CN110860263B - High-efficiency reactor - Google Patents
High-efficiency reactor Download PDFInfo
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- CN110860263B CN110860263B CN201911382119.9A CN201911382119A CN110860263B CN 110860263 B CN110860263 B CN 110860263B CN 201911382119 A CN201911382119 A CN 201911382119A CN 110860263 B CN110860263 B CN 110860263B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0093—Microreactors, e.g. miniaturised or microfabricated reactors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00819—Materials of construction
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00873—Heat exchange
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00889—Mixing
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The invention discloses a high-efficiency reactor, which relates to the technical field of reactors and comprises a reaction device, a heat exchange shell and a heat exchange layer, wherein the reaction device is fixed in the heat exchange shell, the heat exchange layer is positioned between the reaction device and the heat exchange shell, the heat exchange layer is provided with a heat exchange inlet and a heat exchange outlet, the reaction device is provided with a reaction inlet and a reaction outlet, the reaction inlet and the reaction outlet penetrate through the heat exchange shell, the reaction device is internally provided with a reaction layer, and the reaction layer is a fiber module. The invention has the characteristics of simple structure, mass production and good mass transfer efficiency and heat exchange effect, and the fiber module is used as a reaction layer, so that the mixing effect of reactants is improved.
Description
Technical Field
The invention relates to the technical field of reactors, in particular to a high-efficiency reactor.
Background
The chemical industry is closely related to our daily production activities and lives, and medicines, high molecular polymers, petroleum and the like are all products of the chemical industry. In traditional chemical production equipment, the tank reactor and the large-pipe-diameter pipe reactor can meet the large-scale production requirement, but the defects of high energy consumption, poor safety, serious environmental pollution and the like in the production process are gradually revealed along with the improvement of the energy-saving and environment-friendly requirements of production enterprises. In addition, the traditional chemical equipment is used for mixing fluid on a macroscopic scale, has low mixing efficiency and poor heat exchange performance, and is difficult to solve the problems of mass transfer and heat transfer accompanied by chemical reaction, so that the reaction efficiency is low and the safety is poor. Therefore, when the reaction is amplified from laboratory scale to industrial production, data deviation occurs by using the traditional large-volume reaction equipment, so that the defects of long amplification period, poor amplification effect and the like are caused, and the preparation of some fine chemical products is not facilitated.
In order to solve the above problems, a microchannel reactor has been receiving a great deal of attention in recent years. The microchannel reactor is a continuous reactor with small size and ultra-large specific surface area, and is characterized in that the size of the channel is usually in the micron order (50-1000 μm), so that reactants can react at the micron order, and the uniformity and the ideality of fluid flow are ensured. Compared with the traditional large-scale kettle type or pipe type equipment, the heat transfer and mass transfer performance of the reactor is obviously enhanced, so that the conversion rate, the selectivity and the operation safety of the reaction can be obviously improved by the micro-channel reactor. The microchannel reactor can perform homogeneous catalytic reaction, and can load catalyst on the pipe wall to perform heterogeneous catalytic reaction. The reaction system can take a single micro-channel reactor as a basic unit, and realizes the parallel connection of multiple reactors according to actual reaction requirements. The number increase effect can save a pilot scale link, realize the amplification of no side effect from experimental research to industrial production, shorten the amplification period, save the test cost and promote the integration of obstetrics and research. In addition, the reaction units of the microchannel reactor are mutually independent, so that the microchannel reactor has a simple structure, is easy to control the operation conditions, and is convenient to split, inspect and clean in the application process.
But the prior micro-channel reactor has low internal space utilization rate, small flow range of reaction materials, low mixing efficiency and low processing efficiency, is only suitable for laboratory research, and is difficult to meet the requirements of industrial production. In addition, the existing different processing methods have various disadvantages, such as acid-base waste liquid polluting the environment generated by a chemical etching method; the laser etching production efficiency is low and is limited to the processing of micro-fluidic chips with small sizes; ion etching is limited to silicon-based materials and polymers, and the processing quality is also affected by the depth-to-width ratio; the molding method requires manufacturing a high-cost precise micro-channel grinding tool; special micro machining technologies such as fine electric spark machining and the like are complex in process and long in period; microinjection molding is prone to formation into small cracks and the like.
Therefore, there is an urgent need in the market for a new reactor for solving the above problems.
Disclosure of Invention
The invention aims to provide a high-efficiency reactor which is used for solving the technical problems in the prior art, effectively reducing the manufacturing cost and improving the mass transfer effect and the heat exchange performance.
In order to achieve the above object, the present invention provides the following solutions:
The invention discloses a high-efficiency reactor, which comprises a reaction device and a heat exchange shell, wherein the reaction device is fixed in the heat exchange shell, a heat exchange layer is positioned between the reaction device and the heat exchange shell, the heat exchange layer is provided with a heat exchange inlet and a heat exchange outlet, the reaction device is provided with a reaction inlet and a reaction outlet, the reaction inlet and the reaction outlet both pass through the heat exchange shell, and a reaction layer is also arranged in the reaction device.
Preferably, the fiber module is sinter molded or compression molded.
Preferably, the fibre module is a stack of screens woven from fibres.
Preferably, the fiber module is formed by winding or folding fiber felts sintered by fibers.
Preferably, the fiber module comprises one or more of basalt fiber, ceramic fiber, glass fiber, metal fiber or asbestos fiber, the basalt fiber has a diameter of 0.1 μm to 200 μm, the ceramic fiber has a diameter ranging from 0.01 μm to 50 μm, the glass fiber has a diameter of 0.01 μm to 5mm, and the metal fiber has a diameter of 1 μm to 500 μm.
Preferably, the fiber module is subjected to one or more of spray pyrolysis, dipping, non-plasma deposition, anodic oxidation, atomic layer deposition, electroless plating, chemical vapor deposition, galvanic deposition, acid-base treatment, oxidation treatment, low temperature plasma treatment, coupling agent treatment, or adhesive treatment.
Preferably, the heat exchange shell comprises a first shell, the reaction device is a reaction chamber, the heat exchange inlet, the heat exchange outlet, the reaction inlet and the reaction outlet are respectively a first heat exchange inlet, a first heat exchange outlet, a first reaction inlet and a first reaction outlet, the reaction layer is a first reaction layer, the reaction chamber is fixed in the first shell, the first reaction layer is fixed in the reaction chamber, a first heat exchange cavity is arranged between the reaction chamber and the first shell, first ends of the first heat exchange inlet and the first heat exchange outlet are communicated with the first heat exchange cavity, second ends of the first heat exchange inlet and the first heat exchange outlet are positioned on the outer side of the first shell, first ends of the first reaction inlet and the first reaction outlet are communicated with an inner cavity of the reaction chamber, second ends of the first reaction inlet and the first reaction outlet are positioned on the outer side of the first shell, the first reaction layer, the first shell and the first heat exchange chamber are positioned on the first side wall of the first shell, the first heat exchange inlet and the first side wall are positioned on the first side wall of the first shell, and the first side wall is provided with the first heat exchange inlet and the first side wall.
Preferably, the reactor further comprises a plurality of support rods, the reactor is a reaction pipeline, the reaction pipeline is sequentially provided with a second reaction inlet, a second reaction inlet liquid collecting tank, a plurality of branch pipes, a second reaction outlet liquid collecting tank and a second reaction outlet, the heat exchange shell comprises a second shell, the second reaction inlet and the second reaction outlet respectively penetrate through the corresponding two ends of the second shell, the first ends of the support rods are fixed on the inner wall of the second shell, the second ends of the support rods are fixed on the outer wall of the branch pipes, and the reaction layer is a second reaction layer which is fixed in the branch pipes.
Preferably, the heat exchange shell comprises an upper sealing plate, a top heat exchange layer and a bottom heat exchange layer, the reaction device comprises a substrate and a third reaction layer, the two ends of the top heat exchange layer and the bottom heat exchange layer are respectively provided with a third heat exchange inlet liquid collecting tank and a third heat exchange outlet heat collecting tank, a heat exchange flow field is arranged between the third heat exchange inlet liquid collecting tank and the third heat exchange outlet heat collecting tank, the two third heat exchange inlet liquid collecting tanks are opposite in position, the two third heat exchange inlet liquid collecting tanks are communicated through a first connecting channel, the two third heat exchange outlet heat collecting tanks are opposite in position, the two third heat exchange outlet heat collecting tanks are communicated through a second connecting channel, the lower surface of the top heat exchange layer is provided with a reaction groove, the upper sealing plate is fixed on the upper surface of the top heat exchange layer, the third reaction layer is fixed on the upper surface of the substrate, the third reaction layer is positioned in the reaction groove, the upper surface of the substrate is fixed on the lower surface of the top heat exchange layer, the lower surface of the substrate is fixed on the upper surface of the bottom heat exchange layer, the reaction inlet is a third reaction inlet, the reaction outlet is a third reaction outlet, the first end of the third reaction inlet is positioned on the first side of the third reaction layer, the second end of the third reaction inlet is positioned above the top heat exchange layer, the first end of the third reaction outlet is positioned on the second side of the third reaction layer, the second end of the third reaction outlet is positioned above the top heat exchange layer, the heat exchange inlet and the heat exchange outlet are respectively a third heat exchange inlet and a third heat exchange outlet, the first end of the third heat exchange inlet is positioned at the third heat exchange inlet liquid collecting groove of the top heat exchange layer, the second end of the third heat exchange inlet is positioned above the top heat exchange layer, the first end of the third heat exchange outlet is positioned in the third heat exchange outlet liquid collecting tank on the bottom heat exchange layer, and the second end of the third heat exchange outlet is positioned outside the bottom heat exchange layer.
Preferably, the device further comprises a plurality of sealing rings, bolts and nuts, wherein the sealing rings are respectively fixed between the third reaction layer and the inner wall of the reaction groove, between the top heat exchange layer and the base plate, and between the bottom heat exchange layer and the base plate, a plurality of through holes are formed in the corresponding positions of the top heat exchange layer, the base plate and the bottom heat exchange layer, and the bolts penetrate through the through holes and are in threaded connection with the nuts.
Compared with the prior art, the invention has the following technical effects:
The invention avoids the use of precision processing technologies such as chemical etching, laser etching, injection molding, wire cutting, electric spark machining and the like to manufacture the micro-channel when preparing the reactor, and has low processing and manufacturing cost; the three-dimensional structure pore micro-channels formed by stacking and interlacing the fibers can realize an ultrahigh mixing effect in a short time, and have good mass transfer and heat transfer performances. The material of the fiber product has wide selection range, and proper fiber material can be selected according to specific reaction requirements, so that the universality is good. The fiber product can be subjected to surface treatment or coating treatment to increase the specific surface area, roughness and surface energy, adjust the chemical property of the surface and change the surface charge distribution, thereby being beneficial to the loading of the subsequent catalyst. The reaction efficiency is high, the selectivity is high, the structure is simple, the operation is convenient, the control is accurate, the safety is high, and the mass production can be realized.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings that are needed in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a high-efficiency reactor according to an embodiment;
FIG. 2 is a cross-sectional view of a high efficiency reactor according to an embodiment;
FIG. 3 is a schematic diagram of a second embodiment;
FIG. 4 is a schematic view of a third embodiment;
FIG. 5 is a schematic view of a top heat exchange layer structure in a third embodiment;
FIG. 6 is a schematic view of a bottom heat exchange layer structure in a third embodiment;
FIG. 7 is a schematic diagram of a third substrate and a third reaction layer structure according to an embodiment;
FIG. 8 is a schematic view of a fiber module structure;
In the figure: 1-a first housing; 2-a first heat exchange cavity; 3-inner wall of the shell; 4-a first reaction layer; 5-a first reaction inlet; 6-a first reaction outlet; 7-a first heat exchange inlet; 8-a first heat exchange outlet; 9. a second housing; 10. a second heat exchange chamber; 11. a second reaction layer; 12. the outer wall of the branch pipe; 13. a support rod; 14. a second reaction inlet; 15. a second reaction outlet; 16. a second reaction inlet sump; 17. a second reaction outlet sump; 18. a second heat exchange outlet; 19. a second heat exchange inlet; 20. an upper sealing plate; 21. a top heat exchange layer; 22. a third reaction layer; 23. a bottom heat exchange layer; 24. a third reaction inlet; 25. a third reaction outlet; 26. a third heat exchange inlet; 27. a third heat exchange outlet; 28. a third heat exchange inlet sump; 29. a third heat exchange outlet sump; 30. a heat exchange flow field; 31. a substrate.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
The invention aims to provide a high-efficiency reactor which is used for solving the technical problems in the prior art, effectively reducing the manufacturing cost and improving the mass transfer effect and the heat exchange performance.
In order that the above-recited objects, features and advantages of the present invention will become more readily apparent, a more particular description of the invention will be rendered by reference to the appended drawings and appended detailed description.
Embodiment 1,
As shown in fig. 1-2, this embodiment provides a high efficiency reactor comprising a reaction device, a heat exchange shell and a heat exchange layer. The reaction device is fixed in the heat exchange shell, and the reaction device is used for carrying out chemical reaction, and the heat exchange shell ensures the required temperature in the reaction process. The heat exchange layer is positioned between the reaction device and the heat exchange shell, and is provided with a heat exchange inlet and a heat exchange outlet, a heat exchange medium flows in from the heat exchange inlet, flows out from the heat exchange outlet, and the heat exchange medium can heat the reaction device and also can dissipate heat in the heat exchange layer. For the reaction requiring heating, the heat exchange medium flowing through the reaction kettle can be constant-temperature hot water, hot oil and the like; for the reaction requiring heat dissipation, the medium flowing through the reaction chamber can be cooling water, refrigerant working medium and the like. The reaction device is provided with a reaction inlet and a reaction outlet, the reaction inlet and the reaction outlet penetrate through the heat exchange shell, a reaction layer is further arranged in the reaction device, the reaction layer is a fiber module, and the fiber module can increase the mixing effect of reactants.
The shape of the reaction layer may be different according to different reaction devices, and the fiber module in this embodiment is formed by sintering or compression molding. The reaction layer is then filled into the reaction device after being sintered or molded directly according to the shape of the inner cavity of the reaction device.
Similarly, in this embodiment, the fiber module is formed by stacking silk screens woven from fibers. And then in a reaction apparatus having a different shape.
Similarly, in this embodiment, the fiber module is formed by winding or folding a fiber mat sintered by fibers. The fibers are now sintered into a fiber mat, which is then rolled, folded or otherwise formed into a specific three-dimensional structure (see fig. 8) and then installed in a reaction apparatus.
The channels of the fiber modules are three-dimensional structure pores formed by stacking and interlacing the fibers, and the channels extend irregularly in the axial direction and the radial direction of the three-dimensional structure, so that a plurality of irregularly-bent heat exchange layers are formed from the inlet surface to the outlet surface, the specific surface area inside the reactor is greatly increased, the preparation process is greatly simplified, and the preparation difficulty and the preparation cost are reduced. In addition, the irregular and tortuous heat exchange layer built by fibers is beneficial to fluid mixing and shows more excellent mass and heat transfer performance.
The specific material of the fiber module comprises inorganic fibers and organic fibers. Wherein the inorganic fibers include, but are not limited to, basalt fibers, ceramic fibers, glass fibers, metal fibers, asbestos fibers, and the like. Organic fibers include, but are not limited to, polymeric fibers, cellulose nanofibers, and the like. The fiber material in the present embodiment may be a modified material of the above materials, or may be any combination of the above materials. The appropriate fibrous material may be selected according to the particular application.
The material suitable for the microstructure of the fiber module can be basalt fiber belonging to aluminosilicate series. The basalt fiber composite material can be basalt fiber or continuous basalt fiber composite material. The basalt fiber can be chopped basalt fiber or continuous basalt fiber. The basalt fiber has a diameter ranging from 0.1 mu m to 200 mu m and a density ranging from 0.01g/cm 3-5g/cm3. The basalt fiber mainly comprises silicon dioxide, aluminum oxide, ferric oxide, ferrous oxide, titanium dioxide, sodium oxide and the like. The basalt fiber microstructure has the advantages of acid and alkali resistance, oxidation resistance, high temperature resistance, low cost, good mechanical property, environmental protection and the like.
The material suitable for the microstructure of the fiber module can be ceramic fibers, including ceramic fibers such as aluminum silicate, silicon carbide, boron nitride, zirconium oxide, aluminum oxide and the like. Either in filament form or as staple fibers. The ceramic fiber has a diameter ranging from 0.01 μm to 50 μm. The porous ceramic fiber module microstructure has the advantages of large specific surface area, easy catalyst coating, high strength, high thermal stability, light weight and the like. Specific examples are ceramic fibers having a main component of 0.67% ferric oxide, 0.3% silicon oxide, and the balance aluminum oxide.
The material suitable for the microstructure of the fiber module can be glass fiber, and the chemical composition of the fiber module is mainly silicon dioxide and boron trioxide. Including alkali-free glass fibers, medium alkali glass fibers, high alkali glass fibers, alkali-resistant glass fibers, acid-resistant glass fibers, high temperature-resistant glass fibers, high strength glass fibers, and high modulus glass fibers. The fiber can be continuous long fiber or discontinuous short fiber. The diameter of the glass fiber is in the range of 0.01 μm to 5mm. The glass fiber module microstructure has the characteristics of low thermal expansion coefficient, flexibility, low cost and high chemical stability, and a proper glass fiber material can be selected according to specific practical application.
Suitable materials for the microstructure of the fiber module may be polymeric fibers including, but not limited to, aramid fibers (para-aramid fibers and meta-aramid fibers), polyethylene fibers, polyvinyl alcohol fibers, polypropylene fibers, polyacrylonitrile fibers, polyimide fibers, polyphenylene sulfide fibers, polytetrafluoroethylene fibers, polyvinylidene fluoride fibers. Any combination of the above fibers is also possible. The polymer fiber has the excellent performances of ultra-high strength, high modulus, high temperature resistance, acid resistance, alkali resistance, light weight and the like,
Suitable materials for the microstructure of the fiber module may be metal fibers including, but not limited to, stainless steel, nickel, copper, titanium, aluminum, hastelloy, inconel, fecralloy alloy, titanium alloy. The diameter of the metal fiber ranges from 1 μm to 500 μm. The fiber may be a drawn fiber, or may be a cut fiber. The fiber prepared by the cutting method has a rough surface structure and large specific surface area, and is favorable for the adhesion of the catalyst carrier and the catalyst. The metal fiber has high heat conductivity and good mechanical property, and can be selected into proper metal fiber materials according to a specific reaction system. Some alloy fibers have catalytic properties themselves and can be directly applied to specific reactions.
In order to increase the specific surface area of the fiber module, improve the roughness of the fiber module, increase the surface energy of the fiber, adjust the chemical property of the fiber surface, change the charge distribution of the fiber surface, the material suitable for the microstructure of the fiber module can be subjected to surface treatment or coating treatment. Techniques for growing the coating include, but are not limited to, spray pyrolysis, dipping, non-plasma deposition, anodic oxidation, atomic layer deposition, electroless plating, chemical vapor deposition, galvanic deposition, and the like. The surface treatment method includes, but is not limited to, acid-base treatment, oxidation treatment, low-temperature plasma treatment, coupling agent treatment, adhesive treatment, and the like.
Specifically, the heat exchange shell comprises a first shell 1, the reaction device is a reaction chamber, the heat exchange inlet, the heat exchange outlet, the reaction inlet and the reaction outlet are respectively a first heat exchange inlet 7, a first heat exchange outlet 8, a first reaction inlet 5 and a first reaction outlet 6, and the reaction layer is a first reaction layer 4. The reaction chamber is fixed in the first shell 1, the reaction chamber and the first shell 1 are designed as a whole, and the reaction chamber and the first shell 1 cannot mutually communicate. The first reaction layer 4 is fixed in the reaction chamber, and the first reaction layer 4 allows the reactants to be fully mixed. A first heat exchange cavity 2 is arranged between the reaction chamber and the first shell 1, first ends of a first heat exchange inlet 7 and a first heat exchange outlet 8 are communicated with the first heat exchange cavity 2, and a heat exchange medium flows in the first heat exchange cavity 2. The second ends of the first heat exchange inlet 7 and the first heat exchange outlet 8 are positioned outside the first shell 1, so that the heat exchange medium is conveniently led in and led out. The first ends of the first reaction inlet 5 and the first reaction outlet 6 are communicated with the inner cavity of the reaction chamber, and the second ends of the first reaction inlet 5 and the first reaction outlet 6 are positioned on the outer side of the first shell 1, so that the arrangement is convenient for leading in and leading out reactants.
In use, reactants enter from the first reaction inlet 5. Meanwhile, a proper heat exchange medium is led in from the first heat exchange inlet 7 as required, and the heat exchange medium is fully contacted with the inner wall 3 of the shell of the reaction chamber, so that after heat exchange, the heat exchange medium is led out from the first heat exchange outlet 8, and the temperature in the reaction chamber is ensured to be constant. The reactants are sufficiently mixed after passing through the first reaction layer 4, thereby improving reaction efficiency. The product after the reaction is discharged from the first reaction outlet 6, and then collected.
Further, in this embodiment, the first reaction layer 4, the first housing 1 and the reaction chamber are all cylinders. The first heat exchange inlet 7 and the first heat exchange outlet 8 are both positioned on the side wall of the first shell 1, and the first heat exchange inlet 7 and the first heat exchange outlet 8 are diagonally arranged, so that the heat exchange medium can be led out after being fully subjected to heat exchange in the first heat exchange cavity 2. The first reaction inlet 5 is located on one end plane of the first housing 1, and the first reaction outlet 6 is located on the side wall of the first housing 1 and far away from the first reaction inlet 5, so that reactants can be sufficiently reacted and then led out, and incomplete reaction is avoided.
Embodiment II,
As shown in fig. 3, this embodiment is an improvement on the basis of the first embodiment in that: the reaction device is a reaction pipeline, and the reaction pipeline is sequentially provided with a second reaction inlet 14, a second reaction inlet liquid collecting tank 16, a plurality of branch pipes, a second reaction outlet liquid collecting tank 17 and a second reaction outlet 15, and is designed as an integral body. The heat exchange housing comprises a second housing 9, the second housing 9 is a hollow cylinder, and a second reaction inlet 14 and a second reaction outlet 15 respectively penetrate through the upper bottom surface and the lower bottom surface of the second housing 9. A second heat exchange chamber 10 is formed between the second housing 9 and the reaction tube, the second heat exchange chamber 10 having a second heat exchange inlet 19 and a second heat exchange outlet 18. The first end of the supporting rod 13 is fixed on the inner wall of the second housing 9, and the second end of the supporting rod 13 is fixed on the outer wall 12 of the branch pipe, so that the stability of the reaction pipeline can be ensured, and the shaking of the reaction pipeline is avoided. The reaction layer is a second reaction layer 11, the second reaction layer 11 is fixed in the branch pipe, the second reaction layer 11 is a fiber product, and the reaction fluid realizes fully mixed reaction in the second reaction layer 11.
When the reaction device is used, reactants enter from the second reaction inlet 14, enter into the second reaction inlet liquid collecting tank 16 and then enter into a plurality of branch pipes respectively, so that the mixing effect of the reactants can be further improved, the reactants are converged in the second reaction outlet liquid collecting tank 17 and then are led out from the second reaction outlet 15 after reacting, and the second heat exchange cavity 10 ensures that the reaction pipeline is at constant temperature in the reaction process.
Third embodiment,
As shown in fig. 4 to 7, this embodiment is an improvement on the basis of the first embodiment in that: the heat exchange shell comprises an upper sealing plate 20, a top heat exchange layer 21 and a bottom heat exchange layer 23, the reaction device comprises a substrate 31 and a third reaction layer 22, a third heat exchange inlet liquid collecting tank 28 and a third heat exchange outlet liquid collecting tank 29 are respectively arranged at two ends of the top heat exchange layer 21 and the bottom heat exchange layer 23, a heat exchange flow field 30 is arranged between the third heat exchange inlet liquid collecting tank 28 and the third heat exchange outlet liquid collecting tank 29, and the heat exchange flow field 30 can be added without any object or with fiber modules, so that the heat exchange effect is improved. The two third heat exchange inlet liquid collecting tanks 28 are opposite in position, the two third heat exchange inlet liquid collecting tanks 28 are communicated through a first connecting channel, the two third heat exchange outlet liquid collecting tanks 29 are opposite in position, and the two third heat exchange outlet liquid collecting tanks 29 are communicated through a second connecting channel. The first connection channel and the second connection channel each penetrate through the substrate 31. The upper sealing plate 20 is fixed on the upper surface of the top heat exchange layer 21, the lower surface of the top heat exchange layer 21 is provided with a reaction groove, and the third reaction layer 22 is positioned in the reaction groove and fixed on the upper surface of the substrate 31. The upper surface of base plate 31 is fixed in the lower surface of top heat transfer layer 21, and the lower surface of base plate 31 is fixed in the upper surface of bottom heat transfer layer 23, and top heat transfer layer 21, base plate 31 and bottom heat transfer layer 23 are the cuboid and the cross section size of three is the same. The reaction inlet is the third reaction inlet 24, and the reaction outlet is the third reaction outlet 25, and the first end of third reaction inlet 24 is located the first side of third reaction layer 22, and the second end of third reaction inlet 24 is located the top heat transfer layer 21, and the first end of third reaction outlet 25 is located the second side of third reaction layer 22, and the second end of third reaction outlet 25 is located the top heat transfer layer 21, so the setting can make the reactant fully contact with third reaction layer 22 to improve the mixed effect of reactant. The heat exchange inlet and the heat exchange outlet are a third heat exchange inlet 26 and a third heat exchange outlet 27 respectively, the first end of the third heat exchange inlet 26 is positioned at a third heat exchange inlet liquid collecting tank 28 of the top heat exchange layer 21, the second end of the third heat exchange inlet 26 is positioned above the top heat exchange layer 21, the first end of the third heat exchange outlet 27 is positioned in a third heat exchange outlet liquid collecting tank 29 on the bottom heat exchange layer 23, the second end of the third heat exchange outlet 27 is positioned at the outer side of the bottom heat exchange layer 23, and the number of the third heat exchange inlets 26 and the third heat exchange outlets 27 can be set according to actual needs by a person skilled in the art.
In use, reactants enter from the third reaction inlet 24, pass through the third reaction layer 22 and exit from the third reaction outlet 25. During this process, the heat exchange medium flows in from the third heat exchange inlet 26 into the third heat exchange inlet sump 28 of the top heat exchange layer 21. A part of the heat exchange medium in the third heat exchange inlet liquid collection tank 28 flows into the third heat exchange outlet liquid collection tank 29 of the top heat exchange layer 21 from the heat exchange flow field 30 of the top heat exchange layer 21, then the third heat exchange outlet liquid collection tank 29 of the top heat exchange layer 21 flows into the third heat exchange outlet liquid collection tank 29 of the bottom heat exchange layer 23 along the second connecting channel, and finally flows out from the third heat exchange outlet 27; and the other part of the heat exchange medium of the third heat exchange inlet liquid collecting tank 28 flows into the third heat exchange inlet liquid collecting tank 28 of the bottom heat exchange layer 23 from the first connecting channel, then flows into the third heat exchange outlet liquid collecting tank 29 of the bottom heat exchange layer 23 through the heat exchange flow field 30 of the bottom heat exchange layer 23, and finally flows out from the third heat exchange outlet 27.
In order to realize the relative fixation of the top heat exchange layer 21, the bottom heat exchange layer 23 and the base plate 31, the embodiment further comprises a plurality of sealing rings, bolts and nuts, wherein a plurality of through holes are formed in the corresponding positions of the top heat exchange layer 21, the base plate 31 and the bottom heat exchange layer 23, and the bolts are connected with the nuts in a threaded manner after penetrating through the through holes. The sealing rings are fixed between the third reaction layer 22 and the inner wall of the reaction groove, between the top heat exchange layer 21 and the base plate 31, and between the bottom heat exchange layer 23 and the base plate 31. This arrangement can effectively prevent leakage of the reaction layer within the third reaction layer 22.
The principles and embodiments of the present invention have been described in this specification with reference to specific examples, the description of which is only for the purpose of aiding in understanding the method of the present invention and its core ideas; also, it is within the scope of the present invention to be modified by those of ordinary skill in the art in light of the present teachings. In view of the foregoing, this description should not be construed as limiting the invention.
Claims (2)
1. A high efficiency reactor, characterized by: the device comprises a reaction device, a heat exchange shell and a heat exchange layer, wherein the heat exchange layer is provided with a heat exchange inlet and a heat exchange outlet, the reaction device is provided with a reaction inlet and a reaction outlet, the reaction inlet and the reaction outlet both penetrate through the heat exchange shell, the reaction device comprises a substrate and a third reaction layer, and the third reaction layer is a fiber module;
The fiber module is formed by stacking silk screens woven by fibers; or the fiber module is formed by winding or folding fiber felts sintered by fibers;
The heat exchange shell comprises an upper sealing plate, the heat exchange layer comprises a top heat exchange layer and a bottom heat exchange layer, a third heat exchange inlet liquid collecting groove and a third heat exchange outlet liquid collecting groove are respectively arranged at two ends of the top heat exchange layer and the bottom heat exchange layer, a heat exchange flow field is arranged between the third heat exchange inlet liquid collecting groove and the third heat exchange outlet liquid collecting groove, the positions of the two third heat exchange inlet liquid collecting grooves are opposite, the two third heat exchange inlet liquid collecting grooves are communicated through a first connecting channel, the positions of the two third heat exchange outlet liquid collecting grooves are opposite, the two third heat exchange outlet liquid collecting grooves are communicated through a second connecting channel, the lower surfaces of the top heat exchange layer are provided with reaction grooves, the upper sealing plate is fixed on the upper surface of the top heat exchange layer, the third reaction layer is fixed on the upper surface of the substrate, the lower surface of the substrate is fixed on the lower surface of the bottom heat exchange layer, the lower surface of the substrate is fixed on the upper surface of the bottom heat exchange layer, the third reaction inlet is positioned on the upper side of the third reaction layer, the third reaction inlet is positioned on the third reaction inlet and the third reaction outlet is positioned on the top heat exchange layer, the third reaction inlet is positioned on the upper side of the third reaction inlet and the third reaction outlet is positioned on the top heat exchange layer, the third reaction inlet is positioned on the top side of the third reaction inlet and the third heat exchange layer, the second end of the third heat exchange inlet is positioned above the top heat exchange layer, the first end of the third heat exchange outlet is positioned in the third heat exchange outlet liquid collecting tank on the bottom heat exchange layer, and the second end of the third heat exchange outlet is positioned outside the bottom heat exchange layer; the device comprises a first reaction groove, a second reaction groove, a third reaction layer, a bottom heat exchange layer, a substrate, a plurality of sealing rings, bolts and nuts, wherein the sealing rings are respectively fixed between the third reaction layer and the inner wall of the reaction groove, between the top heat exchange layer and the substrate, and between the bottom heat exchange layer and the substrate;
the fiber in the fiber module is one or more of basalt fiber, ceramic fiber, glass fiber, metal fiber or asbestos fiber, the diameter of the basalt fiber is 0.1-200 mu m, the diameter of the ceramic fiber is 0.01-50 mu m, the diameter of the glass fiber is 0.01-5 mm, and the diameter of the metal fiber is 1-500 mu m.
2. The high efficiency reactor of claim 1, wherein: the fiber module is subjected to one or more of spray pyrolysis, dipping, non-plasma deposition, anodic oxidation, atomic layer deposition, chemical plating, chemical vapor deposition, galvanic deposition, acid-base treatment, oxidation treatment, low-temperature plasma treatment, coupling agent treatment or adhesive treatment.
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