CN214716658U - Gas-liquid reaction device - Google Patents
Gas-liquid reaction device Download PDFInfo
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- CN214716658U CN214716658U CN202120369462.6U CN202120369462U CN214716658U CN 214716658 U CN214716658 U CN 214716658U CN 202120369462 U CN202120369462 U CN 202120369462U CN 214716658 U CN214716658 U CN 214716658U
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Abstract
The utility model provides a gas-liquid reaction unit, gas-liquid reaction unit include the casing, be provided with gas dispersion module and two at least reaction pipe fittings in the casing, reaction pipe fitting parallel connection or follow the reaction liquid flow direction and establish ties in proper order and connect. The utility model discloses a reaction unit simple structure, the double-phase area of contact of gas-liquid is big, and no mechanical stirring part is difficult for leaking, possesses reaction temperature accurate control, good mass transfer and heat transfer performance, reaction pressure adjustable range big, reaction time is adjustable, the reaction process material stock is few, the security is strong, can realize performances such as serialization production, extensive adaptability.
Description
Technical Field
The utility model belongs to the technical field of the gas-liquid reaction, especially, relate to a gas-liquid reaction unit.
Background
A heterogeneous reaction process in which a gas phase and a liquid phase are present in a reaction system, typically a gas phase reactant is dissolved in a liquid phase and then reacted with another reactant in the liquid phase; it is also possible that the reactants are present in the gas phase and that they are dissolved in a solution containing the catalyst before the reaction is carried out. The gas-liquid phase reaction is mainly used for directly preparing products, such as ethylene in PdCl2-Cu2Cl2Oxidizing in acetic acid solution to obtain acetaldehyde, and introducing airOxidizing cumene to produce cumene hydroperoxide and the like; and secondly, chemical absorption is used for removing one or more components in the gas phase, for example, acid gases such as carbon dioxide, hydrogen sulfide and the like in the half water gas are removed by alkali liquor, and carbon monoxide and the like in the synthesis gas are removed by copper ammonia liquor.
In order to improve the reaction efficiency of the reaction equipment, three modes of gas external circulation, liquid external circulation and gas internal circulation are generally adopted in industry, and the reaction technologies are fully applied to magnetic reaction kettles, hydrogenation reaction kettles and magnetic drive reaction kettles. The gas-liquid internal circulation reaction kettle is equivalent to self-suction type reaction equipment, is one of core technologies of a gas/liquid reaction device, and is a reaction device which can automatically suck gas in the upper space of the reaction kettle to carry out gas-liquid contact without an additional gas conveying machine. Through the hollow turbine stirrer specially designed for the reaction kettle, the triangular iron core winding machine continuously sucks reaction gas on the liquid level while material liquid is mixed, so that the purposes of gas-liquid circulation and dispersion are achieved, and meanwhile, the gas and the solid catalyst can be uniformly dispersed in the reaction kettle by the combined high-efficiency axial flow paddle, so that the purpose of rapid reaction is achieved. The external circulation reaction kettle is opposite in that reaction liquid is pumped out from the bottom of the reaction kettle under the action of a centrifugal pump, reaction gas in a gas phase space of the reactor is pumped through a Venturi tube, and the reaction gas is fully mixed and dispersed in the Venturi tube, so that very fine bubbles can be obtained, and the gas-liquid contact area and the reaction rate are greatly improved. The operation mode of the gas external circulation reaction kettle is that reaction gas is firstly led out from a gas phase space, and the gas is pressurized by a compressor and then is led in from the bottom of the reaction kettle; then, under the coordination of a magnetic stirrer, a larger gas holding amount and a larger contact area can be obtained, so that the reaction rate of the reaction kettle is improved, and meanwhile, any gas circulation amount can be obtained.
However, the gas-liquid contact interface of the reaction kettle is small, the heat exchange area is small, the phenomenon of high local temperature exists, and the heat transfer problem limits the reaction efficiency.
Disclosure of Invention
Not enough to prior art exists, the utility model aims to provide a gas-liquid reaction device, the utility model discloses a reaction unit simple structure, the double-phase area of contact of gas-liquid is big, does not have mechanical stirring part, is difficult for leaking, possesses that reaction temperature accurate control, good mass transfer and heat transfer performance, reaction pressure adjustable range are big, reaction time is adjustable, reaction process material stock is few, the security is strong, can realize performances such as serialization production, extensive adaptability.
To achieve the purpose, the utility model adopts the following technical proposal:
the utility model provides a gas-liquid reaction device, gas-liquid reaction device include the casing, be provided with in the casing along the gas dispersion module and the reaction module that the reaction liquid flow direction connects gradually.
The reaction module comprises at least two reaction pipe fittings which are connected in parallel or connected in series in sequence along the flow direction of reaction liquid.
When the reaction pipe fittings adopt the series connection mode, along the reaction liquid flow direction, the gas dispersion module insert the entry end of first reaction pipe fittings, gas raw materials and liquid phase raw materials flow through each reaction pipe fitting in proper order after the gas-liquid deconcentrator dispersion is even.
The gas-liquid reaction device provided by the utility model is divided into a gas-liquid two-phase fluid mixing area and a main reaction area, the gas dispersion module is positioned in the gas-liquid two-phase fluid mixing area, the rapid and efficient mixing reaction of two immiscible fluids in large-scale production can be realized, meanwhile, the heat can be rapidly transferred, the side reaction is inhibited, the selectivity of the product is improved, the treatment capacity is large, and the energy consumption is small; the reaction pipe fittings are positioned in the main reaction zone, and when the gas-liquid multiphase material reaction time needs to be prolonged, the length of the reaction pipe fittings can be lengthened or the number of the reaction pipe fittings can be increased according to the needs. The utility model discloses a reaction unit simple structure, the double-phase area of contact of gas-liquid is big, and no mechanical stirring part is difficult for leaking, possesses reaction temperature accurate control, good mass transfer and heat transfer performance, reaction pressure adjustable range big, reaction time is adjustable, the reaction process material stock is few, the security is strong, can realize performances such as serialization production, extensive adaptability. The method can realize the rapid and efficient mixing reaction of gas and liquid in large-scale production, and simultaneously inhibit side reaction by accurately controlling reaction conditions, thereby improving the selectivity of products. Can be widely used in the field of petrochemical industry, and is particularly suitable for gas-liquid multiphase reactions, such as tetrahydrophthalic anhydride synthesis reaction and the like.
As an optimal technical scheme, gaseous dispersion module include the shell, the shell in be provided with the micropore membrane subassembly, the one end of micropore membrane subassembly seal, other end intercommunication intake pipe, the entry end of intake pipe stretch out the shell.
Preferably, one end of the microporous membrane component is sealed by a closed end cap.
Preferably, the side wall of the shell is communicated with a liquid inlet pipe, the gas-phase raw material and the liquid-phase raw material are respectively introduced into the shell through an air inlet pipe and the liquid inlet pipe, and the gas-phase raw material passes through the microporous membrane component to form micro-bubbles and is diffused into the liquid-phase raw material to obtain a reaction liquid.
Preferably, the axis of the liquid inlet pipe is tangential to the shell, and the liquid is fed along the tangential direction of the shell.
Preferably, the top of the shell is communicated with a discharge pipe.
Preferably, the microporous membrane assembly is surrounded by a microporous membrane.
Preferably, the membrane material of the microporous membrane comprises any one of high molecular polymer, ceramic or metal.
Preferably, the pore size of the microporous membrane is 0.1 to 100. mu.m, and may be, for example, 0.1. mu.m, 1. mu.m, 10. mu.m, 20. mu.m, 30. mu.m, 40. mu.m, 50. mu.m, 60. mu.m, 70. mu.m, 80. mu.m, 90. mu.m or 100. mu.m, but is not limited to the values listed, and other values not listed in the range of the values are also applicable.
Preferably, the microporous membrane assembly is an inverted truncated cone structure.
Preferably, the included angle between the truncated cone generatrix of the microporous membrane assembly and the horizontal plane is 0 to 180 °, and may be, for example, 1 °, 10 °, 20 °, 30 °, 40 °, 50 °, 60 °, 70 °, 80 °, 90 °, 100 °, 110 °, 120 °, 130 °, 140 °, 150 °, 160 °, 170 ° or 180 °, but is not limited to the enumerated values, and other non-enumerated values within the range of the enumerated values are also applicable, and more preferably 45 to 135 °.
In the utility model, all reaction raw materials are divided into a gas phase part and a liquid phase part according to the state, the liquid phase raw materials are introduced into the shell from the liquid inlet pipe, and simultaneously the gas phase raw materials are introduced into the shell as a dispersion phase from the gas inlet pipe; the gas phase raw material forms micron-sized micro-bubbles after passing through the microporous membrane component, the micro-sized micro-bubbles are quickly diffused into the shell to be mixed with the liquid phase, the micro-bubbles enter the reaction pipe fitting from the discharge pipe of the gas dispersion module under certain pressure and temperature and flow in parallel for reaction, and the generated reaction product is discharged.
The utility model discloses a microporous membrane structure of gas dispersion module makes gaseous phase raw materials evenly disperse with the form of microbubble and gets into in the liquid phase raw materials, and the phase interface between the gas-liquid increases more than 10 times than traditional reactor to can adjust the diameter control area of contact of microbubble through the aperture adjustment to microporous membrane subassembly, and then realize reaction system's miniaturization and high efficiency; the reaction raw materials after gas-liquid mixing enter the reaction pipe fitting, and the turbulent flow stopper or the filling filler of the reaction pipe fitting ensures to control the efficient operation of the reaction pipe fitting, thereby improving the reaction efficiency.
As a preferred technical scheme of the utility model, the reaction pipe fitting include from interior to exterior coaxial nested interior body and outer body in proper order, interior body let in heat transfer medium, interior body and outer body between form annular channel.
Preferably, both ends of the annular channel are sealed, both ends of the inner tube body are open, the outer tube body is provided with a feed inlet and a discharge outlet, reaction liquid is introduced into the annular channel through the feed inlet on the outer tube body, and the reaction liquid exchanges heat with a heat exchange medium in the inner tube body.
Preferably, the annular channel has a radial width of 1 to 30mm, for example 1mm, 5mm, 10mm, 15mm, 20mm, 25mm or 30mm, but not limited to the values listed, and other values not listed in this range are equally applicable.
The reaction raw materials after gas-liquid mixing enter the reaction pipe fitting, and the turbulent flow stopper or the filling filler of the reaction pipe fitting ensures to control the efficient operation of the reaction pipe fitting, thereby improving the reaction efficiency. The shell of the reaction device is filled with heat exchange medium, the heat exchange area is more than 10 times of that of a common reactor, rapid heat transfer can be realized, and the reaction temperature can be accurately controlled. Taking the reaction of synthesizing tetrahydrophthalic anhydride as an example, the reactor of the utility model increases the gas-liquid phase interface of butadiene and maleic anhydride, ensures that two phases are fully contacted and react quickly. Through the aperture adjustment to microporous membrane subassembly, regulate and control butadiene bubble diameter and make its even entering maleic anhydride liquid phase, react in the annular channel, further strengthen the mixing degree between gaseous phase raw materials and the liquid phase raw materials through the vortex fender piece to improve mass transfer efficiency, realize serialization production, have the great characteristics that the handling capacity is big and the energy consumption is little.
As an optimized technical scheme of the utility model, annular channel in be provided with at least two sets of vortex subassemblies along radial interval.
Preferably, each group of spoiler assemblies comprises at least three spoiler members arranged along the circumferential direction of the annular channel.
Preferably, the spoiler members included in two adjacent groups of spoiler assemblies are staggered.
Preferably, the shape of the spoiler comprises any one of a cylinder, a prism, a cone, a pyramid, a cube or a cuboid, or a combination of at least two groups.
Preferably, the material of the flow spoiler comprises any one or a combination of at least two groups of high molecular polymer, ceramic or metal.
The utility model provides a vortex keeps off piece's effect lies in: (1) the distance between the outer pipe and the inner pipe is strictly controlled, the concentricity of the outer pipe and the inner pipe is ensured, and the fluid does not generate a channeling effect; (2) the turbulence blocking piece in the annular channel can prevent bubbles or liquid drops from merging in the flowing process, simultaneously plays a role in turbulent flow of the fluid, increases the gas-liquid surface renewal and mass transfer in the flowing process, and improves the reaction efficiency.
Preferably, the annular channel is filled with filler.
Preferably, the shape of the filler comprises any one or a combination of at least two groups of spheres, rings, grids, waves or saddles.
Preferably, the filler material comprises any one or a combination of at least two groups of high molecular polymer, ceramic or metal.
The utility model discloses the purpose that sets up the filler is the same with the purpose that the vortex kept off the piece, all is used for preventing that bubble or liquid drop from taking place to gather at the flow in-process, plays turbulent effect simultaneously to the fluid, increases its gas-liquid surface update and mass transfer of flow in-process, improves reaction efficiency. Therefore, it can be understood that the reaction pipe fitting provided by the utility model can simultaneously use the filler and the turbulence blocking piece, and can only use the filler or the turbulence blocking piece.
As an optimal technical scheme of the utility model, casing top and bottom seted up heat transfer medium export and heat transfer medium entry respectively.
Preferably, the shell comprises a cylinder body and end sockets positioned at two ends of the cylinder body, and the end sockets are detachably connected with the cylinder body.
Preferably, the end socket is butted with the cylinder body through a flange.
Preferably, the shell is arranged vertically, and the reaction pipe fittings are longitudinally arranged in the shell side by side.
Preferably, both ends of the reaction pipe fitting are respectively provided with a fixing bracket, and the fixing brackets are used for fixing the reaction pipe fitting in the shell.
As an optimal technical scheme of the utility model, the reaction pipe fitting adopt parallel connection, the reaction module still include the feeding and be responsible for and the ejection of compact is responsible for, the entrance point and the exit end of reaction pipe fitting insert the feeding respectively and be responsible for and the ejection of compact is responsible for.
Preferably, the discharge pipe of the gas dispersion module is connected to the main feed pipe, and the reaction liquid discharged from the gas dispersion module is introduced into the main feed pipe through the discharge pipe and distributed to flow into the annular channels of the respective reaction pipe members.
Preferably, when the reaction pipe fitting adopts the series connection mode, along the reaction liquid flow direction, the row of gas dispersion module expect the feed inlet of pipe access first reaction pipe fitting, the feed inlet of next reaction pipe fitting is connected to the discharge gate of first reaction pipe fitting, according to this connected mode, each reaction pipe fitting is established ties in proper order along the reaction liquid flow direction, the reaction liquid through gas dispersion module exhaust lets in first reaction pipe fitting by arranging the material pipe, the annular channel of each reaction pipe fitting of flowing through in proper order afterwards.
Compared with the prior art, the beneficial effects of the utility model are that:
the gas-liquid reaction device provided by the utility model is divided into a gas-liquid two-phase fluid mixing area and a main reaction area, the gas dispersion module is positioned in the gas-liquid two-phase fluid mixing area, the rapid and efficient mixing reaction of two immiscible fluids in large-scale production can be realized, meanwhile, the heat can be rapidly transferred, the side reaction is inhibited, the selectivity of the product is improved, the treatment capacity is large, and the energy consumption is small; the reaction pipe fittings are positioned in the main reaction zone, and when the gas-liquid multiphase material reaction time needs to be prolonged, the length of the reaction pipe fittings can be lengthened or the number of the reaction pipe fittings can be increased according to the needs. The utility model discloses a reaction unit simple structure, the double-phase area of contact of gas-liquid is big, and no mechanical stirring part is difficult for leaking, possesses reaction temperature accurate control, good mass transfer and heat transfer performance, reaction pressure adjustable range big, reaction time is adjustable, the reaction process material stock is few, the security is strong, can realize performances such as serialization production, extensive adaptability. The method can realize the rapid and efficient mixing reaction of gas and liquid in large-scale production, and simultaneously inhibit side reaction by accurately controlling reaction conditions, thereby improving the selectivity of products. Can be widely used in the field of petrochemical industry, and is particularly suitable for gas-liquid multiphase reactions, such as tetrahydrophthalic anhydride synthesis reaction and the like.
Drawings
Fig. 1 is a schematic structural diagram of a gas dispersion module according to an embodiment of the present invention;
FIG. 2 is a schematic structural diagram of a reaction tube according to an embodiment of the present invention;
FIG. 3 is a schematic structural view of a gas-liquid reaction apparatus according to an embodiment of the present invention;
wherein, 1-microporous membrane component; 2-closing the end cover; 3-a discharge pipe; 4-a housing; 5-a liquid inlet pipe; 6, an air inlet pipe; 7-an outer body; 8-an inner tube; 9-an annular channel; 10-a spoiler; 11-a feed inlet; 12-a discharge hole; 13-heat exchange medium inlet; 14-a flange; 15-a housing; 16-a fixed support; 17-a heat exchange medium outlet; 18-reaction tube; 19-gas dispersion module.
Detailed Description
It is to be understood that in the description of the present invention, the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc., indicate orientations or positional relationships based on those shown in the drawings, and are used only for convenience in describing the present invention and for simplicity in description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be taken as limiting the present invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
It should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "disposed," "connected" and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
It should be understood that the present invention includes the necessary pipeline, conventional valve and general pump equipment for realizing the complete process, but the above contents do not belong to the main invention point of the present invention, and the skilled person can select the type based on the process flow and the equipment structure to add the layout by himself, and the present invention does not have the special requirement and limitation.
The technical solution of the present invention is further explained by the following embodiments with reference to the accompanying drawings.
In a specific embodiment, the utility model provides a gas-liquid reaction device, gas-liquid reaction device as shown in fig. 3, including casing 15, be provided with in casing 15 along the gas dispersion module 19 and the reaction module that the reaction liquid flow direction connects gradually, the reaction module includes two at least reaction pipe fittings 18, reaction pipe fitting 18 parallel connection or along the reaction liquid flow direction series connection in proper order. The top and the bottom of the shell 15 are respectively provided with a heat exchange medium outlet 17 and a heat exchange medium inlet 13. The shell 15 comprises a cylinder body and end sockets positioned at two ends of the cylinder body, the end sockets are detachably connected with the cylinder body, and further the end sockets are butted with the cylinder body through a flange 14. The housing 15 is arranged vertically, and the reaction tubes 18 are arranged longitudinally side by side inside the housing 15. Fixing brackets 16 are respectively provided at both ends of reaction pipe 18, and fixing brackets 16 are used to fix reaction pipe 18 in housing 15.
When the reaction pipe fittings 18 adopt a parallel connection mode, the reaction module further comprises a feeding main pipe and a discharging main pipe, the inlet end and the outlet end of the reaction pipe fittings 18 are respectively connected with the feeding main pipe and the discharging main pipe, the gas dispersion module 19 is connected with the feeding main pipe, and gas raw materials and liquid raw materials are uniformly dispersed by the gas-liquid disperser and then flow into the feeding main pipe and are distributed by the feeding main pipe to enter each reaction pipe fitting 18.
When the reaction pipe fittings 18 are connected in series, the gas dispersion module 19 is connected to the inlet end of the first reaction pipe fitting 18 along the flow direction of the reaction liquid, and the gas raw material and the liquid raw material are uniformly dispersed by the gas-liquid disperser and then sequentially flow through the reaction pipe fittings 18.
As shown in fig. 1, the gas dispersion module 19 includes a housing 4, a microporous membrane module 1 is disposed in the housing 4, one end of the microporous membrane module 1 is sealed, the other end is communicated with a gas inlet pipe 6, and an inlet end of the gas inlet pipe 6 extends out of the housing 4. Further, one end of the microporous membrane assembly 1 is sealed by a cap closure 2. The side wall of the shell 4 is communicated with a liquid inlet pipe 5, a gas phase raw material and a liquid phase raw material are respectively introduced into the shell 4 through an air inlet pipe 6 and the liquid inlet pipe 5, and the gas phase raw material forms micro bubbles after passing through the microporous membrane component 1 and is diffused into the liquid phase raw material to obtain a reaction liquid. The axis of the liquid inlet pipe 5 is tangential to the shell 4, and liquid is fed along the tangential direction of the shell 4. The top of the shell 4 is communicated with a discharge pipe 3.
The microporous membrane component 1 is surrounded by microporous membranes, the membrane material of the microporous membranes comprises any one of high molecular polymer, ceramics or metal, and the aperture of the microporous membranes is 0.1-100 mu m. The microporous membrane component 1 is of an inverted round table-shaped structure, and the included angle between a round table bus of the microporous membrane component 1 and the horizontal plane is 0-180 degrees.
As shown in fig. 2, the reaction pipe 18 includes an inner pipe 8 and an outer pipe 7 coaxially nested from inside to outside, the inner pipe 8 is filled with a heat exchange medium, and an annular channel 9 is formed between the inner pipe 8 and the outer pipe 7. The two ends of the annular channel 9 are sealed, the two ends of the inner pipe body 8 are open, the outer pipe body 7 is provided with a feed inlet 11 and a discharge outlet 12, reaction liquid is introduced into the annular channel 9 through the feed inlet 11 on the outer pipe body 7, and the reaction liquid exchanges heat with a heat exchange medium in the inner pipe body 8. The radial width of the annular channel 9 is 1-30 mm.
At least two groups of turbulence components are arranged in the annular channel 9 at intervals along the radial direction, each group of turbulence components comprises at least three turbulence blocking pieces 10 arranged along the circumferential direction of the annular channel 9, and the turbulence blocking pieces 10 included in the two adjacent groups of turbulence components are distributed in a staggered mode. The shape of the turbulence stopper 10 includes any one or a combination of at least two groups of a cylinder, a prism, a cone, a pyramid, a cube or a cuboid, and the material of the turbulence stopper 10 includes any one or a combination of at least two groups of a high polymer, a ceramic or a metal. The annular channel 9 is also filled with a filler, the shape of the filler comprises any one or the combination of at least two groups of spherical, annular, grid-shaped, corrugated or saddle-shaped fillers, and the material of the filler comprises any one or the combination of at least two groups of high polymer, ceramic or metal.
The reaction pipe fittings 18 are connected in parallel, the discharge pipe 3 of the gas dispersion module 19 is connected to the feed main pipe, the feed ports 11 of the reaction pipe fittings 18 are respectively connected to the feed main pipe, and the reaction liquid discharged by the gas dispersion module 19 is introduced into the feed main pipe through the discharge pipe 3 and distributed to flow into the annular channels 9 of the reaction pipe fittings 18.
When the reaction pipe fittings 18 are connected in series, the discharge pipe 3 of the gas dispersion module 19 is connected to the feed inlet 11 of the first reaction pipe fitting 18 along the flow direction of the reaction liquid, the discharge outlet 12 of the first reaction pipe fitting 18 is connected to the feed inlet 11 of the next reaction pipe fitting 18, according to the connection mode, the reaction pipe fittings 18 are sequentially connected in series along the flow direction of the reaction liquid, the reaction liquid discharged by the gas dispersion module 19 is introduced into the first reaction pipe fitting 18 through the discharge pipe 3, and then sequentially flows through the annular channels 9 of the reaction pipe fittings 18.
In another embodiment, the present invention provides a method for performing a gas-liquid reaction by using the gas-liquid reaction apparatus provided in the above embodiment, the method specifically includes the following steps:
(1) respectively introducing a gas-phase raw material and a liquid-phase raw material into a gas dispersion module 19, wherein the gas-phase raw material penetrates through the microporous membrane component 1 at a linear velocity of 0.1-25 m/s to form micro bubbles and diffuses into the liquid-phase raw material to obtain a reaction solution;
(2) the reaction liquid flows into the annular channel 9 of the reaction pipe 18 at a linear speed of 0.05-10 m/s, meanwhile, a heat exchange medium is introduced into the inner pipe 8 of the reaction pipe 18, the reaction liquid and the heat exchange medium are in contact for heat exchange, and the reaction temperature is controlled through the temperature of the heat exchange medium.
The applicant states that the above description is only a specific embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and those skilled in the art should understand that any changes or substitutions easily conceivable by those skilled in the art within the technical scope of the present invention are within the protection scope and the disclosure scope of the present invention.
Claims (6)
1. The gas-liquid reaction device is characterized by comprising a shell, wherein a gas dispersion module and a reaction module which are sequentially connected along the flow direction of reaction liquid are arranged in the shell;
the reaction module comprises at least two reaction pipe fittings which are connected in parallel or connected in series in sequence along the flow direction of reaction liquid.
2. The gas-liquid reaction device as recited in claim 1, wherein the gas dispersion module includes a housing, a microporous membrane module disposed in the housing, and a liquid inlet pipe;
one end of the microporous membrane component is sealed, the other end of the microporous membrane component is communicated with an air inlet pipe, and the inlet end of the air inlet pipe extends out of the shell; one end of the microporous membrane component is sealed through a closed end cover;
the side wall of the shell is communicated with a liquid inlet pipe, a gas-phase raw material and a liquid-phase raw material are respectively introduced into the shell through an air inlet pipe and the liquid inlet pipe, and the gas-phase raw material forms micro bubbles after passing through the microporous membrane component and is diffused into the liquid-phase raw material to obtain a reaction liquid;
the axis of the liquid inlet pipe is tangent to the shell, and liquid is fed along the tangent direction of the shell;
the top of the shell is communicated with a discharge pipe;
the microporous membrane component is surrounded by a microporous membrane;
the aperture of the microporous membrane is 0.1-100 mu m;
the microporous membrane component is of an inverted round table structure;
the included angle between the round platform bus of the microporous membrane component and the horizontal plane is 0-180 degrees.
3. The gas-liquid reaction device as recited in claim 1, wherein the reaction module includes an inner tube and an outer tube coaxially nested in sequence from inside to outside, and an annular channel is formed between the inner tube and the outer tube; the inner pipe body is filled with a heat exchange medium;
two ends of the annular channel are sealed, two ends of the inner pipe body are open, a feed inlet and a discharge outlet are formed in the outer pipe body, reaction liquid is introduced into the annular channel through the feed inlet in the outer pipe body, and the reaction liquid exchanges heat with a heat exchange medium in the inner pipe body;
the radial width of the annular channel is 1-30 mm.
4. The gas-liquid reaction device as recited in claim 3, wherein at least two sets of flow perturbation elements are radially spaced in the annular channel;
each group of turbulence components comprises at least three turbulence stoppers arranged along the circumferential direction of the annular channel;
the turbulent flow stoppers in the two adjacent groups of turbulent flow assemblies are distributed in a staggered way;
the shape of the turbulence stoppers comprises any one or the combination of at least two groups of cylinders, prisms, cones, pyramids, cubes or cuboids;
the annular channel is filled with filler; the shape of the filler comprises any one or the combination of at least two groups of spherical shape, annular shape, grid shape, corrugated shape or saddle shape.
5. The gas-liquid reaction device according to any one of claims 1 to 2, wherein the top and bottom of the shell are respectively provided with a heat exchange medium outlet and a heat exchange medium inlet;
the shell comprises a cylinder body and end sockets positioned at two ends of the cylinder body, and the end sockets are detachably connected with the cylinder body; the end socket is butted with the cylinder body through a flange; the shell is vertically arranged, and the reaction pipe fittings are longitudinally arranged in the shell side by side; the two ends of the reaction pipe fitting are respectively provided with a fixing support, and the fixing supports are used for fixing the reaction pipe fitting in the shell.
6. The gas-liquid reaction device according to any one of claims 1 to 5, wherein the reaction pipe members are connected in parallel, the reaction module further comprises a main feed pipe and a main discharge pipe, and an inlet end and an outlet end of the reaction pipe members are respectively connected to the main feed pipe and the main discharge pipe;
a discharge pipe of the gas dispersion module is connected to the feeding main pipe, and reaction liquid discharged by the gas dispersion module is introduced into the feeding main pipe through the discharge pipe and distributed to flow into the annular channels of the reaction pipe fittings;
when the reaction pipe fitting adopt series connection, along the reaction liquid flow direction, the row of gas dispersion module expect the feed inlet of pipe access first reaction pipe fitting, the feed inlet of next reaction pipe fitting is connected to the discharge gate of first reaction pipe fitting, according to this connected mode, each reaction pipe fitting is established ties in proper order along the reaction liquid flow, lets in first reaction pipe fitting through row's material pipe to the reaction liquid of gas dispersion module exhaust, the annular channel of each reaction pipe fitting of flowing through in proper order afterwards.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120369462.6U CN214716658U (en) | 2021-02-10 | 2021-02-10 | Gas-liquid reaction device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120369462.6U CN214716658U (en) | 2021-02-10 | 2021-02-10 | Gas-liquid reaction device |
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| Publication Number | Publication Date |
|---|---|
| CN214716658U true CN214716658U (en) | 2021-11-16 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120369462.6U Active CN214716658U (en) | 2021-02-10 | 2021-02-10 | Gas-liquid reaction device |
Country Status (1)
| Country | Link |
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| CN (1) | CN214716658U (en) |
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2021
- 2021-02-10 CN CN202120369462.6U patent/CN214716658U/en active Active
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