Membrane distributed gas-liquid mixer and application thereof

Abstract

The invention relates to the technical field of gas-liquid mixers, in particular to a membrane-distributed gas-liquid mixer and application thereof, and the membrane-distributed gas-liquid mixer comprises a ceramic membrane tube, a sintered membrane and a shell; the shell comprises a liquid inlet, a gas inlet and a gas-liquid mixed outlet, the ceramic membrane tube is arranged in the shell, a liquid inlet of the ceramic membrane tube is connected with the liquid inlet of the shell, and a liquid outlet of the ceramic membrane tube is connected with the gas-liquid mixed outlet through the sintered membrane. When the membrane distributed gas-liquid mixer is applied, in practical application, through the combined action of the ceramic membrane tube and the sintered membrane, the gas-liquid mixing efficiency can be effectively improved, the size of bubbles is reduced, and the membrane distributed gas-liquid mixer has the advantages of being simple in structure, low in cost, high in gas-liquid mixing efficiency and small in bubble size.

Description

Technical Field

[0001] The invention relates to the technical field of gas-liquid mixers, and in particular to a membrane dispersed gas-liquid mixer and applications thereof. Background Art

[0002] There are a large number of gas-liquid reactions in the chemical industry, such as benzene hydrogenation, PX air oxidation, diesel fixed bed hydrogenation and amination reaction, etc. At the same time, it is further found in industrial application practice that compared with large bubbles, microbubbles have the advantages of small volume, large specific surface area, slow floating speed and high mass transfer efficiency. Therefore, microbubbles are widely used in the field of petrochemicals. However, the bubble diameter of traditional bubbling air oxidation reactors is generally between 5 and 30 mm, and the gas-liquid mixing efficiency is low. In many cases, it cannot effectively meet the actual application requirements. In order to further reduce the bubble diameter and improve the gas-liquid mixing efficiency, people usually increase the gas circulation volume and add reactor internal components to reduce the bubble diameter and improve the gas-liquid mixing efficiency, but the effect is very limited.

[0003] Therefore, there is an urgent need for a membrane dispersed gas-liquid mixer to effectively reduce the bubble diameter and improve the gas-liquid mixing efficiency. Summary of the invention

[0004] The purpose of the present invention is to solve the problems of large bubble diameter and low gas-liquid mixing efficiency in the gas-liquid mixer in the prior art, and to provide a membrane dispersed gas-liquid mixer and its application.

[0005] In order to achieve the above-mentioned object, the first aspect of the present invention provides a membrane dispersed gas-liquid mixer, the membrane dispersed gas-liquid mixer comprising a ceramic membrane tube, a sintered membrane and a shell;

[0006] The shell includes a liquid inlet, an air inlet and a gas-liquid mixed outlet. The ceramic diaphragm tube is arranged inside the shell. The liquid inlet of the ceramic diaphragm tube is connected to the liquid inlet of the shell, and the liquid outlet of the ceramic diaphragm tube is connected to the gas-liquid mixed outlet through the sintered diaphragm.

[0007] Preferably, the ceramic membrane tube is provided with an inner channel and a plurality of outer channels arranged around the inner channel.

[0008] Preferably, two partitions are arranged in the inner channel, and the two partitions are arranged crosswise with each other.

[0009] Preferably, the two partitions are arranged perpendicular to each other.

[0010] Preferably, the diameter of the inner channel is 0.15-0.4 times the outer diameter of the ceramic membrane tube, and the diameter of the outer channel is 0.1-0.3 times the diameter of the inner channel.

[0011] Preferably, the pore size of the ceramic membrane tube is 10 nm-10 μm, and the porosity is 30-35%.

[0012] Preferably, the pore size of the ceramic membrane tube is 200-500 nm.

[0013] Preferably, the sintered diaphragm is a stainless steel sintered diaphragm, and the precision of the stainless steel sintered diaphragm is 5-100 μm and the porosity is 70-85%.

[0014] Preferably, the precision of the stainless steel sintered metal diaphragm is 20-50 μm.

[0015] Preferably, the partition is made of polytetrafluoroethylene.

[0016] Preferably, the ceramic membrane tube is made of alumina or zirconia.

[0017] Preferably, both the liquid inlet and the liquid outlet of the ceramic membrane tube are provided with O-rings.

[0018] The second aspect of the present invention provides the use of the membrane dispersed gas-liquid mixer in gas-liquid reaction.

[0019] According to the above technical scheme, based on the membrane dispersed gas-liquid mixer, the ceramic membrane tube is arranged inside the shell, the liquid inlet of the ceramic membrane tube is connected to the liquid inlet of the shell, and the liquid outlet of the ceramic membrane tube is connected to the gas-liquid mixing outlet through the sintered diaphragm, and is further used in conjunction with a conventional gas-liquid reactor. In actual application, the average diameter of the bubbles can be effectively reduced and the gas-liquid mixing efficiency can be improved. It has the advantages of small bubble diameter and good uniformity, high gas-liquid mixing efficiency, simple mixer structure and low cost.

[0020] At the same time, by providing an inner channel on the ceramic membrane tube and a plurality of outer channels surrounding the inner channel, in practical applications, the average diameter of the bubbles can be further effectively reduced and the gas-liquid mixing efficiency can be improved; and by further providing two partitions in the inner channel, and the two partitions are arranged perpendicular to each other, the stability of the bubbles can be effectively improved while suppressing the aggregation of the bubbles.

[0021] By setting the diameter of the inner channel to 0.15-0.4 times the outer diameter of the ceramic membrane tube, the diameter of the outer channel to 0.1-0.3 times the diameter of the inner channel, and the pore size of the ceramic membrane tube to 200-500nm, and the porosity to 30-35%, in actual application, the average diameter of the bubbles can be further effectively reduced and the gas-liquid mixing efficiency and gas flux can be improved.

[0022] By setting the sintered diaphragm to be a stainless steel metal sintered diaphragm, and the precision of the stainless steel metal sintered diaphragm is 20-50μm, and the porosity is 70-85%, in the actual application process, the bubbles can be further sheared and broken to reduce the average diameter of the bubbles. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Figure 1 It is a structural schematic diagram of a membrane dispersed gas-liquid mixer;

[0024] Figure 2 It is a cross-sectional view of a ceramic membrane tube of a membrane dispersed gas-liquid mixer.

[0025] Description of Reference Numerals

[0026] 1. Liquid inlet; 2. Air inlet; 3. Ceramic membrane tube; 31. External channel; 32. Internal channel;

[0027] 33. Partition plate; 4. Sintered diaphragm; 5. Gas-liquid mixing outlet; 6. Shell. DETAILED DESCRIPTION

[0028] The specific implementation of the embodiment of the present invention is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described here is only used to illustrate and explain the embodiment of the present invention, and is not used to limit the embodiment of the present invention.

[0029] In the description of this application, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating relative importance or implicitly indicating the number of technical features indicated. Therefore, unless otherwise specified, features defined as "first" and "second" may explicitly or implicitly include one or more of the features; "plurality" means two or more. The term "include" and any variation thereof means non-exclusive inclusion, possible presence or addition of one or more other features, units, components and / or combinations thereof.

[0030] In addition, unless otherwise clearly specified and limited, the terms "installed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be internally connected between two components. For ordinary technicians in this field, the specific meanings of the above terms in this application can be understood according to specific circumstances.

[0031] The first aspect of the present invention provides a membrane dispersed gas-liquid mixer, such as Figure 1-2 As shown, the membrane dispersed gas-liquid mixer includes a ceramic membrane tube 3, a sintered membrane 4 and a shell 6;

[0032] The shell 6 includes a liquid inlet 1, an air inlet 2 and a gas-liquid mixed outlet 5. The ceramic diaphragm tube 3 is arranged inside the shell 6. The liquid inlet of the ceramic diaphragm tube 3 is connected to the liquid inlet 1 of the shell 6. The liquid outlet of the ceramic diaphragm tube 3 is connected to the gas-liquid mixed outlet 5 through the sintered diaphragm 4.

[0033] Among them, the liquid material enters the ceramic membrane tube 3 through the liquid inlet 1, and the gas material enters the interior of the shell 6 through the gas inlet 2, so that under the action of the internal and external pressure difference, the gas passes through the ceramic membrane tube 3 and is dispersed into tiny bubbles and fully contacts, mixes and reacts with the internal liquid.

[0034] According to the above technical scheme, based on the membrane dispersed gas-liquid mixer, in actual application, the diameter of the bubbles can be effectively reduced and the gas-liquid mixing efficiency can be improved. It has the advantages of small average bubble diameter and good uniformity, high gas-liquid mixing efficiency, simple mixer structure and low cost.

[0035] In the membrane dispersed gas-liquid mixer of the present invention, preferably, the ceramic membrane tube 3 is provided with an inner channel 32 and a plurality of outer channels 31 arranged around the inner channel 32. The number of the outer channels 31 may be 6-20, preferably 8-16, and most preferably 10-15.

[0036] In a specific embodiment, Figure 2 As shown, by opening a penetrating inner channel 32 on the axis of the ceramic membrane tube 3, and arranging a plurality of (e.g., 12) penetrating outer channels 31 around the inner channel 32 at preset intervals, in actual application, the average size of the bubbles can be effectively reduced and the mixing efficiency between gas and liquid can be improved.

[0037] In a further preferred embodiment, two baffles 33 are arranged in the inner channel 32, and the two baffles 33 are arranged crosswise. More preferably, the two baffles 33 are arranged perpendicular to each other. Thus, in practical application, the stability of bubbles can be effectively improved while suppressing the coalescence of bubbles. The baffles 33 are made of polytetrafluoroethylene, which can further suppress the coalescence of bubbles and improve the stability of bubbles.

[0038] In a further preferred embodiment, the diameter of the inner channel 32 is 0.15-0.4 times the outer diameter of the ceramic membrane tube 3, and the diameter of the outer channel 31 is 0.1-0.3 times the diameter of the inner channel 32. In practical applications, the diameter of the bubbles can be further effectively reduced and the gas-liquid mixing efficiency and gas flux can be improved. In a specific embodiment, the diameter of the outer channel 31 is preferably 2-8 mm, and more preferably 4-6 mm.

[0039] In a further preferred embodiment, the pore size of the ceramic membrane tube 3 is 10nm-10μm, and the porosity is 30-35%. Thereby further effectively reducing the diameter of the bubbles and improving the mixing efficiency between gas and liquid. Preferably, the pore size of the ceramic membrane tube 3 is 200-500nm. Among them, the ceramic membrane tube 3 is made of aluminum oxide or zirconium oxide, which has the advantages of good stability, corrosion resistance, high temperature resistance and not easy to oxidize in practical applications. The liquid inlet and outlet of the ceramic membrane tube 3 are both provided with O-rings, which can ensure air tightness while facilitating connection with other device pipelines.

[0040] In the membrane dispersed gas-liquid mixer of the present invention, preferably, the sintered membrane 4 is a stainless steel sintered membrane, and the precision of the stainless steel sintered membrane is 5-100 μm, and the porosity is 70-85%. Therefore, in the actual application process, the average diameter of the bubbles can be further reduced by shearing and crushing the bubbles. More preferably, the precision of the stainless steel sintered membrane is 20-50 μm.

[0041] In some embodiments, the membrane dispersed gas-liquid mixer described in the present invention includes a ceramic membrane tube 3, a sintered diaphragm 4 and a shell 6; the shell 6 includes a liquid inlet 1, an air inlet 2 and a gas-liquid mixing outlet 5, the ceramic membrane tube 3 is arranged inside the shell 6, the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the shell 6, and the liquid outlet of the ceramic membrane tube 3 is connected to the gas-liquid mixing outlet 5 through the sintered diaphragm 4.

[0042] In other embodiments, the membrane dispersed gas-liquid mixer described in the present invention includes a ceramic diaphragm tube 3, a sintered diaphragm 4 and a shell 6; the shell 6 includes a liquid inlet 1, an air inlet 2 and a gas-liquid mixing outlet 5, the ceramic diaphragm tube 3 is arranged inside the shell 6, the liquid inlet of the ceramic diaphragm tube 3 is connected to the liquid inlet 1 of the shell 6, and the liquid outlet of the ceramic diaphragm tube 3 is connected to the gas-liquid mixing outlet 5 through the sintered diaphragm 4; the ceramic diaphragm tube 3 is made of aluminum oxide or zirconium oxide; the ceramic diaphragm tube 3 is provided with an inner channel 32 and a plurality of outer channels 31 arranged around the inner channel 32.

[0043] In other embodiments, the membrane dispersed gas-liquid mixer described in the present invention includes a ceramic membrane tube 3, a sintered diaphragm 4 and a shell 6; the shell 6 includes a liquid inlet 1, an air inlet 2 and a gas-liquid mixing outlet 5, the ceramic membrane tube 3 is arranged inside the shell 6, the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the shell 6, and the liquid outlet of the ceramic membrane tube 3 is connected to the gas-liquid mixing outlet 5 through the sintered diaphragm 4; the ceramic membrane tube 3 is made of aluminum oxide or zirconium oxide; the ceramic membrane tube 3 is provided with an inner channel 32 and a plurality of outer channels 31 arranged around the inner channel 32; two partitions 33 are arranged in the inner channel 32, and the two partitions 33 are arranged crosswise with each other.

[0044] In other embodiments, the membrane dispersed gas-liquid mixer described in the present invention includes a ceramic membrane tube 3, a sintered diaphragm 4 and a shell 6; the shell 6 includes a liquid inlet 1, an air inlet 2 and a gas-liquid mixing outlet 5, the ceramic membrane tube 3 is arranged inside the shell 6, the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the shell 6, and the liquid outlet of the ceramic membrane tube 3 is connected to the gas-liquid mixing outlet 5 through the sintered diaphragm 4; the ceramic membrane tube 3 is made of aluminum oxide or zirconium oxide; the ceramic membrane tube 3 is provided with an inner channel 32 and a plurality of outer channels 31 arranged around the inner channel 32; two partitions 33 are arranged in the inner channel 32, and the two partitions 33 are arranged crosswise with each other; the two partitions 33 are arranged perpendicular to each other; the partitions 33 are made of polytetrafluoroethylene.

[0045] In other embodiments, the membrane dispersed gas-liquid mixer described in the present invention includes a ceramic membrane tube 3, a sintered diaphragm 4 and a shell 6; the shell 6 includes a liquid inlet 1, an air inlet 2 and a gas-liquid mixing outlet 5, the ceramic membrane tube 3 is arranged inside the shell 6, the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the shell 6, and the liquid outlet of the ceramic membrane tube 3 is connected to the gas-liquid mixing outlet 5 through the sintered diaphragm 4; the ceramic membrane tube 3 is made of aluminum oxide or zirconium oxide; the ceramic membrane tube 3 is provided with an inner channel 32 and a plurality of outer channels 31 arranged around the inner channel 32; two partitions 33 are arranged in the inner channel 32, and the two partitions 33 are arranged crosswise with each other; the two partitions 33 are arranged perpendicular to each other; the partitions 33 are made of polytetrafluoroethylene; the pore size of the ceramic membrane tube 3 is 10nm-10μm, and the porosity is 30-35%.

[0046] In other embodiments, the membrane dispersed gas-liquid mixer described in the present invention includes a ceramic membrane tube 3, a sintered diaphragm 4 and a shell 6; the shell 6 includes a liquid inlet 1, an air inlet 2 and a gas-liquid mixing outlet 5, the ceramic membrane tube 3 is arranged inside the shell 6, the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the shell 6, and the liquid outlet of the ceramic membrane tube 3 is connected to the gas-liquid mixing outlet 5 through the sintered diaphragm 4; the ceramic membrane tube 3 is made of aluminum oxide or zirconium oxide; the ceramic membrane tube 3 is provided with an inner channel 32 and a plurality of outer channels 31 arranged around the inner channel 32; two partitions 33 are arranged in the inner channel 32, and the two partitions 33 are arranged crosswise with each other; the two partitions 33 are arranged perpendicular to each other; the partition 33 is made of polytetrafluoroethylene; the diameter of the inner channel 32 is 0.15-0.4 times the outer diameter of the ceramic membrane tube 3, and the diameter of the outer channel 31 is 0.1-0.3 times the diameter of the inner channel 32.

[0047] In other embodiments, the membrane dispersed gas-liquid mixer of the present invention comprises a ceramic membrane tube 3, a sintered membrane sheet 4 and a shell 6; the shell 6 comprises a liquid inlet 1, a gas inlet 2 and a gas-liquid mixing outlet 5, the ceramic membrane tube 3 is arranged inside the shell 6, the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the shell 6, and the liquid outlet of the ceramic membrane tube 3 is connected to the gas-liquid mixing outlet 5 through the sintered membrane sheet 4; the ceramic membrane tube 3 is made of alumina or zirconium oxide; an inner channel 3 is provided on the ceramic membrane tube 3 2 and a plurality of outer channels 31 arranged around the inner channel 32; two partitions 33 are arranged in the inner channel 32, and the two partitions 33 are arranged crosswise; the two partitions 33 are arranged perpendicular to each other; the partitions 33 are made of polytetrafluoroethylene; the diameter of the inner channel 32 is 0.15-0.4 times the outer diameter of the ceramic membrane tube 3, and the diameter of the outer channel 31 is 0.1-0.3 times the diameter of the inner channel 32; the pore size of the ceramic membrane tube 3 is 10nm-10μm, and the porosity is 30-35%.

[0048] In other embodiments, the membrane dispersed gas-liquid mixer described in the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4 and a shell 6; the shell 6 includes a liquid inlet 1, an air inlet 2 and a gas-liquid mixing outlet 5, the ceramic membrane tube 3 is arranged inside the shell 6, the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the shell 6, and the liquid outlet of the ceramic membrane tube 3 is connected to the gas-liquid mixing outlet 5 through the sintered membrane sheet 4; the ceramic membrane tube 3 is made of alumina or zirconium oxide; the ceramic membrane tube 3 is provided with an inner channel 32 and a surrounding portion of the inner channel 3 2 is provided with a plurality of outer channels 31; two partitions 33 are provided in the inner channel 32, and the two partitions 33 are cross-arranged; the two partitions 33 are arranged perpendicular to each other; the partitions 33 are made of polytetrafluoroethylene; the diameter of the inner channel 32 is 0.15-0.4 times the outer diameter of the ceramic membrane tube 3, and the diameter of the outer channel 31 is 0.1-0.3 times the diameter of the inner channel 32; the sintered diaphragm 4 is a stainless steel metal sintered diaphragm, and the precision of the stainless steel metal sintered diaphragm is 20-50μm, and the porosity is 70-85%.

[0049] In other embodiments, the membrane dispersed gas-liquid mixer described in the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4 and a shell 6; the shell 6 includes a liquid inlet 1, an air inlet 2 and a gas-liquid mixing outlet 5, the ceramic membrane tube 3 is arranged inside the shell 6, the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the shell 6, and the liquid outlet of the ceramic membrane tube 3 is connected to the gas-liquid mixing outlet 5 through the sintered membrane sheet 4; the ceramic membrane tube 3 is made of alumina or zirconia; the ceramic membrane tube 3 is provided with a An inner channel 32 and a plurality of outer channels 31 arranged around the inner channel 32; two partitions 33 are arranged in the inner channel 32, and the two partitions 33 are arranged crosswise with each other; the two partitions 33 are arranged perpendicular to each other; the partitions 33 are made of polytetrafluoroethylene; the pore size of the ceramic membrane tube 3 is 10nm-10μm, and the porosity is 30-35%; the sintered diaphragm 4 is a stainless steel metal sintered diaphragm, and the precision of the stainless steel metal sintered diaphragm is 5-100μm, and the porosity is 70-85%.

[0050] In other embodiments, the membrane dispersed gas-liquid mixer of the present invention comprises a ceramic membrane tube 3, a sintered membrane sheet 4 and a shell 6; the shell 6 comprises a liquid inlet 1, a gas inlet 2 and a gas-liquid mixing outlet 5, the ceramic membrane tube 3 is arranged inside the shell 6, the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the shell 6, and the liquid outlet of the ceramic membrane tube 3 is connected to the gas-liquid mixing outlet 5 through the sintered membrane sheet 4; the ceramic membrane tube 3 is made of alumina or zirconium oxide; an inner channel 3 is provided on the ceramic membrane tube 3 2 and a plurality of outer channels 31 arranged around the inner channel 32; two partitions 33 are arranged in the inner channel 32, and the two partitions 33 are arranged crosswise; the two partitions 33 are arranged perpendicular to each other; the partitions 33 are made of polytetrafluoroethylene; the diameter of the inner channel 32 is 0.15-0.4 times the outer diameter of the ceramic membrane tube 3, and the diameter of the outer channel 31 is 0.1-0.3 times the diameter of the inner channel 32; the pore size of the ceramic membrane tube 3 is 200-500nm, and the porosity is 30-35%.

[0051] In other embodiments, the membrane dispersed gas-liquid mixer described in the present invention includes a ceramic membrane tube 3, a sintered diaphragm 4 and a shell 6; the shell 6 includes a liquid inlet 1, an air inlet 2 and a gas-liquid mixing outlet 5, the ceramic membrane tube 3 is arranged inside the shell 6, the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the shell 6, and the liquid outlet of the ceramic membrane tube 3 is connected to the gas-liquid mixing outlet 5 through the sintered diaphragm 4; the ceramic membrane tube 3 is made of aluminum oxide or zirconium oxide; the ceramic membrane tube 3 is provided with an inner channel 32 and a plurality of outer channels 31 arranged around the inner channel 32; the inner Two partitions 33 are arranged in the channel 32, and the two partitions 33 are arranged crosswise with each other; the two partitions 33 are arranged perpendicular to each other; the partitions 33 are made of polytetrafluoroethylene; the diameter of the inner channel 32 is 0.15-0.4 times the outer diameter of the ceramic membrane tube 3, and the diameter of the outer channel 31 is 0.1-0.3 times the diameter of the inner channel 32; the pore size of the ceramic membrane tube 3 is 200-500nm, and the porosity is 30-35%; the sintered diaphragm 4 is a stainless steel metal sintered diaphragm, and the precision of the stainless steel metal sintered diaphragm is 5-100μm, and the porosity is 70-85%.

[0052] In other embodiments, the membrane dispersed gas-liquid mixer described in the present invention includes a ceramic membrane tube 3, a sintered diaphragm 4 and a shell 6; the shell 6 includes a liquid inlet 1, an air inlet 2 and a gas-liquid mixing outlet 5, the ceramic membrane tube 3 is arranged inside the shell 6, the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the shell 6, and the liquid outlet of the ceramic membrane tube 3 is connected to the gas-liquid mixing outlet 5 through the sintered diaphragm 4; the ceramic membrane tube 3 is made of aluminum oxide or zirconium oxide; the ceramic membrane tube 3 is provided with an inner channel 32 and a plurality of outer channels 31 arranged around the inner channel 32; the inner Two partitions 33 are arranged in the channel 32, and the two partitions 33 are arranged crosswise with each other; the two partitions 33 are arranged perpendicular to each other; the partitions 33 are made of polytetrafluoroethylene; the diameter of the inner channel 32 is 0.15-0.4 times the outer diameter of the ceramic membrane tube 3, and the diameter of the outer channel 31 is 0.1-0.3 times the diameter of the inner channel 32; the pore size of the ceramic membrane tube 3 is 200-500nm, and the porosity is 30-35%; the sintered diaphragm 4 is a stainless steel metal sintered diaphragm, and the precision of the stainless steel metal sintered diaphragm is 20-50μm, and the porosity is 70-85%.

[0053] The second aspect of the present invention provides the use of the membrane dispersed gas-liquid mixer described above in a gas-liquid reaction, wherein the gas-liquid reaction may be cyclohexane air oxidation, diesel hydrogenation, toluene fluorination, and the like.

[0054] The present invention will be described in detail below through examples, but the protection scope of the present invention is not limited thereto.

[0055] Use Figure 1-2 The membrane dispersed gas-liquid mixer shown is implemented, specifically, the membrane dispersed gas-liquid mixer includes a ceramic membrane tube 3, a sintered membrane 4 and a shell 6;

[0056] The shell 6 includes a liquid inlet 1, a gas inlet 2 and a gas-liquid mixed outlet 5, the ceramic membrane tube 3 is arranged inside the shell 6, the liquid inlet of the ceramic membrane tube 3 is connected to 1 of the liquid inlet shell 6, and the liquid outlet of the ceramic membrane tube 3 is connected to the gas-liquid mixed outlet 5 through the sintered membrane 4;

[0057] The ceramic membrane tube 3 is provided with an inner channel 32 and 12 outer channels 31 arranged around the inner channel 32; two partitions 33 are arranged in the inner channel 32, and the two partitions 33 are arranged perpendicular to each other; the diameter of the inner channel 32 is 0.15-0.4 times the outer diameter of the ceramic membrane tube 3, and the diameter of the outer channel 31 is 0.1-0.3 times the diameter of the inner channel 32; the pore size of the ceramic membrane tube 3 is 10nm-10μm, and the porosity is 34%; the sintered diaphragm 4 is a stainless steel metal sintered diaphragm, and the precision of the stainless steel metal sintered diaphragm is 5-100μm, and the porosity is 80%; the partition 33 is made of polytetrafluoroethylene; the ceramic membrane tube 3 is made of alumina or zirconia, and has a diameter of 40mm.

[0058] Example 1

[0059] The outer channel diameter of the ceramic membrane tube is 2mm, the pore size is 200nm, the precision of the stainless steel metal sintered diaphragm is 20μm. In actual application, the water flow rate entering the inner channel and the outer channel is set to 2L / min, and the gas flow rate entering the shell is 1L / min; the membrane dispersed gas-liquid mixer is fixed to the bottom of an acrylic transparent square cylinder (length and width of 50mm, height of 2m, that is, a conventional mixer).

[0060] After testing, the air was quickly dispersed in the water after being mixed by the membrane dispersed gas-liquid mixer, and formed an emulsion in the acrylic transparent square tube, which flowed out from the top, and after gas-liquid phase separation, the liquid was circulated and fed. After the bubble flow was stable, it was photographed at a height of 0.2m, 1m, and 2m using a high-speed camera, and the size was characterized. At this time, the transmembrane pressure difference was 0.34MPa, and densely dispersed tiny bubble groups were observed, with an average bubble diameter of about 468μm, and no obvious aggregation occurred within a height of 2m.

[0061] Example 2

[0062] The outer channel diameter of the ceramic membrane tube is 4 mm, the pore size is 200 nm, the precision of the stainless steel metal sintered diaphragm is 20 μm. In actual application, the water flow rate entering the inner channel and the outer channel is set to 2 L / min, and the gas flow rate entering the shell is 1 L / min; the membrane dispersed gas-liquid mixer is fixed to the bottom of an acrylic transparent square cylinder (length and width of 50 mm, height of 2 m, that is, a conventional mixer).

[0063] After testing, the air was quickly dispersed in the water after being mixed by the membrane dispersed gas-liquid mixer, and formed an emulsion in the acrylic transparent square tube, which flowed out from the top, and after gas-liquid phase separation, the liquid was circulated and fed. After the bubble flow was stable, it was photographed at a height of 0.2m, 1m, and 2m using a high-speed camera, and the size was characterized. At this time, the transmembrane pressure difference was 0.33MPa, and densely dispersed tiny bubble groups were observed, with an average bubble diameter of about 320μm, and no obvious aggregation occurred within a height of 2m.

[0064] Example 3

[0065] The outer channel diameter of the ceramic membrane tube is 6 mm, the pore size is 200 nm, the precision of the stainless steel metal sintered diaphragm is 20 μm. In actual application, the water flow rate entering the inner channel and the outer channel is set to 2 L / min, and the gas flow rate entering the shell is 1 L / min; the membrane dispersed gas-liquid mixer is fixed to the bottom of an acrylic transparent square cylinder (length and width of 50 mm, height of 2 m, that is, a conventional mixer).

[0066] After testing, the air was quickly dispersed in the water after being mixed by the membrane dispersed gas-liquid mixer, and formed an emulsion in the acrylic transparent square tube, which flowed out from the top, and after gas-liquid phase separation, the liquid was circulated and fed. After the bubble flow was stable, it was photographed at a height of 0.2m, 1m, and 2m using a high-speed camera, and the size was characterized. At this time, the transmembrane pressure difference was 0.30MPa, and densely dispersed tiny bubble groups were observed, with an average bubble diameter of about 292μm, and no obvious aggregation occurred within a height of 2m.

[0067] Example 4

[0068] The outer channel diameter of the ceramic membrane tube is 8 mm, the pore size is 200 nm, the precision of the stainless steel metal sintered diaphragm is 20 μm. In actual application, the water flow rate entering the inner channel and the outer channel is set to 2 L / min, and the gas flow rate entering the shell is 1 L / min; the membrane dispersed gas-liquid mixer is fixed to the bottom of an acrylic transparent square cylinder (length and width of 50 mm, height of 2 m, that is, a conventional mixer).

[0069] After testing, the air was quickly dispersed in the water after being mixed by the membrane dispersed gas-liquid mixer, and formed an emulsion in the acrylic transparent square tube, which flowed out from the top, and after gas-liquid phase separation, the liquid was circulated and fed. After the bubble flow was stable, it was photographed at a height of 0.2m, 1m, and 2m using a high-speed camera, and the size was characterized. At this time, the transmembrane pressure difference was 0.28MPa, and densely dispersed tiny bubble groups were observed, with an average bubble diameter of about 358μm, and no obvious aggregation occurred within a height of 2m.

[0070] Example 5

[0071] The outer channel diameter of the ceramic membrane tube is 4 mm, the pore size is 50 nm, the precision of the stainless steel metal sintered diaphragm is 20 μm. In actual application, the water flow rate entering the inner channel and the outer channel is set to 2 L / min, and the gas flow rate entering the shell is 1 L / min; the membrane dispersed gas-liquid mixer is fixed to the bottom of an acrylic transparent square cylinder (length and width of 50 mm, height of 2 m, that is, a conventional mixer).

[0072] After testing, the air was quickly dispersed in the water after being mixed by the membrane dispersed gas-liquid mixer, and formed an emulsion in the acrylic transparent square tube, which flowed out from the top, and after gas-liquid phase separation, the liquid was circulated and fed. After the bubble flow was stable, it was photographed at 0.2m, 1m, and 2m heights using a high-speed camera, and the size was characterized. At this time, the transmembrane pressure difference was 0.60MPa, and densely dispersed micro-bubble groups were observed, with an average bubble diameter of about 150μm, and no obvious aggregation occurred within a height of 2m. However, due to the high transmembrane pressure difference, reaching 0.60MPa, the micro-bubble production was significantly reduced.

[0073] Example 6

[0074] The outer channel diameter of the ceramic membrane tube is 4 mm, the pore size is 500 nm, the precision of the stainless steel metal sintered diaphragm is 20 μm. In actual application, the water flow rate entering the inner channel and the outer channel is set to 2 L / min, and the gas flow rate entering the shell is 1 L / min; the membrane dispersed gas-liquid mixer is fixed to the bottom of an acrylic transparent square cylinder (length and width of 50 mm, height of 2 m, that is, a conventional mixer).

[0075] After testing, the air was quickly dispersed in the water after being mixed by the membrane dispersed gas-liquid mixer, and formed an emulsion in the acrylic transparent square tube, which flowed out from the top, and after gas-liquid phase separation, the liquid was circulated and fed. After the bubble flow was stable, it was photographed at a height of 0.2m, 1m, and 2m using a high-speed camera, and the size was characterized. At this time, the transmembrane pressure difference was 0.30MPa, and densely dispersed tiny bubble groups were observed, with an average bubble diameter of about 450μm, and no obvious aggregation occurred within a height of 2m.

[0076] Example 7

[0077] The outer channel diameter of the ceramic membrane tube is 4 mm, the pore size is 5 μm, the precision of the stainless steel metal sintered diaphragm is 20 μm. In actual application, the water flow rate entering the inner channel and the outer channel is set to 2 L / min, and the gas flow rate entering the shell is 1 L / min; the membrane dispersed gas-liquid mixer is fixed to the bottom of an acrylic transparent square cylinder (length and width of 50 mm, height of 2 m, that is, a conventional mixer).

[0078] After testing, the air was quickly dispersed in the water after being mixed by the membrane dispersed gas-liquid mixer, and formed an emulsion in the acrylic transparent square tube, which flowed out from the top, and after gas-liquid phase separation, the liquid was circulated and fed. After the bubble flow was stable, it was photographed at a height of 0.2m, 1m, and 2m using a high-speed camera, and the size was characterized. At this time, the transmembrane pressure difference was 0.25MPa, and densely dispersed tiny bubble groups were observed, with an average bubble diameter of about 685μm, and no obvious aggregation occurred within a height of 2m.

[0079] Example 8

[0080] The outer channel diameter of the ceramic membrane tube is 4 mm, the pore size is 200 nm, the precision of the stainless steel metal sintered diaphragm is 5 μm. In actual application, the water flow rate entering the inner channel and the outer channel is set to 2 L / min, and the gas flow rate entering the shell is 1 L / min; the membrane dispersed gas-liquid mixer is fixed to the bottom of an acrylic transparent square cylinder (length and width of 50 mm, height of 2 m, that is, a conventional mixer).

[0081] After testing, the air was quickly dispersed in the water after being mixed by the membrane dispersed gas-liquid mixer, and formed an emulsion in the acrylic transparent square tube, which flowed out from the top, and after gas-liquid phase separation, the liquid was circulated and fed. After the bubble flow was stable, it was photographed with a high-speed camera at heights of 0.2m, 1m, and 2m, and the size was characterized. At this time, the transmembrane pressure difference was 0.54MPa, and densely dispersed micro-bubble groups were observed, with an average bubble diameter of about 258μm, and no obvious aggregation occurred within a height of 2m. However, due to the high transmembrane pressure difference, reaching 0.54MPa, the micro-bubble production was significantly reduced.

[0082] Example 9

[0083] The outer channel diameter of the ceramic membrane tube is 4 mm, the pore size is 200 nm, the precision of the stainless steel metal sintered diaphragm is 50 μm. In actual application, the water flow rate entering the inner channel and the outer channel is set to 2 L / min, and the gas flow rate entering the shell is 1 L / min; the membrane dispersed gas-liquid mixer is fixed to the bottom of an acrylic transparent square cylinder (length and width of 50 mm, height of 2 m, that is, a conventional mixer).

[0084] After testing, the air was quickly dispersed in the water after being mixed by the membrane dispersed gas-liquid mixer, and formed an emulsion in the acrylic transparent square tube, which flowed out from the top, and after gas-liquid phase separation, the liquid was circulated and fed. After the bubble flow was stable, it was photographed at a height of 0.2m, 1m, and 2m using a high-speed camera, and the size was characterized. At this time, the transmembrane pressure difference was 0.32MPa, and densely dispersed tiny bubble groups were observed, with an average bubble diameter of about 445μm, and no obvious aggregation occurred within a height of 2m.

[0085] Example 10

[0086] The outer channel diameter of the ceramic membrane tube is 4 mm, the pore size is 200 nm, the precision of the stainless steel metal sintered diaphragm is 80 μm. In actual application, the water flow rate entering the inner channel and the outer channel is set to 2 L / min, and the gas flow rate entering the shell is 1 L / min; the membrane dispersed gas-liquid mixer is fixed to the bottom of an acrylic transparent square cylinder (length and width of 50 mm, height of 2 m, that is, a conventional mixer).

[0087] After testing, the air was quickly dispersed in the water after being mixed by the membrane dispersed gas-liquid mixer, and formed an emulsion in the acrylic transparent square tube, which flowed out from the top, and after gas-liquid phase separation, the liquid was circulated and fed. After the bubble flow was stable, it was photographed at a height of 0.2m, 1m, and 2m using a high-speed camera, and the size was characterized. At this time, the transmembrane pressure difference was 0.30MPa, and densely dispersed tiny bubble groups were observed, with an average bubble diameter of about 612μm, and no obvious aggregation occurred within a height of 2m.

[0088] Comparative Example 1

[0089] An acrylic transparent square cylinder (length and width of 50 mm, height of 2 m) was filled with water, and air was directly introduced into the bottom with a flow rate of 1 L / min.

[0090] After testing, when the bubble flow stabilized, high-speed cameras were used to shoot at heights of 0.2m, 1m, and 2m, and the size was characterized. Millimeter-sized bubbles were observed, and the bubble rising process was not significant, with an average bubble diameter of about 8mm.

[0091] Further, based on the above Examples 1-10, the data results are shown in Table 1 below.

[0092] Table 1

[0093]

[0094]

[0095] It can be seen from Table 1 above that, preferably, when the diameter of the 12 outer channels of the ceramic membrane tube is 4-6 mm, the pore size is 200-500 nm, and the precision of the stainless steel metal sintered diaphragm is 20-50 μm, the average diameter of the bubbles can be effectively reduced, specifically to the micron level, while making the transmembrane pressure difference of the membrane dispersed gas-liquid mixer less than 0.35 MPa. Finally, compared with the scheme in Comparative Example 1, while effectively reducing the average diameter of the bubbles, the yield of microbubbles is also effectively increased.

[0096] The membrane dispersed gas-liquid mixer provided by the present invention is configured such that the ceramic membrane tube is disposed inside the shell, the liquid inlet of the ceramic membrane tube is connected to the liquid inlet, the liquid outlet of the ceramic membrane tube is connected to the gas-liquid mixing outlet through the sintered membrane, and is further used in conjunction with a conventional gas-liquid reactor. In actual application, the diameter of the bubbles can be effectively reduced and the mixing efficiency can be improved. The mixer has the advantages of small bubble diameter and good uniformity, high mixing efficiency, simple mixer structure and low cost.

[0097] The preferred embodiments of the present invention are described in detail above with reference to the accompanying drawings, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications. In order to avoid unnecessary repetition, the present invention will not further describe various possible combinations. However, these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to the protection scope of the present invention.

Claims

1. A membrane dispersed gas-liquid mixer, characterized in that: The membrane dispersed gas-liquid mixer comprises a ceramic membrane tube (3), a sintered membrane sheet (4) and a shell (6); The shell (6) comprises a liquid inlet (1), an air inlet (2) and a gas-liquid mixed outlet (5); the ceramic membrane tube (3) is arranged inside the shell (6); the liquid inlet of the ceramic membrane tube (3) is connected to the liquid inlet (1) of the shell (6); and the liquid outlet of the ceramic membrane tube (3) is connected to the gas-liquid mixed outlet (5) through the sintered membrane (4).

2. The membrane dispersed gas-liquid mixer according to claim 1, characterized in that: The ceramic membrane tube (3) is provided with an inner channel (32) and a plurality of outer channels (31) arranged around the inner channel (32).

3. The membrane dispersed gas-liquid mixer according to claim 2, characterized in that: Two partitions (33) are arranged in the inner channel (32), and the two partitions (33) are arranged to cross each other.

4. The membrane dispersed gas-liquid mixer according to claim 3, characterized in that: The two partitions (33) are arranged perpendicular to each other.

5. The membrane dispersed gas-liquid mixer according to claim 2, characterized in that: The diameter of the inner channel (32) is 0.15-0.4 times the outer diameter of the ceramic membrane tube (3), and the diameter of the outer channel (31) is 0.1-0.3 times the diameter of the inner channel (32).

6. The membrane dispersed gas-liquid mixer according to any one of claims 1 to 5, characterized in that: The pore size of the ceramic membrane tube (3) is 10 nm-10 μm, and the porosity is 30-35%.

7. The membrane dispersed gas-liquid mixer according to claim 6, characterized in that: The pore size of the ceramic membrane tube (3) is 200-500 nm.

8. The membrane dispersed gas-liquid mixer according to claim 1 or 7, characterized in that: The sintered diaphragm (4) is a stainless steel sintered diaphragm, and the precision of the stainless steel sintered diaphragm is 5-100 μm, and the porosity is 70-85%.

9. The membrane dispersed gas-liquid mixer according to claim 8, characterized in that: The precision of the stainless steel sintered metal diaphragm is 20-50 μm.

10. The membrane dispersed gas-liquid mixer according to claim 3, characterized in that: The partition plate (33) is made of polytetrafluoroethylene.

11. The membrane dispersed gas-liquid mixer according to claim 1, characterized in that: The ceramic membrane tube (3) is made of aluminum oxide or zirconium oxide.

12. The membrane dispersed gas-liquid mixer according to claim 1 or 11, characterized in that: The liquid inlet and the liquid outlet of the ceramic membrane tube (3) are both provided with O-type sealing rings.

13. Use of the membrane dispersed gas-liquid mixer according to any one of claims 1 to 12 in a gas-liquid reaction.

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