A membrane dispersion gas-liquid mixer and its application

Abstract

This invention relates to the field of gas-liquid mixer technology, specifically to a membrane dispersion gas-liquid mixer and its application. The membrane dispersion gas-liquid mixer includes a ceramic membrane tube, a sintered membrane sheet, and a housing. The housing includes a liquid inlet, a gas inlet, and a gas-liquid mixing outlet. The ceramic membrane tube is disposed inside the housing, with its liquid inlet connected to the liquid inlet of the housing, and its liquid outlet connected to the gas-liquid mixing outlet via the sintered membrane sheet. In practical applications, this membrane dispersion gas-liquid mixer, through the combined action of the ceramic membrane tube and the sintered membrane sheet, can effectively improve gas-liquid mixing efficiency and reduce bubble size, offering advantages such as simple structure, low cost, high gas-liquid mixing efficiency, and small bubble size.

Description

Technical Field

[0001] This invention relates to the field of gas-liquid mixer technology, and more specifically to a membrane dispersion gas-liquid mixer and its application. Background Technology

[0002] Numerous gas-liquid reactions occur in the chemical industry, such as benzene hydrogenation, PX air oxidation, diesel fixed-bed hydrogenation, and amination reactions. Furthermore, practical industrial applications have revealed that microbubbles, compared to large bubbles, possess advantages such as small volume, large specific surface area, slow rising velocity, and high mass transfer efficiency. Therefore, microbubbles are widely used in the petrochemical field. However, the bubble diameter in traditional bubble-type air oxidation reactors is generally between 5 and 30 mm, and the gas-liquid mixing efficiency is relatively low. In many cases, this cannot effectively meet practical application requirements. To further reduce the bubble diameter and improve gas-liquid mixing efficiency, methods such as increasing the gas circulation volume and adding internal reactor components are commonly used, but the effects are quite limited.

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

[0004] The purpose of this invention is to solve the problems of large bubble diameter and low gas-liquid mixing efficiency in existing gas-liquid mixers, and to provide a membrane dispersion gas-liquid mixer and its application.

[0005] To achieve the above objectives, the first aspect of the present invention provides a membrane dispersion gas-liquid mixer, which includes a ceramic membrane tube, a sintered membrane sheet, and a shell;

[0006] The housing includes a liquid inlet, an air inlet, and a gas-liquid mixing outlet. The ceramic membrane tube is disposed inside the housing. The liquid inlet of the ceramic membrane tube is connected to the liquid inlet of the housing, and the liquid outlet of the ceramic membrane tube is connected to the gas-liquid mixing outlet through the sintered membrane.

[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, the inner channel is provided with two partitions, and the two partitions are arranged to cross 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 ceramic membrane tube has a pore size of 10 nm-10 μm and a porosity of 30-35%.

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

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

[0014] Preferably, the stainless steel sintered metal film has a precision of 20-50 μm.

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

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

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

[0018] The second aspect of the present invention provides the application of the membrane dispersion gas-liquid mixer in gas-liquid reactions.

[0019] According to the above technical solution, based on this membrane dispersion gas-liquid mixer, the ceramic membrane tube is set 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 membrane. It can be used in conjunction with a conventional gas-liquid reactor. In practical applications, it can effectively reduce the average diameter of bubbles and improve the gas-liquid mixing efficiency. It has the advantages of small bubble diameter and good uniformity, high gas-liquid mixing efficiency, simple mixer structure and low cost.

[0020] Meanwhile, by setting an inner channel and several outer channels surrounding the inner channel on the ceramic membrane tube, the average diameter of the bubbles can be further reduced and the gas-liquid mixing efficiency can be improved in practical applications. Furthermore, by setting two baffles in the inner channel and setting the two baffles perpendicular to each other, the stability of the bubbles can be effectively improved while suppressing bubble coalescence.

[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 200-500 nm with a porosity of 30-35%, the average diameter of the bubbles can be further effectively reduced and the gas-liquid mixing efficiency and gas flux can be improved in practical applications.

[0022] By setting the sintered film to be a stainless steel sintered film, and the stainless steel sintered film has a precision of 20-50μm and a porosity of 70-85%, the average diameter of the bubbles can be further reduced by shearing and breaking the bubbles in practical applications. Attached Figure Description

[0023] Figure 1 This is a schematic diagram of a membrane dispersion gas-liquid mixer;

[0024] Figure 2 This is a cross-sectional view of the ceramic membrane tube of a membrane dispersion gas-liquid mixer.

[0025] Explanation of reference numerals in the attached figures

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

[0027] 33. Partition plate; 4. Sintered membrane; 5. Gas-liquid mixing outlet; 6. Shell. Detailed Implementation

[0028] The specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for illustration and explanation only and are not intended to limit the scope 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 construed as indicating relative importance or implying the number of indicated technical features. Therefore, unless otherwise stated, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature; "multiple" means two or more. The term "comprising" and any variations thereof mean a non-exclusive inclusion, the possibility of the presence or addition of one or more other features, units, components, and / or combinations thereof.

[0030] Furthermore, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. For example, they can refer to fixed connections, detachable connections, or integral connections; they can refer to mechanical connections or electrical connections; they can refer to direct connections or indirect connections through an intermediate medium, or internal connections between two components. Those skilled in the art can understand the specific meaning of the above terms in this application based on the specific circumstances.

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

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

[0033] Liquid material enters the ceramic membrane tube 3 through the liquid inlet 1, while gaseous material enters the interior of the shell 6 through the gas inlet 2. Under the action of the internal and external pressure difference, the gas is dispersed into tiny bubbles through the ceramic membrane tube 3 and fully contacts, mixes and reacts with the liquid inside.

[0034] According to the above technical solution, based on this membrane dispersion gas-liquid mixer, in practical applications, the diameter of 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 dispersion 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 outer channels 31 can be 6-20, preferably 8-16, and most preferably 10-15.

[0036] In specific implementation methods, such as Figure 2 As shown, by opening a through inner channel 32 on the axis of the ceramic membrane tube 3, and setting a number of (e.g., 12) through outer channels 31 around the inner channel 32 at preset intervals, the average size of the bubbles can be effectively reduced and the mixing efficiency between gas and liquid can be improved in practical applications.

[0037] In a further preferred embodiment, two partitions 33 are provided within the inner channel 32, and the two partitions 33 are arranged intersecting each other. More preferably, the two partitions 33 are arranged perpendicular to each other. Thus, in practical applications, the stability of bubbles can be effectively improved while suppressing bubble coalescence. The partitions 33 are made of polytetrafluoroethylene, which further suppresses bubble coalescence and improves bubble stability.

[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, this can further effectively reduce the bubble diameter and improve gas-liquid mixing efficiency and gas throughput. 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 ceramic membrane tube 3 has a pore size of 10 nm-10 μm and a porosity of 30-35%. This effectively reduces the diameter of the bubbles and improves the mixing efficiency between the gas and liquid. Preferably, the pore size of the ceramic membrane tube 3 is 200-500 nm. The ceramic membrane tube 3 is made of alumina or zirconium oxide, which offers advantages such as good stability, corrosion resistance, high temperature resistance, and resistance to oxidation in practical applications. Both the inlet and outlet of the ceramic membrane tube 3 are equipped with O-ring seals, ensuring airtightness while facilitating connection to other devices and pipelines.

[0040] In the membrane dispersion gas-liquid mixer of the present invention, preferably, the sintered membrane 4 is a stainless steel sintered membrane with a micrometer density of 5-100 μm and a porosity of 70-85%. This allows for further reduction of the average bubble diameter through shearing and breaking up of bubbles in practical applications. More preferably, the micrometer density of the stainless steel sintered membrane is 20-50 μm.

[0041] In some embodiments, the membrane dispersion gas-liquid mixer of the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4, and a housing 6; the housing 6 includes a liquid inlet 1, a gas inlet 2, and a gas-liquid mixing outlet 5; the ceramic membrane tube 3 is disposed inside the housing 6; the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the housing 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.

[0042] In other embodiments, the membrane dispersion gas-liquid mixer of the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4, and a housing 6; the housing 6 includes a liquid inlet 1, a gas inlet 2, and a gas-liquid mixing outlet 5; the ceramic membrane tube 3 is disposed inside the housing 6; the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the housing 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 plurality of outer channels 31 arranged around the inner channel 32.

[0043] In other embodiments, the membrane dispersion gas-liquid mixer of the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4, and a housing 6; the housing 6 includes a liquid inlet 1, a gas inlet 2, and a gas-liquid mixing outlet 5; the ceramic membrane tube 3 is disposed inside the housing 6; the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the housing 6; 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 plurality of outer channels 31 arranged around the inner channel 32; two partitions 33 are provided in the inner channel 32, and the two partitions 33 are arranged intersecting each other.

[0044] In other embodiments, the membrane dispersion gas-liquid mixer of the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4, and a housing 6; the housing 6 includes a liquid inlet 1, a gas inlet 2, and a gas-liquid mixing outlet 5; the ceramic membrane tube 3 is disposed inside the housing 6; the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the housing 6; 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 plurality of outer channels 31 arranged around the inner channel 32; two partitions 33 are provided in the inner channel 32, and the two partitions 33 are arranged intersecting 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 dispersion gas-liquid mixer of the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4, and a housing 6; the housing 6 includes a liquid inlet 1, a gas inlet 2, and a gas-liquid mixing outlet 5; the ceramic membrane tube 3 is disposed inside the housing 6; the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the housing 6; 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 plurality of outer channels 31 arranged around the inner channel 32; two partitions 33 are provided in the inner channel 32, and the two partitions 33 are arranged intersecting 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 dispersion gas-liquid mixer of the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4, and a housing 6; the housing 6 includes a liquid inlet 1, a gas inlet 2, and a gas-liquid mixing outlet 5; the ceramic membrane tube 3 is disposed inside the housing 6; the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the housing 6; 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 plurality of outer channels 31 arranged around the inner channel 32; two partitions 33 are provided in the inner channel 32, and the two partitions 33 are arranged intersecting 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 channels 31 is 0.1-0.3 times the diameter of the inner channel 32.

[0047] In other embodiments, the membrane dispersion gas-liquid mixer of the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4, and a housing 6; the housing 6 includes a liquid inlet 1, a gas inlet 2, and a gas-liquid mixing outlet 5; the ceramic membrane tube 3 is disposed inside the housing 6; the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the housing 6; 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; and an inner channel 3 is provided on the ceramic membrane tube 3. 2. A plurality of outer channels 31 are arranged around the inner channel 32; two partitions 33 are arranged inside the inner channel 32, and the two partitions 33 are arranged intersecting 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 channels 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 dispersion gas-liquid mixer of the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4, and a housing 6; the housing 6 includes a liquid inlet 1, a gas inlet 2, and a gas-liquid mixing outlet 5; the ceramic membrane tube 3 is disposed inside the housing 6; the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the housing 6; 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 surrounding the inner channel 3. 2. Several outer channels 31 are provided; two partitions 33 are provided 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 sintered membrane 4 is a stainless steel sintered membrane, and the stainless steel sintered membrane has a precision of 20-50μm and a porosity of 70-85%.

[0049] In other embodiments, the membrane dispersion gas-liquid mixer of the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4, and a housing 6; the housing 6 includes a liquid inlet 1, a gas inlet 2, and a gas-liquid mixing outlet 5; the ceramic membrane tube 3 is disposed inside the housing 6; the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the housing 6; 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; a [missing information - likely a device or component] is provided on the ceramic membrane tube 3. The inner channel 32 and a plurality of outer channels 31 arranged around the inner channel 32; two partitions 33 are arranged inside the inner channel 32, and the two partitions 33 are arranged intersecting 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 membrane 4 is a stainless steel sintered membrane, and the precision of the stainless steel sintered membrane is 5-100μm, and the porosity is 70-85%.

[0050] In other embodiments, the membrane dispersion gas-liquid mixer of the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4, and a housing 6; the housing 6 includes a liquid inlet 1, a gas inlet 2, and a gas-liquid mixing outlet 5; the ceramic membrane tube 3 is disposed inside the housing 6; the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the housing 6; 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; and an inner channel 3 is provided on the ceramic membrane tube 3. 2. A plurality of outer channels 31 are arranged around the inner channel 32; two partitions 33 are arranged inside the inner channel 32, and the two partitions 33 are arranged intersecting 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 channels 31 is 0.1-0.3 times the diameter of the inner channel 32; the pore size of the ceramic membrane tube 3 is 200-500 nm, and the porosity is 30-35%.

[0051] In other embodiments, the membrane dispersion gas-liquid mixer of the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4, and a housing 6; the housing 6 includes a liquid inlet 1, a gas inlet 2, and a gas-liquid mixing outlet 5; the ceramic membrane tube 3 is disposed inside the housing 6, the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the housing 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 plurality of outer channels 31 arranged around the inner channel 32; the inner channel 32 is provided with an inner channel 32, and the outer channel 31 is provided with an outer channel 32. Two partitions 33 are disposed within the channel 32, and the two partitions 33 are arranged intersecting 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 200-500 nm, and the porosity is 30-35%; 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%.

[0052] In other embodiments, the membrane dispersion gas-liquid mixer of the present invention includes a ceramic membrane tube 3, a sintered membrane sheet 4, and a housing 6; the housing 6 includes a liquid inlet 1, a gas inlet 2, and a gas-liquid mixing outlet 5; the ceramic membrane tube 3 is disposed inside the housing 6, the liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet 1 of the housing 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 plurality of outer channels 31 arranged around the inner channel 32; the inner channel 32 is provided with an inner channel 32, and the outer channel 31 is provided with an outer channel 32. Two partitions 33 are disposed within the channel 32, and the two partitions 33 are arranged intersecting 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 200-500 nm, and the porosity is 30-35%; the sintered membrane 4 is a stainless steel sintered membrane, and the precision of the stainless steel sintered membrane is 20-50 μm, and the porosity is 70-85%.

[0053] A second aspect of this invention provides the application of the membrane dispersion gas-liquid mixer described above in gas-liquid reactions. The gas-liquid reactions can include cyclohexane air oxidation, diesel hydrogenation, toluene fluorination, etc.

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

[0055] Adopting such Figure 1-2 The membrane dispersion gas-liquid mixer shown is specifically implemented in that it includes a ceramic membrane tube 3, a sintered membrane sheet 4, and a shell 6.

[0056] The housing 6 includes a liquid inlet 1, an air inlet 2, and a gas-liquid mixing outlet 5. The ceramic membrane tube 3 is disposed inside the housing 6. The liquid inlet of the ceramic membrane tube 3 is connected to the liquid inlet housing 6 1, and the liquid outlet of the ceramic membrane tube 3 is connected to the gas-liquid mixing 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 inside 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 channels 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 membrane 4 is a stainless steel sintered membrane, and the precision of the stainless steel sintered membrane is 5-100μm, and the porosity is 80%; the partitions 33 are made of polytetrafluoroethylene; the ceramic membrane tube 3 is made of alumina or zirconium oxide, and the diameter is 40mm.

[0058] Example 1

[0059] The outer channel diameter of the ceramic membrane tube is 2mm and the pore size is 200nm. The precision of the stainless steel sintered membrane is 20μm. In actual application, the water flow rate into the inner channel and the outer channel is set to 2L / min, and the gas flow rate into the shell is 1L / min. The membrane dispersion gas-liquid mixer is fixed to the bottom of the acrylic transparent square cylinder (50mm long and wide, 2m high, i.e., a conventional mixer).

[0060] Testing revealed that air, after being mixed in the membrane dispersion gas-liquid mixer, rapidly dispersed in the water, forming an emulsion within the acrylic transparent square cylinder. The emulsion flowed out from the top, underwent gas-liquid phase separation, and was then fed back as liquid. After the bubble flow stabilized, high-speed cameras were used to capture images at heights of 0.2m, 1m, and 2m, and the dimensions were characterized. At this point, the transmembrane pressure difference was 0.34MPa, and densely dispersed microbubble clusters were observed, with an average bubble diameter of approximately 468μm. No significant aggregation occurred within the 2m height.

[0061] Example 2

[0062] The outer channel diameter of the ceramic membrane tube is 4mm and the pore size is 200nm. The precision of the stainless steel sintered membrane is 20μm. In actual application, the water flow rate into the inner channel and the outer channel is set to 2L / min, and the gas flow rate into the shell is 1L / min. The membrane dispersion gas-liquid mixer is fixed to the bottom of the acrylic transparent square cylinder (50mm long and wide, 2m high, i.e., a conventional mixer).

[0063] Testing revealed that air, after being mixed in the membrane-dispersed gas-liquid mixer, rapidly dispersed in water, forming an emulsion within the acrylic transparent square cylinder. The emulsion flowed out from the top, underwent gas-liquid phase separation, and was then fed back as liquid. After the bubble flow stabilized, high-speed cameras were used to capture images at heights of 0.2m, 1m, and 2m, and the dimensions were characterized. At this point, the transmembrane pressure difference was 0.33MPa, and densely dispersed microbubble clusters were observed, with an average bubble diameter of approximately 320μm. No significant aggregation occurred within the 2m height.

[0064] Example 3

[0065] The outer channel diameter of the ceramic membrane tube is 6mm and the pore size is 200nm. The precision of the stainless steel sintered membrane is 20μm. In actual application, the water flow rate into the inner channel and the outer channel is set to 2L / min, and the gas flow rate into the shell is 1L / min. The membrane dispersion gas-liquid mixer is fixed to the bottom of the acrylic transparent square cylinder (50mm long and wide, 2m high, i.e., a conventional mixer).

[0066] Testing revealed that air, after being mixed in the membrane dispersion gas-liquid mixer, rapidly dispersed in the water, forming an emulsion within the acrylic transparent square cylinder. The emulsion flowed out from the top, underwent gas-liquid phase separation, and was then fed back as liquid. After the bubble flow stabilized, high-speed cameras were used to capture images at heights of 0.2m, 1m, and 2m, and the dimensions were characterized. At this point, the transmembrane pressure difference was 0.30MPa, and densely dispersed microbubble clusters were observed, with an average bubble diameter of approximately 292μm. No significant aggregation occurred within the 2m height.

[0067] Example 4

[0068] The outer channel diameter of the ceramic membrane tube is 8mm and the pore size is 200nm. The precision of the stainless steel sintered membrane is 20μm. In actual application, the water flow rate into the inner channel and the outer channel is set to 2L / min, and the gas flow rate into the shell is 1L / min. The membrane dispersion gas-liquid mixer is fixed to the bottom of the acrylic transparent square cylinder (50mm long and wide, 2m high, i.e., a conventional mixer).

[0069] Testing revealed that air, after being mixed in the membrane-dispersed gas-liquid mixer, rapidly dispersed in the water, forming an emulsion within the acrylic transparent square cylinder. The emulsion flowed out from the top, underwent gas-liquid phase separation, and was then fed back as liquid. After the bubble flow stabilized, high-speed cameras were used to capture images at heights of 0.2m, 1m, and 2m, and the dimensions were characterized. At this point, the transmembrane pressure difference was 0.28MPa, and densely dispersed microbubble clusters were observed, with an average bubble diameter of approximately 358μm. No significant aggregation occurred within the 2m height.

[0070] Example 5

[0071] The outer channel diameter of the ceramic membrane tube is 4mm and the pore size is 50nm. The precision of the stainless steel sintered membrane is 20μm. In actual application, the water flow rate into the inner channel and the outer channel is set to 2L / min, and the gas flow rate into the shell is 1L / min. The membrane dispersion gas-liquid mixer is fixed to the bottom of the acrylic transparent square cylinder (50mm long and wide, 2m high, i.e., a conventional mixer).

[0072] Testing revealed that air, after being mixed in the membrane dispersion gas-liquid mixer, rapidly dispersed in the water, forming an emulsion within the acrylic transparent square cylinder. The emulsion flowed out from the top, underwent gas-liquid phase separation, and was then fed back as a liquid feed. After the bubble flow stabilized, high-speed cameras were used to capture images at heights of 0.2m, 1m, and 2m, and the dimensions were characterized. At this height, the transmembrane pressure difference was 0.60 MPa, and densely dispersed microbubble clusters were observed, with an average bubble diameter of approximately 150 μm. No significant aggregation occurred within the 2m height. However, due to the high transmembrane pressure difference of 0.60 MPa, the microbubble yield was significantly reduced.

[0073] Example 6

[0074] The outer channel diameter of the ceramic membrane tube is 4mm and the pore size is 500nm. The precision of the stainless steel sintered membrane is 20μm. In actual application, the water flow rate into the inner channel and the outer channel is set to 2L / min, and the gas flow rate into the shell is 1L / min. The membrane dispersion gas-liquid mixer is fixed to the bottom of the acrylic transparent square cylinder (50mm long and wide, 2m high, i.e., a conventional mixer).

[0075] Testing revealed that air, after being mixed in the membrane dispersion gas-liquid mixer, rapidly dispersed in the water, forming an emulsion within the acrylic transparent square cylinder. The emulsion flowed out from the top, underwent gas-liquid phase separation, and was then fed back as liquid. After the bubble flow stabilized, high-speed cameras were used to capture images at heights of 0.2m, 1m, and 2m, and the dimensions were characterized. At this point, the transmembrane pressure difference was 0.30MPa, and densely dispersed microbubble clusters were observed, with an average bubble diameter of approximately 450μm. No significant aggregation occurred within the 2m height.

[0076] Example 7

[0077] The outer channel diameter of the ceramic membrane tube is 4mm and the pore size is 5μm. The precision of the stainless steel sintered membrane is 20μm. In actual application, the water flow rate into the inner channel and the outer channel is set to 2L / min, and the gas flow rate into the shell is 1L / min. The membrane dispersion gas-liquid mixer is fixed to the bottom of the acrylic transparent square cylinder (50mm long and wide, 2m high, i.e., a conventional mixer).

[0078] Testing revealed that air, after being mixed in the membrane dispersion gas-liquid mixer, rapidly dispersed in the water, forming an emulsion within the acrylic transparent square cylinder. The emulsion flowed out from the top, underwent gas-liquid phase separation, and was then fed back as liquid. After the bubble flow stabilized, high-speed cameras were used to capture images at heights of 0.2m, 1m, and 2m, and the dimensions were characterized. At this point, the transmembrane pressure difference was 0.25MPa, and densely dispersed microbubble clusters were observed, with an average bubble diameter of approximately 685μm. No significant aggregation occurred within the 2m height.

[0079] Example 8

[0080] The outer channel diameter of the ceramic membrane tube is 4mm and the pore size is 200nm. The precision of the stainless steel sintered membrane is 5μm. In actual application, the water flow rate into the inner channel and the outer channel is set to 2L / min, and the gas flow rate into the shell is 1L / min. The membrane dispersion gas-liquid mixer is fixed to the bottom of the acrylic transparent square cylinder (50mm long and wide, 2m high, i.e., a conventional mixer).

[0081] Testing revealed that air, after being mixed in the membrane dispersion gas-liquid mixer, rapidly dispersed in the water, forming an emulsion within the acrylic transparent square cylinder. The emulsion flowed out from the top, underwent gas-liquid phase separation, and was then fed back as a liquid feed. After the bubble flow stabilized, high-speed cameras were used to capture images at heights of 0.2m, 1m, and 2m, and the dimensions were characterized. At this height, the transmembrane pressure difference was 0.54MPa, and densely dispersed microbubble clusters were observed, with an average bubble diameter of approximately 258μm. No significant aggregation occurred within the 2m height. However, due to the high transmembrane pressure difference of 0.54MPa, the microbubble yield was significantly reduced.

[0082] Example 9

[0083] The outer channel diameter of the ceramic membrane tube is 4mm and the pore size is 200nm. The precision of the stainless steel sintered membrane is 50μm. In actual application, the water flow rate into the inner channel and the outer channel is set to 2L / min, and the gas flow rate into the shell is 1L / min. The membrane dispersion gas-liquid mixer is fixed to the bottom of the acrylic transparent square cylinder (50mm long and wide, 2m high, i.e., a conventional mixer).

[0084] Testing revealed that air, after being mixed with the membrane-dispersed gas-liquid mixer, rapidly dispersed in water, forming an emulsion within the acrylic transparent square cylinder. The emulsion flowed out from the top, underwent gas-liquid phase separation, and was then fed back as liquid. After the bubble flow stabilized, high-speed cameras were used to capture images at heights of 0.2m, 1m, and 2m, and the dimensions were characterized. At this point, the transmembrane pressure difference was 0.32MPa, and densely dispersed microbubble clusters were observed, with an average bubble diameter of approximately 445μm. No significant aggregation occurred within the 2m height.

[0085] Example 10

[0086] The outer channel diameter of the ceramic membrane tube is 4mm and the pore size is 200nm. The precision of the stainless steel sintered membrane is 80μm. In actual application, the water flow rate into the inner channel and the outer channel is set to 2L / min, and the gas flow rate into the shell is 1L / min. The membrane dispersion gas-liquid mixer is fixed to the bottom of the acrylic transparent square cylinder (50mm long and wide, 2m high, i.e., a conventional mixer).

[0087] Testing revealed that air, after being mixed in the membrane dispersion gas-liquid mixer, rapidly dispersed in the water, forming an emulsion within the acrylic transparent square cylinder. The emulsion flowed out from the top, underwent gas-liquid phase separation, and was then fed back as liquid. After the bubble flow stabilized, high-speed cameras were used to capture images at heights of 0.2m, 1m, and 2m, and the dimensions were characterized. At this point, the transmembrane pressure difference was 0.30MPa, and densely dispersed microbubble clusters were observed, with an average bubble diameter of approximately 612μm. No significant aggregation occurred within the 2m height.

[0088] Comparative Example 1

[0089] Fill a transparent acrylic square tube (50mm long and wide, 2m high) with water, and introduce air directly into the bottom at a flow rate of 1L / min.

[0090] After the bubble flow stabilized, high-speed cameras were used to capture images at heights of 0.2m, 1m, and 2m, and the dimensions were characterized. Millimeter-sized bubbles were observed, and the bubble rise process was not significant. The average bubble diameter was approximately 8mm.

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

[0092] Table 1

[0093]

[0094]

[0095] As shown in Table 1 above, preferably, when the diameter of the 12 external channels of the ceramic membrane tube is 4-6 mm, the pore size is 200-500 nm, and the precision of the stainless steel sintered membrane is 20-50 μm, the average diameter of the bubbles can be effectively reduced to the micrometer level while keeping the transmembrane pressure difference of the membrane dispersion gas-liquid mixer less than 0.35 MPa. Ultimately, compared with the scheme in Comparative Example 1, it effectively reduces the average diameter of the bubbles while also effectively increasing the yield of microbubbles.

[0096] The membrane dispersion gas-liquid mixer provided by this invention features a ceramic membrane tube disposed inside the housing. The inlet of the ceramic membrane tube is connected to the liquid inlet, and the outlet of the ceramic membrane tube is connected to the gas-liquid mixing outlet via a sintered membrane. Furthermore, when used in conjunction with a conventional gas-liquid reactor, it effectively reduces bubble diameter and improves mixing efficiency in practical applications. It boasts advantages such as small bubble diameter and good uniformity, high mixing efficiency, simple mixer structure, and low cost.

[0097] The preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention. To avoid unnecessary repetition, the present invention will not describe the various possible combinations separately. However, these simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A film dispersion gas-liquid mixer characterized by, The film dispersion type 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), a gas inlet (2) and a gas-liquid mixing outlet (5), the ceramic membrane tube (3) is arranged in the shell (6), the liquid inlet of the ceramic membrane tube (3) is connected with the liquid inlet (1) of the shell (6), and the liquid outlet of the ceramic membrane tube (3) is connected with the gas-liquid mixing outlet (5) through the sintered membrane sheet (4); The ceramic membrane tube (3) is provided with an inner channel (32) and a plurality of outer channels (31) surrounding the inner channel (32); the inner channel (32) is provided with two baffles (33), and the two baffles (33) are arranged in a cross manner; 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%; the sintered membrane sheet (4) is a stainless steel sintered membrane sheet, the precision of the stainless steel sintered membrane sheet is 5-100μm, and the porosity is 70-85%.

2. The film-distributed gas-liquid mixer of claim 1, wherein, The two baffles (33) are arranged in a perpendicular manner.

3. The film dispersed gas-liquid mixer of claim 1, wherein, The pore size of the ceramic membrane tube (3) is 200-500nm.

4. The film-distributed gas-liquid mixer of claim 1, wherein, The precision of the stainless steel sintered membrane sheet is 20-50μm.

5. The film distributed gas-liquid mixer of claim 1, wherein, The baffle (33) is made of polytetrafluoroethylene.

6. The film distributed gas-liquid mixer of claim 1, wherein, The ceramic membrane tube (3) is made of alumina or zirconia.

7. The film dispersed gas-liquid mixer according to claim 1 or 6, wherein The liquid inlet and the liquid outlet of the ceramic membrane tube (3) are both provided with O-shaped sealing rings.

8. The film dispersion type gas-liquid mixer in the gas-liquid reaction according to any one of claims 1-7.

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