22 generates intense vortex and turbulent flow phenomena in the liquid, and then realizes efficient mixing with the gas entering the internal flow channel through the gas inlet section 23. In an embodiment of the present application, the throttling section 22 of the injection pipe 20 is provided with a sieve plate 25, and a plurality of sieve holes 251 are arranged on the sieve plate 25. By arranging the sieve plate 25 with a plurality of sieve holes 251 on the flow path of the liquid, the liquid passing through the throttling section 22 is sufficiently disturbed, and the efficient mixing between the liquid and the gas is promoted.

[0051] In the present application, the aperture and the number of the sieve holes 251 can be adaptively selected according to the specific type of the liquid, which can generate sufficient vortex and turbulent flow in the gas inlet section 23, and then realize the efficient mixing of the liquid and the gas. In some embodiments of the present application, the aperture of the sieve hole 251 is 1-3 mm, and the number of the sieve hole 251 is 1-30, preferably 4-12.

[0052] In some embodiments, the angle between the axial direction of the sieve hole 251 and the cross section of the injection pipe 20 perpendicular to the length direction is 90°; through this structural design, the liquid flowing through the liquid inlet section 21 directly enters the multiple sieve holes 251 of the sieve plate 25, and after compression and acceleration, enters the air inlet section 23 for release.

[0053] In some embodiments, the angle between the axial direction of the sieve hole 251 and the cross-section of the injection pipe 20 perpendicular to the length direction is 30°-60°; at this time, the liquid flowing through the liquid inlet section 21 changes direction when entering the sieve hole 251 of the sieve plate 25, further increasing the degree of turbulence of the liquid after flowing through the throttling section 22, thereby promoting more complete mixing of the liquid and the gas entering the internal flow channel through the air inlet section 23.

[0054] In some embodiments, the end of the air inlet section 23 near the throttle section 22 is spaced apart from the liquid outlet end of the throttle section 22. Due to the compression and acceleration of the throttle section 22, the liquid generates intense eddy currents and turbulence as it leaves the throttle section 22. This spacing provides space for the eddy currents and turbulence. Preferably, the spacing between the end of the air inlet section 23 near the throttle section 22 and the liquid outlet end of the throttle section 22 is 1-10 mm, more preferably 2-5 mm.

[0055] In some embodiments, the ratio of the length of the gas-liquid two-phase development section 24 to the length of the gas inlet section 23 is 1-50:1, preferably 5-20:1.

[0056] In some embodiments, multiple injection tubes 20 and multiple porous membrane tubes 30 are provided, and the multiple injection tubes 20 and the multiple porous membrane tubes 30 are coaxially connected in a one-to-one correspondence to form multiple continuous internal flow channels for liquid to pass through. In the present invention, by providing multiple parallel internal flow channels for liquid to pass through, and coordinating the injection tubes 20 and the porous membrane tubes 30 to introduce air into the internal flow channels, the contact area between the gas and liquid phases is increased while ensuring high gas and liquid flux, thereby promoting sufficient mixing between the gas and liquid phases.

[0057] It is understood that the number of the internal flow channels connected in parallel in the mixer housing 10 is designed according to the required liquid phase flux. In one embodiment of the present invention, the outer diameter of a single injection pipe 20 and a single porous material membrane tube 30 is 10-50 mm, preferably 20-30 mm; the liquid phase flux is 30-1000 L / h, preferably 60-300 L / h; the gas flux per unit length is 30-10000 L / h, preferably 60-5000 L / h; the gas-liquid volume ratio per unit length is 0.1-10m -1 , preferably 0.5-4m -1 .

[0058] In some embodiments, one end of the mixer housing 10 is provided with an inlet head 11 for connecting the plurality of the injection tubes 20 to the one end of the plurality of the porous material membrane tubes 30, and the other end of the mixer housing 10 is provided with an outlet head 12 for connecting the plurality of the porous material membrane tubes 30 to the other end of the plurality of the injection tubes 20; the inlet head 11 is provided with a liquid inlet 111 for liquid to enter, and the outlet head 12 is provided with an outlet 121 for the gas-liquid mixture to flow out. In the specific operation of the gas-liquid mixer of this embodiment, liquid enters the inlet head 11 through the liquid inlet 111, then enters the plurality of the internal flow channels, fully contacts with the gas to form micro-bubbles, and the gas-liquid mixture rich in micro-bubbles then enters the outlet head 12 and is discharged from the gas-liquid mixer through the outlet 121.

[0059] It should be noted that in the present application, the inlet head 11 can be provided in any appropriate form to one end of the mixer housing 10, as long as it can effectively isolate the inlet head 11 from the first pressure-charged gas zone 101. For example, the inlet head 11 and the one end of the mixer housing 10 are sealed by gasket compression, metal mechanical compression, welding or gluing, preferably metal mechanical compression or welding.

[0060] Similarly, the outlet head 12 can be provided in any appropriate form to the other end of the mixer housing 10, as long as it can effectively isolate the outlet head 12 from the second pressure-charged gas zone 102. For example, the outlet head 12 and the other end of the mixer housing 10 are sealed by gasket compression, metal mechanical compression, welding or gluing, preferably gasket compression.

[0061] In some embodiments, the inlet head 11 is provided with a liquid distributor 13 connected to the liquid inlet 111, which is used to disperse the liquid into the internal flow channels. By providing the liquid distributor 13, it is ensured that the liquid can uniformly enter each internal flow channel.

[0062] It can be understood that the liquid distributor 13 can be in any appropriate form, as long as it can uniformly distribute the liquid entering the inlet head 11 to each internal flow channel. For example, the liquid distributor 13 is a branch-type perforated tube, a circular ring-type perforated tube, a slot-type distributor, a baffle distributor or a metal sintered distributor. As a preferred, the liquid distributor 13 is a metal sintered distributor, a branch-type perforated tube or a circular ring-type perforated tube.

[0063] In some embodiments, the outlet head 12 is filled with a packing 14. It is to be noted that in this embodiment, the gas-liquid mixture entering into the outlet head 12 is already rich in micro-bubbles, and the packing 14 can further enhance the turbulence of the gas-liquid mixture, achieve the partition disturbance of the gas-liquid mixture, and promote the generation of more micro-bubbles.

[0064] It is to be noted that the structure of the packing 14 can adopt any appropriate form as long as it can promote the generation of more micro-bubbles. The shape of the packing 14 can be selected as a Pall ring, a Raschig ring, a corrugated mesh, or a hollow spherical shape.

[0065] In addition, for some gas-liquid phase reactions that need to provide a catalyst, by loading a corresponding catalyst in the packing 14, the efficient reaction of the gas-liquid phases can be achieved at the end of the gas-liquid mixer simultaneously; further, the packing 14 is directly prepared from a material containing a catalyst active component.

[0066] It can be understood that in the present application, the injection pipe 20 needs to meet the strength requirement of the gas-liquid pressure difference, and further considering the cost, the wall thickness of the injection pipe 20 is 1-5 mm, and further preferably 1-2 mm.

[0067] In the present application, part of the gas in the gas-liquid mixture enters into the internal flow channel through the gas inlet section 23 of the injection pipe 20. In some embodiments, the pipe wall of the injection pipe 20 located at the gas inlet section 23 is provided as a sintered film of metal material, and the average pore size of the sintered film of metal material is 1-50 μm, and preferably 1-20 μm. Specifically, the metal material for preparing the sintered film of metal material is titanium, carbon steel, stainless steel, or hastelloy, and preferably stainless steel or hastelloy.

[0068] Further, in the present application, another part of the gas in the gas-liquid mixture enters into the internal flow channel through the porous material film pipe 30. In some embodiments, the base material of the porous material film pipe 30 is selected from one of stainless steel, quartz, alumina, polytetrafluoroethylene, polypropylene, and polyethylene; and preferably stainless steel or alumina. The pipe wall of the porous material film pipe 30 is a porous structure, and the pore size is 1-100 μm, and preferably 3-10 μm.

[0069] It can be understood that the base material for preparing the porous material film pipe 30 is pre-formed into a pipe type, and is subjected to a sintering treatment, so as to obtain the porous material film pipe 30 with the internal flow channel and the porous structure of the pipe wall. In specific use, the liquid flows in the internal flow channel, and the pressurized gas penetrates into the internal flow channel through the porous structure on the pipe wall, mixes with the liquid, and forms a gas-liquid mixture.

[0070] In some embodiments, the porous material membrane tube 30 is provided with a plurality of channels 31 extending along the axial direction thereof, which channels 31 combine to form the internal flow channel for the liquid to flow through the porous material membrane tube 30; by providing the plurality of channels 31, 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.

[0071] In some embodiments, the number of channels 31 is set to 9-60, preferably 18-40.

[0072] In some embodiments, the inner wall of each channel 31 is provided with a porous structure coating; 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 31, the gas penetrates into the internal flow channel through the porous structure coating, which promotes the generation of more micro-bubbles. Specifically, the porous structure coating is formed by sintering a nano material, and the nano material is an oxide, preferably alumina, zirconia, silica or titanium dioxide.

[0073] In the present application, the first pressurized aeration zone 101 and the second pressurized aeration zone 102 are provided with an intermediate seal 15, and the mixer housing 10 is provided with a first gas inlet 16 for the gas to enter the first pressurized aeration zone 101 and a second gas inlet 17 for the gas to enter the second pressurized aeration zone 102. The interior of the mixer housing 10 is separated by the intermediate seal 15 to form independent first pressurized aeration zone 101 and second pressurized aeration zone 102, so that the operation of introducing gas into the internal flow channel through the gas inlet section 23 of the injection pipe 20 and the operation of introducing gas into the internal flow channel through the porous material membrane tube 30 do not affect each other.

[0074] It should be noted that in the present application, the intermediate seal 15 can be provided in any appropriate form in the mixer housing 10, as long as it can effectively isolate the first pressurized aeration zone 101 and the second pressurized aeration zone 102. For example, the intermediate seal 15 and the mixer housing 10 can be sealed by a gasket, a metal mechanical seal, welding or gluing, preferably a gasket.

[0075] Further, the first gas inlet 16 and the second gas inlet 17 are respectively provided with a plurality of first gas inlets 16 and a plurality of second gas inlets 17, which are respectively arranged along the circumference of the mixer housing 10. By providing a plurality of first gas inlets 16 and a plurality of second gas inlets 17, the gas flux is improved, and the uniformity of the gas entering the internal flow channel through the gas inlet section 23 and the porous material membrane tube 30 is improved.

[0076] In some embodiments, the first air inlets 16 and the second air inlets 17 are respectively arranged in 1-5 groups, preferably 2-3 groups, and each group of the first air inlets 16 and each group of the second air inlets 17 are respectively symmetrically arranged along the center of the mixer housing 10 .

[0077] In the present invention, the length of the mixer shell 10 depends on the total length of the injection pipe 20 and the porous material membrane tube 30 and the number of parallel connections thereof. The diameter of the mixer shell 10 can be designed according to the heat exchanger shell design specification.

[0078] The gas-liquid mixer provided by the present invention is further described below through specific embodiments.

[0079] Example 1

[0080] This embodiment provides a Figure 1 The gas-liquid mixer shown includes a mixer housing 10, an inlet head 11 disposed at one end of the mixer housing 10, and an outlet head 12 disposed at the other end of the mixer housing 10. The inlet head 11 is sealed to one end of the mixer housing 10 with a gasket, while the outlet head 12 is sealed to the other end of the mixer housing 10 with a gasket. The inlet head 11 is provided with a liquid inlet 111 for liquid entry, and a branch-type liquid distributor is provided within the inlet head 11, communicating with the liquid inlet 111. The outlet head 12 is provided with an outlet 121 for the gas-liquid mixture to flow out, and the outlet head 12 is filled with Raschig ring packing.

[0081] The inner diameter of the mixer housing 10 is 80 mm;

[0082] A first pressurized aeration zone 101 having three injection tubes 20 and a second pressurized aeration zone 102 having three porous material membrane tubes 30 are provided in the mixer housing 10; the three injection tubes 20 and the three porous material membrane tubes 30 are coaxially connected one by one to form three continuous internal flow channels for liquid to flow through.

[0083] The outer diameter of the injection tube 20 and the porous material membrane tube 30 is 30 mm;

[0084] The injection pipe 20 includes a liquid inlet section 21, a throttling section 22, a gas inlet section 23 and a gas-liquid two-phase development section 24 which are sequentially arranged along the flow direction of the liquid.

[0085] A sieve plate 25 is provided in the injection pipe 20 at the throttling section 22 . The sieve plate 25 is provided with eight sieve holes 251 . The aperture of the eight sieve holes 251 is 1 mm respectively.

[0086] The angle between the axial direction of the screen hole 251 and the cross section of the injection pipe 20 perpendicular to the length direction is 60°; the distance between the end of the inlet section 23 close to the throttle section 22 and the outlet end of the throttle section 22 is 1 mm.

[0087] The length of the gas-liquid two-phase development section 24 is 10 mm, and the length of the inlet section 23 is 1 mm.

[0088] The pipe wall of the injection pipe 20 located in the inlet section 23 is a porous stainless steel sintered film with an average pore size of 10 μm and a length of 1 mm; the material of the porous material film pipe 30 is alumina, and the pore size of the pipe wall is 5 μm; the porous material film pipe 30 is provided with 37 channels 31 extending in the axial direction, and the inner wall of the channel 31 is provided with a porous structure coating, and the material of the porous structure coating is nano-alumina with a pore size of 200 nm.

[0089] The gas-liquid mixer provided in the embodiment is used for mixing ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 6 L / min.

[0090] The bubble size in the gas-liquid mixture flowing out of the outlet 121 is statistically analyzed by a bubble imaging monitoring system, and the average bubble size is 102 μm.

[0091] Example 2

[0092] The gas-liquid mixer provided in the embodiment is used for mixing benzene and air, wherein the feed flow rate of benzene is 3 L / min, and the feed flow rate of air is 6 L / min.

[0093] The bubble size in the gas-liquid mixture flowing out of the outlet 121 is statistically analyzed by a bubble imaging monitoring system, and the average bubble size is 164 μm.

[0094] Example 3

[0095] The gas-liquid mixer provided in the embodiment is used for mixing water and air, wherein the feed flow rate of water is 3 L / min, and the feed flow rate of air is 6 L / min.

[0096] The bubble size in the gas-liquid mixture flowing out of the outlet 121 is statistically analyzed by a bubble imaging monitoring system, and the average bubble size is 281 μm.

[0097] Example 4

[0098] The gas-liquid mixer provided in the embodiment is used for mixing ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 12 L / min.

[0099] The bubble imaging monitoring system was used to statistically analyze the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 173 μm.

[0100] Example 5

[0101] The gas-liquid mixer provided in Example 1 was used to mix ethanol and air, wherein the feed flow rate of ethanol was 6 L / min and the feed flow rate of air was 6 L / min.

[0102] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 87 μm.

[0103] Example 6

[0104] The gas-liquid mixer provided in Example 1 was used to mix ethanol and air, wherein the feed flow rate of ethanol was 12 L / min and the feed flow rate of air was 6 L / min.

[0105] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 54 μm.

[0106] Example 7

[0107] The structure of the gas-liquid mixer provided in this embodiment is basically the same as that provided in embodiment 1, except that the inner diameter of the mixer housing 10 is 800 mm; the number of the injection pipes 20 and the porous material membrane tubes 30 is 30;

[0108] The gas-liquid mixer provided in this embodiment is used to mix ethanol and air, wherein the feed flow rate of ethanol is 300 L / min and the feed flow rate of air is 600 L / min.

[0109] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 108 μm.

[0110] Example 8

[0111] The structures of the gas-liquid mixers provided in this embodiment are substantially the same as those provided in embodiment 1, except that the aperture of the sieve holes 251 on the sieve plate 25 is 2 mm; the rest remain unchanged.

[0112] The gas-liquid mixer provided in this embodiment 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 6 L / min.

[0113] The bubble imaging monitoring system was used to statistically analyze the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 131 μm.

[0114] Example 9

[0115] The gas-liquid mixer provided in this example has the same structure as the gas-liquid mixer provided in Example 1, except that the length of the gas inlet section 23 is 3 mm; the rest remains unchanged.

[0116] The gas-liquid mixer provided in this example was used to mix ethanol and air, with the feed flow rate of ethanol being 3 L / min and the feed flow rate of air being 6 L / min.

[0117] The bubble size in the gas-liquid mixture flowing out of the outlet 121 was statistically analyzed by the bubble imaging monitoring system, and the average bubble size was 166 μm.

[0118] Example 10

[0119] The gas-liquid mixer provided in this example has the same structure as the gas-liquid mixer provided in Example 1, except that the distance between the end of the gas inlet section 23 close to the throttling section 22 and the liquid outlet end of the throttling section 22 is 5 mm; the rest remains unchanged.

[0120] The gas-liquid mixer provided in this example was used to mix ethanol and air, with the feed flow rate of ethanol being 3 L / min and the feed flow rate of air being 6 L / min.

[0121] The bubble size in the gas-liquid mixture flowing out of the outlet 121 was statistically analyzed by the bubble imaging monitoring system, and the average bubble size was 234 μm.

[0122] Example 11

[0123] The gas-liquid mixer provided in this example has the same structure as the gas-liquid mixer provided in Example 1, except that the porous material film tube 30 is provided with 10 channels 31 extending in the axial direction; the rest remains unchanged.

[0124] The gas-liquid mixer provided in this example was used to mix ethanol and air, with the feed flow rate of ethanol being 3 L / min and the feed flow rate of air being 6 L / min.

[0125] The bubble size in the gas-liquid mixture flowing out of the outlet 121 was statistically analyzed by the bubble imaging monitoring system, and the average bubble size was 141 μm.

[0126] Example 12

[0127] The gas-liquid mixer provided in this example has the same structure as the gas-liquid mixer provided in Example 1, except that the pore size of the porous structure coating in the channel 31 of the porous material film tube 30 is 1000 nm; the rest remains unchanged.

[0128] The gas-liquid mixer provided in this embodiment 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 6 L / min.

[0129] The bubble imaging monitoring system was used to statistically analyze the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 223 μm.

[0130] Example 13

[0131] The structures of the gas-liquid mixers provided in this embodiment are basically the same as those provided in Embodiment 1, except that the liquid distributor in the inlet head 11 is a baffle-type distributor; the rest remain unchanged.

[0132] The gas-liquid mixer provided in this embodiment 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 6 L / min.

[0133] The bubble imaging monitoring system was used to statistically analyze the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 122 μm.

[0134] Example 14

[0135] The structures of the gas-liquid mixers provided in this embodiment are basically the same as those provided in Embodiment 1, except that the liquid distributor in the inlet head 11 is a metal sintered distributor; the rest remain unchanged.

[0136] The gas-liquid mixer provided in this embodiment 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 6 L / min.

[0137] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 89 μm.

[0138] Example 15

[0139] The structures of the gas-liquid mixers provided in this embodiment are basically the same as those provided in embodiment 1, except that the Raschig ring packing filled in the outlet head 12 is a corrugated mesh packing; the rest remain unchanged.

[0140] The gas-liquid mixer provided in this embodiment 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 6 L / min.

[0141] The bubble imaging monitoring system was used to statistically analyze the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 63 μm.

[0142] In the above test provided by the present application, the smaller the average size of the bubbles obtained after mixing the gas phase and the liquid phase, the better the effect of mixing the gas-liquid two phases.

[0143] Based on the test data, the gas-liquid mixer provided by the present application has a good gas-liquid mixing effect on different gas phases and liquid phases, and the average size of the bubbles after gas-liquid mixing can be controlled to be below 300 μm. It can be seen from the data of Examples 1, 4, 5, 6 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; it can be seen from the data of Examples 1, 7 that overall enlarging the specification of the gas-liquid mixer has little effect on the average size of the bubbles; it can be seen from the data of Examples 1, 8 that increasing the pore size of the sieve hole 151 will cause the average size of the bubbles to increase; it can be seen from the data of Examples 1, 9 that increasing the length of the gas inlet section 23 is not conducive to reducing the average size of the bubbles; it can be seen from the data of Examples 1, 10 that increasing the distance between the end of the gas inlet section 23 close to the throttling section 22 and the liquid outlet end of the throttling section 22 is not conducive to reducing the average size of the bubbles; it can be seen from the data of Examples 1, 11 that reducing the number of the channels 31 will increase the average size of the bubbles; it can be seen from the data of Examples 1, 12 that increasing the pore size of the porous structure coating in the channel 31 will increase the average size of the bubbles; it can be seen from the data of Examples 1, 13, 14 that different liquid distributors will affect the average size of the bubbles, and the metal sintered distributor is the best; it can be seen from the data of Examples 1, 15 that the corrugated mesh packing is better than the Rasching ring packing, and the corrugated mesh packing can obtain bubbles with a relatively low average size.

[0144] The gas-liquid mixer provided by the present application is suitable for the mixing process of gas and liquid under high flux and high gas-liquid ratio conditions, and uses liquid to divide the gas to form micron-level small bubbles. The gas includes non-condensable gas and steam, the non-condensable gas includes oxygen, hydrogen, air, carbon monoxide and ammonia, and the steam includes various organic or inorganic steam.

[0145] The gas-liquid mixer provided by the present application can be applied to gas-liquid-solid three-phase or gas-liquid two-phase oxidation, hydrogenation, ammonia oxidation, nitration, chlorination, fluorination and the like. In particular, the inventors of the present application found that the gas-liquid mixer provided by the present application has a significant promoting effect in the cumene oxidation process.

[0146] Based on this, in combination with Figure 3As shown, the second aspect of the present application provides an application of the aforementioned gas-liquid mixer in cumene oxidation, wherein a gas and a liquid for cumene oxidation reaction are mixed in the gas-liquid mixer to form a gas-liquid mixture, and the gas-liquid mixture is transported to a cumene oxidation reactor 1 for reaction; the gas is an oxygen-containing gas, and the liquid is a liquid containing cumene or an oxidation liquid containing cumene hydroperoxide.

[0147] Cumene hydroperoxide, abbreviated as CHP, is an organic aromatic hydrocarbon derivative, which can be used for ethylene cracking gasoline arsenic removal and ABS graft polymerization initiator, epoxide oxidant and phenol acetone production. However, the traditional cumene oxidation process has many defects, such as slow reaction process rate, low selectivity of target product and the like. In recent years, the research on the cumene oxidation process at home and abroad mainly focuses on improving the conversion rate and selectivity, and the reaction temperature and pressure are relatively high, and the cost is also relatively high. Moreover, since the mechanism of cumene oxidation reaction is relatively complex, it is essentially a slow reaction process, and the improvement of process conditions is also very limited.

[0148] Although the use of catalysts can significantly improve the oxidation efficiency, it makes the process more complex, and many problems still exist in the separation and reuse of catalysts; non-catalytic oxidation is more widely used in industrial applications, but its initial reaction rate is very slow, and there is a long induction period, which is not conducive to large-scale production. In order to overcome the above technical problems, low content CHP is used as an initiator in industrial production to speed up the free radical chain reaction, so as to shorten or eliminate the induction period. In addition, a small amount of organic acid is usually generated during the oxidation process, which leads to the decomposition of CHP, thereby reducing the yield of CHP. In order to prevent side reactions (byproducts such as 2-phenyl-2-propanol (PP) and acetophenone (AP)) and excessive decomposition of CHP, the conversion rate of cumene is usually controlled to be less than 30%, but the problems of slow oxidation rate and large energy consumption of reaction equipment have not been significantly improved.

[0149] The inventors of the present application found that by using the gas-liquid mixer provided by the present application, the contact interface between the gas and liquid phases in the cumene oxidation process is effectively improved, and the micron-sized bubbles formed under the conditions of high flux and high gas-liquid ratio significantly improve the oxidation rate.

[0150] According to an embodiment of the present application, the catalyst active component is loaded in the internal flow channel at the porous material membrane tube 30; by coupling the catalyst active component in the porous material membrane tube 30, the separation problem of the catalyst in the cumene oxidation is effectively solved, and the micron-sized small bubbles generated in the porous material membrane tube 30 improve the contact area between gas-liquid-solid, and further improve the cumene oxidation efficiency and CHP selectivity.

[0151] According to another embodiment of the present application, a filler 14 is arranged at the outlet of the porous material membrane tube 30, and the filler 14 is loaded with a catalyst active component; in this embodiment, the filler 14 can be made of alumina, titania, ceria, zirconia or molecular sieve, preferably alumina, titania and molecular sieve; the size of the filler 14 is 1-10 mm, preferably 2-5 mm. The catalyst active component is loaded on the filler 14 by any appropriate form, such as impregnation, vacuum coating, chemical vapor deposition or atomic layer deposition.

[0152] According to still another embodiment of the present application, a filler 14 is arranged at the outlet of the porous material membrane tube 30, and the filler 14 is made of a material containing a catalyst active component. In this embodiment, the catalyst powder is prepared by co-precipitation or deposition precipitation, and then the filler 14 is further formed.

[0153] In the application of the gas-liquid mixer in the oxidation of cumene, the structure of the filler 14 can be any appropriate form as long as it can facilitate the loading of the catalyst and promote the generation of more micro-bubbles. The shape of the filler 14 can be selected as Pall ring, Raschig ring, corrugated mesh or hollow sphere, preferably corrugated mesh or hollow sphere.

[0154] In the present application, by arranging the filler 14 and further loading the catalyst active component on the filler 14, the filler 14 can further improve the turbulence degree of the gas-liquid mixture, realize the segmentation disturbance of the gas-liquid mixture, promote the generation of more micro-bubbles, and cooperate with the loaded catalyst active component to further improve the oxidation efficiency and selectivity of cumene.

[0155] In the present application, the catalyst active component is selected from the oxides of at least one of copper, magnesium, cobalt, manganese, nickel, chromium, zinc, iron, silver and gold; further, the loading amount of the catalyst active component is 0.01%-10% of the weight of the porous material membrane tube 30 or the filler 14, preferably 0.05%-5%; still further, the loading mode of the catalyst active component is impregnation, vacuum coating, chemical vapor deposition or atomic layer deposition.

[0156] The application of the gas-liquid mixer in the oxidation of cumene provided by the present application is further described below through specific application examples.

[0157] Application Example 1

[0158] In this application example, the gas-liquid mixer provided in Example 1 was used to perform gas-liquid mixing of cumene hydroperoxide and air (oxygen concentration 21% (by volume percentage)), with a gas feed rate of 6 L / min and a liquid feed rate of 3 L / min. The resulting gas-liquid mixture was transported to a cumene oxidation reactor via a pipeline for reaction. The reaction temperature was maintained at 100° C., the reaction pressure was 0.3 MPaG, and the initial cumene hydroperoxide concentration was 14 wt %. After 6 h, a sample was taken and analyzed for cumene hydroperoxide concentration by iodine titration, and other byproducts, such as acetophenone and dimethylbenzyl alcohol, were analyzed by liquid chromatography. The reaction results are summarized in Table 1.

[0159] In the gas-liquid mixer, both the porous membrane tube 30 and the filler 14 are loaded with CuO active components. The catalytic active component loaded on the porous membrane tube 30, calculated as Cu, is 1% of the mass of the porous membrane tube 30; the catalytic active component loaded on the filler 14, calculated as Cu, is 1% of the mass of the filler 14.

[0160] Application Example 2

[0161] This application example is basically the same as application example 1, except that the gas is replaced with oxygen-enriched gas (oxygen concentration is 50% (by volume percentage)); the other conditions remain unchanged, and the final analysis results are summarized in Table 1.

[0162] Application Example 3

[0163] This application example is basically the same as application example 1, except that the liquid feed rate is controlled to 6 L / min, and the rest remain unchanged. The final analysis results are summarized in Table 1.

[0164] Application Example 4

[0165] This application example is basically the same as application example 1, except that the liquid feed rate is controlled to 1.5 L / min, and the other conditions remain unchanged. The final analysis results are summarized in Table 1.

[0166] Application Example 5

[0167] This application example is basically the same as application example 1, except that the catalyst active component on the porous material membrane tube 30 is loaded in an amount of 3% of the mass of the porous material membrane tube 30, calculated as Cu; the catalyst active component on the filler 14 is loaded in an amount of 3% of the mass of the filler 14, calculated as Cu; the other conditions remain unchanged, and the final analysis results are summarized in Table 1.

[0168] Application Example 6

[0169] This application example is basically the same as application example 1, except that the porous material membrane tube 30 and the filler 14 are both loaded with MgO active components, the loading amount remains unchanged, and the other conditions remain unchanged. The final analysis results are summarized in Table 1.

[0170] Application Example 7

[0171] This application example is basically the same as application example 1, except that the porous material membrane tube 30 and the filler 14 are not loaded with catalyst active components. Other conditions remain unchanged. The final analysis results are summarized in Table 1.

[0172] The conventional aeration method was used as a comparative example. The gas phase feed rate during aeration was 6 L / min. The reaction results are summarized in Table 1.

[0173] Table 1:

[0174]

[0175]

[0176] Combining the data of Application Example 1 and the comparative example, it can be seen that the gas-liquid mixer provided by the present invention can increase the reaction rate and improve the selectivity of CHP. Combining the data of Application Examples 1 and 2, it can be seen that oxygen-enriched conditions can increase the reaction rate, but are detrimental to the selectivity of CHP; Combining the data of Application Examples 1, 3, and 4, it can be seen that a lower gas-liquid ratio and a better mixing effect can increase the reaction rate and help improve the selectivity of CHP; an increase in the gas-liquid ratio reduces the oxidation rate and is detrimental to the selectivity of CHP; Combining the data of Application Examples 1 and 5, it can be seen that increasing the loading amount of the catalyst active component can increase the reaction rate but is detrimental to the selectivity of CHP; Combining the data of Application Examples 1 and 6, it can be seen that the reaction rate when MgO is loaded is better than that when CuO is loaded, but the selectivity of CHP when CuO is loaded is better than that when MgO is loaded; Combining the data of Application Examples 1 and 7, it can be seen that the loaded catalyst can increase the reaction rate, but has an impact on the selectivity of CHP.

[0177] 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 mixer, characterized in that: The mixer comprises a housing (10) having a first pressurized aeration zone (101) and a second pressurized aeration zone (102), wherein an injection pipe (20) is provided in the first pressurized aeration zone (101), and a porous material membrane tube (30) is provided in the second pressurized aeration zone (102), wherein the injection pipe (20) and the porous material membrane tube (30) are coaxially connected to form a continuous internal flow channel for liquid to flow through; The injection pipe (20) comprises a liquid inlet section (21), a throttling section (22), an air inlet section (23) and a gas-liquid two-phase development section (24) which are sequentially arranged along the flow direction of the liquid. The flow channel cross-sectional areas of the liquid inlet section (21) and the air inlet section (23) are equal and larger than the flow channel cross-sectional area of ​​the throttling section (22). The air inlet section (23) and the porous material membrane tube (30) are respectively used to introduce gas into the internal flow channel. An intermediate sealing member (15) is provided between the first pressurized inflation zone (101) and the second pressurized inflation zone (102); The mixer housing (10) is provided with a first air inlet (16) for the gas to enter the first pressurized inflation zone (101) and a second air inlet (17) for the gas to enter the second pressurized inflation zone (102).

2. The gas-liquid mixer according to claim 1, characterized in that A sieve plate (25) is provided at the throttling section (22) of the injection pipe (20), and a plurality of sieve holes (251) are provided on the sieve plate (25).

3. The gas-liquid mixer according to claim 1, characterized in that One end of the air inlet section (23) close to the throttling section (22) is arranged to be spaced apart from the liquid outlet end of the throttling section (22).

4. The gas-liquid mixer according to claim 1, characterized in that The ratio of the length of the gas-liquid two-phase development section (24) to the length of the air inlet section (23) is 1-50:

1.

5. The gas-liquid mixer according to claim 1, characterized in that A plurality of injection tubes (20) are provided, and a plurality of porous material membrane tubes (30) are provided. The plurality of injection tubes (20) are coaxially connected with the plurality of porous material membrane tubes (30) in a one-to-one correspondence to form a plurality of continuous internal flow channels for liquid to pass through.

6. The gas-liquid mixer according to claim 5, characterized in that One end of the mixer housing (10) is provided with an inlet seal (11) for connecting the ends of the plurality of injection tubes (20) away from the ends of the plurality of porous material membrane tubes (30), and the other end of the mixer housing (10) is provided with an outlet seal (12) for connecting the ends of the plurality of porous material membrane tubes (30) away from the ends of the plurality of injection tubes (20); The inlet seal (11) is provided with a liquid inlet (111) for liquid to enter, and the outlet seal (12) is provided with an outlet (121) for the gas-liquid mixture to flow out.

7. The gas-liquid mixer according to claim 6, characterized in that A liquid distributor (13) communicating with the liquid inlet (111) is provided in the inlet seal (11), and the liquid distributor (13) is used to disperse the liquid into the internal flow channel.

8. The gas-liquid mixer according to claim 6, characterized in that The outlet head (12) is filled with filler (14).

9. The gas-liquid mixer according to claim 1, characterized in that The tube wall of the injection tube (20) located in the air inlet section (23) is configured as a porous metal sintered film, and the average pore size of the metal sintered film is 1-50 μm.

10. The gas-liquid mixer according to claim 1, characterized in that The base material of the porous material membrane tube (30) is selected from one of stainless steel, quartz, alumina, polytetrafluoroethylene, polypropylene, and polyethylene.

11. The gas-liquid mixer according to claim 1, characterized in that The porous material membrane tube (30) is provided with a plurality of channels (31) extending along its axial direction, and the plurality of channels (31) are combined to form the internal flow channel for the liquid to flow through the porous material membrane tube (30).

12. The gas-liquid mixer according to claim 11, characterized in that A porous structure coating is provided on the inner wall of each channel (31).

13. The gas-liquid mixer according to claim 12, characterized in that: A plurality of the first air inlet (16) and a plurality of the second air inlet (17) are provided, and the plurality of the first air inlet (16) and the plurality of the second air inlet (17) are arranged at intervals along the circumference of the mixer housing (10).

14. Use of the gas-liquid mixer according to any one of claims 1 to 13 in cumene oxidation, characterized in that: The gas and liquid for the cumene oxidation reaction are mixed in the gas-liquid mixer to form a gas-liquid mixture, and the gas-liquid mixture is transported to the cumene oxidation reactor (1) through a pipeline for reaction; The gas is an oxygen-containing gas, and the liquid is a liquid containing cumene or an oxidizing liquid containing cumene hydroperoxide.

15. Use of the gas-liquid mixer according to claim 14 in cumene oxidation, characterized in that: The internal flow channel located at the porous material membrane tube (30) is loaded with catalyst active components; or A filler (14) is provided at the outlet of the porous material membrane tube (30), and the filler (14) is loaded with catalyst active components; or A filler (14) made of a material containing catalyst active components is provided at the outlet of the porous material membrane tube (30).

16. Use of the gas-liquid mixer according to claim 15 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.

17. Use of the gas-liquid mixer according to claim 16 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 (30) or the filler (14).

18. Use of the gas-liquid mixer according to claim 17 in cumene oxidation, characterized in that: The loading amount of the catalyst active component is 0.05%-5% of the weight of the porous material membrane tube (30) or the filler (14).

19. Use of the gas-liquid mixer according to claim 16 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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