Gas-liquid mixing device and gas-liquid mixing vaporization method

Abstract

The invention relates to the field of enhanced intrinsic safety in a gas-liquid phase mixing process, and discloses a gas-liquid mixing device and a gas-liquid mixing vaporization method. The device comprises a shell, a Venturi gas-phase turbulent mixing section, a liquid-phase atomizing mixing section and a static mixing section are sequentially arranged in the shell in the flowing direction of material flow, the Venturi gas-phase turbulent mixing section comprises a reducing structure and an expanding structure, a liquid inlet component is arranged at the position, close to the reducing structure, of the expanding structure, and the static mixing section is connected with the liquid inlet component. The liquid phase atomization mixing section is provided with a membrane tube base body, the membrane tube base body is provided with a plurality of inner holes in the axial direction, the surfaces of the inner holes are coated with nanometer materials, and the static mixing section is provided with filler. According to the device, the liquid-phase oxidizing agent and the gas-phase oxidizing agent are subjected to multi-stage mixing vaporization, the atomization degree of the liquid phase is increased, the uniformity degree of the obtained mixed gas phase is improved, meanwhile, the device can be quenched after burning explosion by coupling a porous membrane pipe and filler, and the burning explosion risk in the mixing vaporization process is reduced.

Description

Technical Field

[0001] This invention relates to the field of enhancing intrinsic safety in gas-liquid phase mixing processes, and specifically to a gas-liquid mixing device and a method for gas-liquid vaporization. Background Technology

[0002] Industrial oxidation processes are crucial for producing bulk chemical raw materials and intermediates. However, oxidation reactions typically involve mixing oxidants with combustible gases / vapors, posing a risk of combustion and explosion. Currently, most oxidation reactions require controlling the reactant ratios outside the explosive range or operating in environments with oxygen concentrations below the limiting oxygen level to avoid combustion and explosion. Some oxidation processes are limited by reaction thermodynamics and kinetics, and to ensure economic efficiency, the reactant ratios must be within the explosive limits, such as the maleic anhydride, phthalic anhydride, and terephthalaldehyde processes. In these processes, the combustible materials are all liquefied gases or liquids. Therefore, the mixing of raw materials with air can be carried out in two ways: ① Preheating the raw materials to above their boiling point to generate steam, and then mixing them with air in a mixer; ② Atomizing the liquid directly from a nozzle, allowing it to vaporize instantaneously at a lower vapor partial pressure, and then mixing with air. The second method, which effectively reduces preheating temperature and significantly lowers energy consumption in the mixing process, has been widely adopted in industrial production. However, in actual engineering processes, the atomization performance of liquid nozzles has defects. Liquid materials do not evaporate completely, and some droplets adhere to the pipe wall or are carried into the reactor, greatly increasing the probability of carbon buildup or explosion, which can easily affect the normal operation of the device or cause catalyst deactivation. Summary of the Invention

[0003] The purpose of this invention is to overcome the problems existing in the prior art where, during the oxidation reaction process, the organic liquid phase cannot be completely evaporated through nozzle atomization, and some droplets adhere to the pipe wall or are carried into the reactor, resulting in carbon buildup or combustion explosion, affecting the normal operation of the device or causing catalyst deactivation. This invention provides a gas-liquid mixing device and a gas-liquid mixing vaporization method. The device has a multi-stage gas-liquid mixing section to perform multi-stage mixing and vaporization of the liquid phase and the gaseous oxidant, increasing the atomization degree of the liquid phase and improving the uniformity of the resulting mixed gas phase. Simultaneously, the device employs a porous membrane tube coupled with packing material to perform post-combustion quenching, reducing the risk of combustion explosion during the mixing vaporization process.

[0004] To achieve the above objectives, a first aspect of the present invention provides a gas-liquid mixing device, which includes a housing. Along the flow direction of the material, a Venturi gas-phase turbulent mixing section, a liquid-phase atomizing mixing section, and a static mixing section are sequentially arranged within the housing.

[0005] The Venturi gas-phase turbulent mixing section includes a narrowing structure and an expanding structure. A liquid inlet component is provided near the narrowing structure in the expanding structure. The gas phase input through the narrowing structure and the liquid phase entering through the liquid inlet component are mixed in the expanding structure.

[0006] The liquid phase atomization mixing section is provided with a membrane tube substrate, which has a plurality of inner holes arranged along the axial direction. The surface of the inner holes is coated with nanomaterials. The membrane tube substrate is a porous material. A chamber for providing liquid phase is formed between the outer side of the membrane tube substrate and the shell. The flow from the Venturi gas phase turbulence mixing section is input from one end of the inner hole of the membrane tube substrate and mixes with the liquid phase entering through the side wall of the membrane tube substrate.

[0007] The static mixing section is equipped with packing material, and the material from the liquid phase atomization mixing section is further mixed under the obstruction of the packing material.

[0008] Preferably, a metal wire mesh is provided at the connection between the reduced diameter structure and the expanded diameter structure.

[0009] Preferably, a vaporization mixing development section is further disposed between the diameter expansion structure and the membrane tube substrate.

[0010] Preferably, the liquid inlet component has a sintered metal film.

[0011] Preferably, the material of the sintered metal film is selected from at least one of titanium, carbon steel, stainless steel and Hastelloy.

[0012] Preferably, the average pore size of the metal sintered film is 1-50 μm, more preferably 1-20 μm.

[0013] Preferably, the pore size of the membrane substrate is 1-100 μm, more preferably 3-10 μm.

[0014] Preferably, the material of the membrane substrate is selected from inorganic porous materials and / or organic polymers, and more preferably alumina.

[0015] Preferably, the number of inner holes is 9-60, more preferably 18-40.

[0016] Preferably, the diameter of the inner hole is 1-5 mm, more preferably 1-3 mm.

[0017] Preferably, the pore size of the nanomaterial is 20-800 nm, more preferably 150-600 nm.

[0018] Preferably, the nanomaterial is a nano-inorganic metal oxide, more preferably nano-alumina.

[0019] Preferably, the filler material is selected from at least one of alumina, titanium dioxide, cerium oxide, zirconium oxide, and molecular sieves.

[0020] Preferably, the size of the filler is 1-10 mm, more preferably 1-4 mm.

[0021] Preferably, the shape of the filler is selected from at least one of Pall rings, Raschig rings, corrugated mesh, hollow spheres, and hollow four-leaf clover.

[0022] Preferably, the housing is provided with a first liquid inlet and a second liquid inlet at the positions corresponding to the Venturi gas-phase turbulent mixing section and the liquid-phase atomizing mixing section. A first organic liquid phase is injected into the cavity formed between the outer side of the diameter-reducing structure and the diameter-expanding structure and the housing through the first liquid inlet, and a second organic liquid phase is injected into the cavity formed between the outer side of the membrane tube substrate and the housing through the second liquid inlet.

[0023] A second aspect of the present invention provides a method for gas-liquid mixing and vaporization, the method being carried out in the gas-liquid mixing apparatus described above, the method comprising:

[0024] (1) A gaseous oxidant is input from the inlet component of the Venturi gas-phase turbulent mixing section and mixed with the first organic liquid phase that enters through the liquid inlet component on the expansion structure to obtain a first gas-phase mixture;

[0025] (2) The first gas phase mixture is introduced from one end of the inner hole of the membrane tube substrate and mixed with the second organic liquid phase that enters through the side wall of the membrane tube substrate to obtain the second gas phase mixture;

[0026] (3) The second gas phase mixture is fed into the static mixing section for further mixing.

[0027] Preferably, the feed flow rate ratio of the first organic liquid phase to the second organic liquid phase is 1:1.5-8, more preferably 1:2-6.

[0028] Preferably, the feed flow rate of the first organic liquid phase is 1-80 mL / min, more preferably 20-60 mL / min.

[0029] Preferably, the feed flow rate of the second organic liquid phase is 1.5-640 mL / min, more preferably 40-360 mL / min.

[0030] Preferably, the feed flow rate of the gas-phase oxidant is 0.1-3 m³ / h. 3 / min, preferably 0.5-1.7m 3 / min.

[0031] Preferably, the gaseous oxidant is selected from at least one of air, pure oxygen, ozone, and a nitrogen-oxygen mixture.

[0032] Preferably, the organic liquid phase is selected from at least one of hydrocarbons, aldehydes, ethers, alcohols and acids with C6 or less.

[0033] The gas-liquid mixing device of this invention is configured with multiple gas-liquid mixing sections along the flow direction. The device first generates low pressure by forming a Venturi tube flow to entrain side gas, creating cavitation and rapidly vaporizing the liquid phase. Simultaneously, it enhances the conventional and turbulent diffusion of the resulting first gas-phase mixture and extends its mixing trajectory. The device then further vaporizes the liquid phase and mixes it with the first gas-phase mixture through the relatively high shear stress generated by the airflow and liquid jet within the membrane tube, increasing the atomization degree of the liquid phase. Finally, the device uses packing to form small vortices to further enhance the mixing of the resulting gas-phase mixture, improving its uniformity. The device also employs a porous membrane tube coupled with packing, enabling quenching after combustion / explosion, thereby reducing the risk of combustion / explosion during the mixing and vaporization process.

[0034] The gas-liquid mixing vaporization method of the present invention relies on the above-mentioned device. By performing multi-stage mixing and vaporization of the organic liquid phase and the gas phase oxidant, the organic liquid phase can be efficiently atomized. At the same time, the resulting mixed gas phase is uniformly mixed to avoid local droplets adhering to the pipe wall or being carried into the reactor, which would cause the local concentration of reactants in the reactor to be too high, thereby causing carbon buildup or combustion explosion. Attached Figure Description

[0035] Figure 1 This is a cross-sectional view of an exemplary gas-liquid mixing device;

[0036] Figure 2 This is an exemplary cross-sectional view of a gas-liquid mixing device with an ignition point and a flame observation window.

[0037] Explanation of reference numerals in the attached figures

[0038] 1. Shell; 11. First liquid inlet; 12. Second liquid inlet; 2. Venturi gas-phase turbulent mixing section; 21. Diameter reduction structure; 211. Metal wire mesh; 212. Throat; 22. Diameter expansion structure; 221. Liquid inlet component; 222. Vaporization mixing development section; 3. Liquid-phase atomization mixing section; 31. Membrane tube substrate; 4. Static mixing section; 41. Packing material; 5. First ignition point; 51. Second ignition point; 6. First flame observation window; 61. Second flame observation window; 62. Third flame observation window. Detailed Implementation

[0039] The following provides a detailed description of specific embodiments of the present invention. It should be understood that the specific embodiments described herein are for illustrative and explanatory purposes only and are not intended to limit the scope of the invention.

[0040] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0041] As used herein, the terms “connected”, “connected to”, etc., mean that two components are directly or indirectly connected to each other. Such a connection can be static (e.g., permanent) or movable (e.g., removable or releasable). Such a connection can be achieved by two components or two components and any other intermediate components being integrally formed into a single unit, or by two components or two components and any other intermediate components being interconnected.

[0042] Figure 1 A cross-sectional view of an exemplary gas-liquid mixing device is shown. The gas-liquid mixing device of the present invention includes a housing 1 and a multi-stage mixing device disposed within the housing 1. The multi-stage mixing device is configured to vaporize the liquid phase and provide substantially uniform gaseous reactants to the downstream reactor. Along the flow direction of the stream, the housing 1 is sequentially configured with a Venturi gas-phase turbulent mixing section 2, a liquid-phase atomizing mixing section 3, and a static mixing section 4. The gas-liquid mixing device of the present invention can be constructed to vaporize the liquid phase using a low-pressure region and shear stress generated by the gas flow, and to produce uniform reactant dispersion in the uniform gas flow into the downstream reactor. The device can efficiently vaporize the liquid phase, thereby reducing the formation and accumulation of deposits in the gas-liquid mixing device and the downstream reactor, reducing the risk of combustion and explosion, and preventing incompletely vaporized liquid phase from affecting the normal operation of the device or causing catalyst deactivation.

[0043] In this exemplary embodiment, the Venturi gas-phase turbulent mixing section 2 is a Venturi tube structure, specifically including a narrowing structure 21 and an expanding structure 22. The narrowing structure 21 can be configured to provide a low-pressure region for the airflow, and the expanding structure 22 can be configured to perform gas-liquid mixing and vaporization. The connection between the narrowing structure 21 and the expanding structure 22 is the throat 212 of the Venturi tube. In the device described in this invention, the Venturi gas-phase turbulent mixing section 2 utilizes the Venturi principle to provide a lower-pressure region for the airflow, achieving mixing and vaporization with the liquid phase.

[0044] In the device described in this invention, the reduced diameter structure 21 can be circular, conical, truncated conical, streamlined, or other similar shapes, preferably conical.

[0045] In this exemplary embodiment, the reduced-diameter structure 21 can be a conical pipe with a gradually decreasing cross-sectional diameter. The ratio of the maximum diameter to the minimum diameter of the conical pipe can be 10-40:1, preferably 2-20:1. The angle between the edge of the conical pipe and the axial direction of the gas-liquid mixing device can be 5-75°, preferably 10-30°. In some embodiments, when the reduced-diameter structure 21 is within the above range, especially within the above preferred range, the gas flow can obtain lower pressure, thereby achieving efficient vaporization of the subsequent liquid phase.

[0046] In a preferred embodiment, a metal mesh 211 is provided at the connection between the reduced diameter structure 21 and the expanded diameter structure 22. The metal mesh 211 may have a perforated structure, with the aperture of the perforated structure being 0.001-2 mm, more preferably 0.005-1 mm. In these preferred embodiments, the device utilizes the Venturi principle to provide a lower pressure region for the airflow, thereby achieving subsequent mixing and vaporization of the liquid phase.

[0047] In this exemplary embodiment, the diameter-expanding structure 22 can be a conical pipe with a gradually increasing cross-sectional diameter. The angle between the edge of the conical pipe and the axial direction of the gas-liquid device can be 5-75°, preferably 10-30°. When the angle between the edge of the conical pipe and the axial direction of the gas-liquid device is within the above range, especially within the above preferred range, the liquid phase vaporization is more complete, and the resulting first gas phase mixture is more uniformly dispersed.

[0048] In this exemplary embodiment, a liquid inlet member 221 is provided on the expanding structure 22 near the contracting structure 21. The airflow from the contracting structure 21 expands rapidly in the expanding structure 22 after passing through the throat 212, and the fluid entrains the side gas to form cavitation. The liquid phase entering through the liquid inlet member 221 enters from the cavitation position. Because the overall cavitation pressure is low and the partial pressure of the liquid phase is lower than its saturated vapor pressure, the liquid phase can vaporize rapidly.

[0049] In a preferred embodiment, the ratio of the distance between the liquid inlet member 221 and the throat 212 to the diameter of the throat 212 can be 0.1-6:1, more preferably 0.2-2:1. In these preferred embodiments, when the ratio of the distance between the liquid inlet member 221 and the throat 212 to the diameter of the throat 212 is within the above-mentioned preferred range, efficient vaporization of the liquid phase and uniform dispersion of the gaseous reactants can be achieved.

[0050] In a preferred embodiment, the liquid inlet member 221 may be composed of a sintered metal film. The material of the sintered metal film is selected from at least one of titanium, carbon steel, stainless steel, and Hastelloy, more preferably stainless steel or Hastelloy. The average pore size of the sintered metal film is 1-50 μm, more preferably 1-20 μm. The ratio of the length of the sintered metal film to the diameter of the throat 212 is 1-40:1, more preferably 1-10:1. In these preferred embodiments, the liquid inlet member is corrosion-resistant and configured to form a large number of small droplets from the liquid phase, effectively reducing the surface energy of the liquid phase to achieve efficient vaporization.

[0051] In this exemplary embodiment, a vaporization mixing development section 222 is further disposed between the diameter expansion structure 22 and the membrane tube substrate 31. The vaporization mixing development section 222 is connected to the throat 212 via a pipe with a gradually increasing diameter, and the vaporization mixing development section 222 is connected to the air inlet end of the liquid-phase atomization mixing section 3. The vaporization mixing development section 222 can be configured to extend the mixing trajectory of the resulting gas-phase mixture to achieve sufficient vaporization of the liquid phase and sufficient dispersion of the resulting first gas-phase mixture.

[0052] In a preferred embodiment, the length ratio of the vaporization mixing development section 222 to the diameter of the shell 1 is 1-10:1, more preferably 1-3:1. In these preferred embodiments, the liquid phase vaporization is more complete, and the resulting gas phase mixture is more uniformly dispersed.

[0053] In this exemplary embodiment, the liquid-phase atomizing mixing section 3 is provided with a membrane tube substrate 31, which has a plurality of inner holes arranged axially, and the surface of the inner holes is coated with nanomaterials. The membrane tube substrate 31 is a porous material, and a chamber for providing liquid phase is formed between the outer side of the membrane tube substrate 31 and the shell 1. The flow from the Venturi gas-phase turbulent mixing section 2 is input from one end of the inner hole of the membrane tube substrate 31, and generates relatively high shear stress with the liquid phase seepage entering through the sidewall of the membrane tube substrate 31, thereby vaporizing the liquid phase.

[0054] In a preferred embodiment, the pore size of the membrane substrate 31 is 1-100 μm, more preferably 3-10 μm. The material of the membrane substrate 31 is selected from inorganic porous materials and / or organic polymers, more preferably alumina. The outer diameter of the membrane substrate 31 is 10-50 mm, more preferably 20-30 mm. The ratio of the length of the membrane substrate 31 to the diameter of the shell 1 is 1-5:1, more preferably 1-3:1. In these preferred embodiments, the membrane substrate 31 is configured to provide stronger shear stress for the liquid phase permeation and gas flow, thereby achieving efficient vaporization of the organic liquid phase and improving the dispersion uniformity of the resulting gas phase mixture.

[0055] In a preferred embodiment, the number of inner holes is 9-60, more preferably 18-40. The diameter of the inner holes is 1-5 mm, more preferably 1-3 mm.

[0056] In a preferred embodiment, the pore size of the nanomaterial is 20-800 nm, more preferably 150-600 nm. The nanomaterial is a nano-inorganic metal oxide, more preferably nano-alumina. In these preferred embodiments, when the properties of the nanomaterial are within the above-mentioned preferred range, corrosion of the liquid phase can be avoided, while effectively reducing the risk of combustion and explosion during the mixing and vaporization process.

[0057] In this exemplary embodiment, the static mixing section 4 is provided with a packing 41, and the material from the liquid phase atomizing mixing section 3 is further mixed under the blocking effect of the packing 41.

[0058] In a preferred embodiment, the material of the packing 41 is selected from at least one of alumina, titanium dioxide, cerium oxide, zirconium oxide, and molecular sieves, more preferably alumina. The size of the packing 41 is 1-10 mm, more preferably 1-4 mm. The shape of the packing 41 is selected from at least one of Pall rings, Raschig rings, corrugated mesh, hollow spheres, and hollow four-leaf clover, more preferably at least one of Pall rings, hollow spheres, and hollow four-leaf clover. In these preferred embodiments, the packing blocks the flow from the liquid-phase atomization mixing section 3 from forming small vortices to enhance mixing, while the presence of the packing effectively suppresses the combustion and explosion of explosive gases within the explosion limits.

[0059] In a preferred embodiment, the length ratio of the static mixing section 4 to the length of the shell 1 is 0.05-0.3:1, more preferably 0.1-0.2:1. In these preferred embodiments, the material from the liquid-phase atomizing mixing section 3 can be further mixed uniformly inside the static mixing section 4, preventing combustion and explosion when it enters the next stage reactor.

[0060] In this exemplary embodiment, the housing 1 is provided with a first liquid inlet 11 and a second liquid inlet 12 corresponding to the positions of the Venturi gas-phase turbulent mixing section 2 and the liquid-phase atomizing mixing section 3. A portion of the liquid phase is injected through the first liquid inlet 11 into the cavity formed between the outer side of the constriction structure 21 and the expansion structure 22 and the housing 1, and then enters the expansion structure 22 through the liquid inlet member 221 to mix and vaporize with the gas phase from the constriction structure 21. Another portion of the liquid phase is injected through the second liquid inlet 12 into the cavity formed between the outer side of the membrane tube substrate 31 and the housing 1, and then enters the inner hole of the membrane tube through the membrane tube substrate 31, where it mixes and vaporizes with the material flowed into the expansion structure 22.

[0061] The gas-liquid mixing device disclosed in this invention may include one or more components or embodiments described in this invention. For example, multiple embodiments of the gas-liquid mixing device described in this invention may be connected in parallel with a main feed pipe.

[0062] The present invention also provides a method for gas-liquid mixing and vaporization, the method being carried out in a gas-liquid mixing device. Figure 1 This is a cross-sectional view of an exemplary gas-liquid mixing apparatus, the method comprising:

[0063] (1) A gaseous oxidant is input from the inlet end of the Venturi gas-phase turbulent mixing section 2 and mixed with the first organic liquid phase that enters through the liquid inlet component 221 on the expansion structure 22 to obtain a first gas-phase mixture;

[0064] (2) The first gas phase mixture is introduced from one end of the inner hole of the membrane tube substrate 31 and mixed with the second organic liquid phase that enters through the side wall of the membrane tube substrate 31 to obtain the second gas phase mixture;

[0065] (3) The second gas phase mixture is fed into the static mixing section 4 for further mixing.

[0066] In some embodiments, the feed flow rate ratio of the first organic liquid phase to the second organic liquid phase is 1:1.5-8, preferably 1:2-6, and more preferably 1:3-5. In these embodiments, when the feed flow rate ratio of the first organic liquid phase to the second organic liquid phase is within the above range, the organic liquid phase vaporizes more completely, and the second gas phase mixture is dispersed more uniformly.

[0067] In other embodiments, the feed flow rate of the first organic liquid phase is 1-80 mL / min, preferably 20-60 mL / min, and more preferably 30-50 mL / min. The feed flow rate of the second organic liquid phase is 1.5-640 mL / min, preferably 40-360 mL / min, and more preferably 90-250 mL / min. In these embodiments, when the feed flow rates of the first and second organic liquid phases are within the above ranges, the organic liquid phase vaporizes more completely, the second gas phase mixture is more uniformly dispersed, and the organic phase in the first and second gas phase mixtures is within the explosion limits, thus preventing combustion and explosion.

[0068] In other embodiments, the feed flow rate of the gaseous oxidant is 0.1-3 m³ / h. 3 / min, preferably 0.5-1.7m 3 / min, more preferably 1-1.5m 3 / min. In these embodiments, when the feed flow rate of the gaseous oxidant is within the above range, the Venturi flow formed by the gaseous oxidant has a lower low-pressure region, the second gaseous mixture is more uniformly dispersed, and the organic phase in the first gaseous mixture and the second gaseous mixture is within the explosion limit range, thus avoiding combustion and explosion.

[0069] In this invention, the gaseous oxidant is selected from at least one of air, pure oxygen, ozone and nitrogen-oxygen mixture, preferably air or nitrogen-oxygen mixture with an oxygen concentration >21%.

[0070] In this invention, the organic liquid phase is selected from at least one of hydrocarbons, aldehydes, ethers, alcohols and acids with C6 or less, preferably C4 hydrocarbons.

[0071] The following examples further illustrate the gas-liquid mixing device and gas-liquid vaporization method of the present invention. These examples are implemented based on the technical solution of the present invention, providing detailed implementation methods and specific operating procedures; however, the scope of protection of the present invention is not limited to the following examples.

[0072] The following examples 1-3 are in Figure 1 The illustrated gas-liquid mixing device has a total pipeline diameter of 30 mm and uses a single gas-liquid mixing unit. The gas-liquid mixing unit includes a housing 1. Along the flow direction of the material, the housing 1 is sequentially configured with a Venturi gas-phase turbulent mixing section 2, a liquid-phase atomizing mixing section 3, and a static mixing section 4.

[0073] The Venturi gas-phase turbulent mixing section 2 includes a narrowing structure 21 and an expanding structure 22. The connection between the narrowing structure 21 and the expanding structure 22 is a throat 212. A metal mesh 211 is provided at the throat 212. The diameter of the throat 212 is 5 mm, and the aperture of the metal mesh is 0.02 mm. The expanding structure 22 also includes a liquid inlet component 221. The distance between the liquid inlet component 221 and the throat 212 is 5 mm. A vaporization mixing development section 222 is also arranged between the expanding structure 22 and the membrane tube substrate 31. The length of the vaporization mixing development section 222 is 60 mm. The liquid inlet component 221 has a sintered metal film. The sintered metal film is made of titanium, with a aperture of 5 μm and a length of 20 mm. The angle between the edge of the narrowing structure 21 and the horizontal direction is 45°, and the angle between the edge of the expanding structure 22 and the horizontal direction is 30°.

[0074] The length of the liquid phase atomization mixing section 3 is 60 mm. The liquid phase atomization mixing section 3 is provided with a membrane tube substrate 31. The membrane tube substrate 31 is made of alumina and has a length of 5 μm. The membrane tube substrate 31 has an inner hole with a pore diameter of 2 mm and a number of 37. The surface of the inner hole is coated with nano-alumina with an average pore diameter of 200 nm.

[0075] The static mixing section 4 is 30mm long and is equipped with packing 41, which is a Pall ring metal packing with a size of 3mm.

[0076] The housing 1 is provided with a first liquid inlet 11 and a second liquid inlet 12 at the positions corresponding to the Venturi gas-phase turbulent mixing section 2 and the liquid-phase atomizing mixing section 3.

[0077] Example 1

[0078] Air is used as the gaseous oxidant, and n-butane is used as the organic liquid phase. The air feed rate is 1.3 m³ / h. 3The total feed flow rate of n-butane liquid phase is 200 mL / min. The feed flow rate ratio of the first organic liquid phase to the second organic liquid phase is 1:4. The n-butane is preheated to 60°C and then introduced into the chamber between the shell 1 and the Venturi gas-phase turbulent mixing section 2, and the chamber between the shell 1 and the liquid-phase atomizing mixing section 3, respectively, through the first inlet 11 and the second inlet 12. Air enters the constriction structure 21 through the air inlet end of the Venturi gas-phase turbulent mixing section 2, and mixes with the first organic liquid phase entering through the liquid inlet component 221 in the expansion structure 22 after passing through the throat 212. The first organic liquid phase vaporizes to obtain a first gas-phase mixture. The first gas-phase mixture flows into the liquid-phase atomizing mixing section 3 and mixes with the second organic liquid phase entering through the membrane tube substrate 31. The second organic liquid phase vaporizes to obtain a second gas-phase mixture. The second gas-phase mixture enters the static mixing section 4 for static mixing and then enters the next stage reactor.

[0079] Example 2

[0080] This embodiment is implemented according to the method of Embodiment 1, except that the air feed flow rate is 0.1 m³ / s. 3 The total feed flow rate of the n-butane liquid phase is 20 mL / min.

[0081] Example 3

[0082] This embodiment is implemented according to the method of Embodiment 1, except that the total feed flow rate of the n-butane liquid phase is 2 mL / min, and the feed flow rate ratio of the first organic liquid phase to the second organic liquid phase is 1:1.

[0083] Example 4

[0084] This embodiment is implemented according to the method of Embodiment 1, except that the length of the metal sintered film in the gas-liquid mixing device is 5 mm.

[0085] Example 5

[0086] This embodiment is implemented according to the method of Embodiment 1, except that in the gas-liquid mixing device, the angle between the expansion structure 22 and the horizontal direction is 75°.

[0087] Example 6

[0088] This embodiment is implemented according to the method of Embodiment 1, except that in the gas-liquid mixing device, the distance between the liquid inlet component 221 and the throat 212 is 30mm.

[0089] Example 7

[0090] This embodiment is implemented according to the method of Embodiment 1, except that the length of the vaporization mixing development section 222 in the gas-liquid mixing device is 30 mm.

[0091] Example 8

[0092] The comparative example was carried out according to the method of Example 1, except that the length of the Venturi gas-phase turbulent mixing section 2 was changed to 30 mm in the gas-liquid mixing device.

[0093] Example 9

[0094] The comparative example was carried out according to the method of Example 1, except that the average pore size of the metal sintered film was 50 μm in the gas-liquid mixing device.

[0095] Example 10

[0096] The comparative example was carried out according to the method of Example 1, except that in the gas-liquid mixing device, the packing 41 of the static mixing section 4 used 6mm Pall rings.

[0097] Comparative Example 1

[0098] The comparative example is implemented according to the method of Example 1, except that the Venturi gas-phase turbulent mixing section 2 in the gas-liquid mixing device does not have a narrowing structure 21 and a widening structure 22.

[0099] Comparative Example 2

[0100] The comparative example was carried out according to the method of Example 1, except that in the gas-liquid mixing device, the liquid phase atomization mixing section 3 was not provided with a membrane tube substrate 31, and a regular nozzle was used for feeding.

[0101] Comparative Example 3

[0102] The comparative example was carried out according to the method of Example 1, except that in the gas-liquid mixing device, the inner surface of the membrane tube substrate 31 was not coated with nanomaterials.

[0103] Comparative Example 4

[0104] The comparative example was carried out according to the method of Example 1, except that in the gas-liquid mixing device, the static mixing section 4 was not equipped with packing 41.

[0105] Test case

[0106] like Figure 2As shown, along the flow direction of the gas-liquid mixture, a first ignition point 5 is set on the inner wall 20mm from the end of the housing 1, and a second ignition point 51 is set on the inner wall of the housing 1 corresponding to the vaporization mixing development section 222. A first flame observation window 6, a second flame observation window 61, and a third flame observation window 62 are respectively set at the reduced diameter structure 21, the first ignition point 5, and the second ignition point 51 to detect whether a flame appears in order to determine the mixing effect and explosion suppression and flame arresting effect of the gas-liquid mixing device. When igniting at the first ignition point 5, the presence of a flame in the first flame observation window 6 indicates that the final gas-phase mixture is relatively uniformly mixed; the absence of a flame in the first flame observation window 6 indicates that the final gas-phase mixture is not uniformly mixed. The absence of a flame in the second flame observation window 61 indicates that the static mixing section 4 can effectively block flame propagation and prevent the flame from spreading upstream; the presence of a flame in the second flame observation window 61 indicates that the static mixing section 4 cannot block flame. When igniting at the second ignition point 51, the absence of a flame in the second flame observation window 61 indicates that the first gas-phase mixture is uniformly mixed; the presence of a flame in the second flame observation window 61 indicates that the first gas-phase mixture is not uniformly mixed; the presence of a flame in the third flame observation window 62 indicates that the throat 212 does not block flame; the absence of a flame in the third flame observation window 62 indicates that the throat 212 blocks flame.

[0107] The results are shown in Table 1.

[0108] Table 1

[0109]

[0110]

[0111] As can be seen from Examples 1-9 and Comparative Examples 1-4, in Examples 1-9, ignition at the first ignition point 5 resulted in a flame observed at the first flame observation window 6, indicating that the final gas-phase mixture was relatively uniformly mixed. No flame was observed at the second flame observation window 61 and the third flame observation window 62, indicating that the static mixing section 4 effectively extinguishes flames. In the preferred embodiment 1, ignition at the second ignition point 51 resulted in no flame observed at the first flame observation window 6, the second flame observation window 61, and the third flame observation window 62, indicating that the first gas-phase mixture was uniformly mixed. In the non-preferred embodiments 2-7, ignition at the second ignition point 51 resulted in a flame observed at the second flame observation window 61, indicating that the first gas-phase mixture was not uniformly mixed. No flame was observed at the first flame observation window 6 and the third flame observation window 62, indicating that the throat 212 and the liquid-phase atomizing mixing section 3 had good flame-retardant properties. In non-preferred embodiments 8 and 9, ignition at the second ignition point 51 and the presence of a flame at the second flame observation window 61 indicate that the first gas phase mixture is not uniformly mixed. The presence of a flame at the third flame observation window 62 indicates that the throat 212 has poor flame retardant performance. In non-preferred embodiment 10, ignition at the first ignition point 5 and the presence of a flame at both the first and second flame observation windows 6 and 61 indicate that the static mixing section can achieve uniform mixing of the gas phase mixture, but the flame retardant performance is poor. In Comparative Examples 1-4, ignition at the first ignition point 5 and the absence of a flame at the first flame observation window 6 indicate that the final gas phase mixture is not uniformly mixed. In Comparative Example 1, ignition at the second ignition point 51 and the presence of a flame at the second flame observation window 61 indicate that the first gas phase mixing section is not uniformly mixed; the presence of a flame at the third flame observation window 62 indicates that the first gas phase mixing section has poor flame retardant performance. In Comparative Example 2, ignition was performed at the second ignition point 5, and a flame was observed at the second flame observation window 61, indicating that the liquid phase atomization mixing section 3 was not mixed evenly, and some droplets were sprayed onto the pipe wall and flowed to the second ignition point 5, resulting in a local increase in concentration; a flame was observed at the first flame observation window 6, indicating that the flame retardant performance of the filler alone was poor.

[0112] The preferred embodiments of the present invention have been described in detail above; 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, including combining the various technical features in any other suitable manner. 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 gas-liquid mixing device, characterized in that, The gas-liquid mixing device includes a housing (1). Along the flow direction of the material, the housing (1) is sequentially configured with a Venturi gas-phase turbulent mixing section (2), a liquid-phase atomizing mixing section (3), and a static mixing section (4), wherein... The Venturi gas-phase turbulent mixing section (2) includes a narrowing structure (21) and an expanding structure (22). The expanding structure (22) is provided with a liquid inlet component (221) near the narrowing structure (21). The gas phase input through the narrowing structure (21) and the liquid phase entering through the liquid inlet component (221) are mixed in the expanding structure (22). The liquid phase atomization mixing section (3) is provided with a membrane tube substrate (31), which has a plurality of inner holes arranged along the axial direction. The surface of the inner holes is coated with nanomaterials. The membrane tube substrate (31) is a porous material. A chamber for providing liquid phase is formed between the outer side of the membrane tube substrate (31) and the shell (1). The flow from the Venturi gas phase turbulence mixing section (2) is input from one end of the inner hole of the membrane tube substrate (31) and mixed with the liquid phase entering through the side wall of the membrane tube substrate (31). The static mixing section (4) is provided with a packing material (41), and the material from the liquid phase atomizing mixing section (3) is further mixed under the blocking effect of the packing material (41).

2. The gas-liquid mixing device according to claim 1, characterized in that, A metal wire mesh (211) is provided at the connection between the reduced diameter structure (21) and the expanded diameter structure (22).

3. The gas-liquid mixing device according to claim 1, characterized in that, A vaporization mixing development section (222) is also disposed between the diameter expansion structure (22) and the membrane tube substrate (31).

4. The gas-liquid mixing device according to claim 1, characterized in that, The liquid inlet component (221) has a sintered metal film; Preferably, the material of the sintered metal film is selected from at least one of titanium, carbon steel, stainless steel and Hastelloy; Preferably, the average pore size of the metal sintered film is 1-50 μm, more preferably 1-20 μm.

5. The gas-liquid mixing device according to claim 1, characterized in that, The pore size of the membrane substrate (31) is 1-100 μm, preferably 3-10 μm; Preferably, the material of the membrane substrate (31) is selected from inorganic porous materials and / or organic polymers, and more preferably alumina.

6. The gas-liquid mixing device according to claim 1 or 5, characterized in that, The number of inner holes is 9-60, preferably 18-40; Preferably, the diameter of the inner hole is 1-5 mm, more preferably 1-3 mm.

7. The gas-liquid mixing apparatus according to any one of claims 1 or 5, characterized in that, The pore size of the nanomaterial is 20-800 nm, preferably 150-600 nm; Preferably, the nanomaterial is a nano-inorganic metal oxide, more preferably nano-alumina.

8. The gas-liquid mixing device according to claim 1, characterized in that, The material of the filler (41) is selected from at least one of alumina, titanium dioxide, cerium oxide, zirconium oxide and molecular sieve; Preferably, the size of the filler (41) is 1-10 mm, more preferably 1-4 mm; Preferably, the shape of the filler (41) is selected from at least one of Pall rings, Raschig rings, corrugated mesh, hollow spheres, and hollow four-leaf clover.

9. The gas-liquid mixing device according to any one of claims 1, characterized in that, The housing (1) is provided with a first liquid inlet (11) and a second liquid inlet (12) at the positions corresponding to the Venturi gas-phase turbulent mixing section (2) and the liquid-phase atomizing mixing section (3). A first organic liquid phase is injected into the cavity formed between the outer side of the reduced diameter structure (21) and the expanded diameter structure (22) and the housing (1) through the first liquid inlet (11), and a second organic liquid phase is injected into the cavity formed between the outer side of the membrane tube substrate (31) and the housing (1) through the second liquid inlet (12).

10. A method for vaporizing a gas-liquid mixture, characterized in that, The method is implemented in the gas-liquid mixing apparatus according to any one of claims 1-9, and the method includes: (1) A gaseous oxidant is input from the inlet end of the Venturi gas-phase turbulent mixing section (2) and mixed with the first organic liquid phase that enters through the liquid inlet component (221) on the expansion structure (22) to obtain a first gas-phase mixture; (2) The first gas phase mixture is introduced from one end of the inner hole of the membrane tube substrate (31) and mixed with the second organic liquid phase that enters through the side wall of the membrane tube substrate (31) to obtain the second gas phase mixture; (3) The second gas phase mixture is fed into the static mixing section (4) for further mixing.

11. The method according to claim 10, characterized in that, The feed flow rate ratio of the first organic liquid phase to the second organic liquid phase is 1:1.5-8, preferably 1:2-6; Preferably, the feed flow rate of the first organic liquid phase is 1-80 mL / min, more preferably 20-60 mL / min; Preferably, the feed flow rate of the second organic liquid phase is 1.5-640 mL / min, more preferably 40-360 mL / min.

12. The method according to claim 10, characterized in that, The feed flow rate of the gaseous oxidant is 0.1-3 m³ / h. 3 / min, preferably 0.5-1.7m 3 / min.

13. The method according to any one of claims 10-12, characterized in that, The gaseous oxidant is selected from at least one of air, pure oxygen, ozone, and a nitrogen-oxygen mixture.

14. The method according to any one of claims 10-12, characterized in that, The organic liquid phase is selected from at least one of hydrocarbons, aldehydes, ethers, alcohols, and acids with C6 or fewer atoms.

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