CN110860263A - High-efficiency reactor - Google Patents
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- CN110860263A CN110860263A CN201911382119.9A CN201911382119A CN110860263A CN 110860263 A CN110860263 A CN 110860263A CN 201911382119 A CN201911382119 A CN 201911382119A CN 110860263 A CN110860263 A CN 110860263A
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00819—Materials of construction
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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
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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
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 both penetrate through the heat exchange shell, the reaction device is also internally provided with a reaction layer, and the reaction layer is a fiber module. The invention has the characteristics of simple structure, mass production, good mass transfer efficiency and heat exchange effect, and the fiber module is used as a reaction layer to improve the mixing effect of reactants.
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 daily production activities and lives of people, and medicines, high molecular polymers, petroleum and the like are all products of the chemical industry. In traditional chemical production equipment, a kettle type reactor and a large-diameter tubular reactor can meet the requirement of large-scale production, but with the improvement of energy-saving and environment-friendly requirements of production enterprises, the defects of high energy consumption, poor safety, serious environmental pollution and the like in the production process are gradually shown. In addition, the traditional chemical equipment mixes 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 accompanying chemical reaction, thus resulting in low reaction efficiency and poor safety. Therefore, when the reaction is amplified from laboratory scale to industrial production by using the traditional large-volume reaction equipment, data deviation occurs, 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, microchannel reactors have been receiving much attention in recent years. The microchannel reactor is a continuous reactor with small size and super large specific surface area, the characteristic channel size is usually micron-sized (50-1000 μm), reactants can react under micron-sized, and the uniformity and the ideality of fluid flow are ensured. Compared with the traditional large-scale kettle type or tubular equipment, the heat transfer and mass transfer performance of the reactor is obviously enhanced, so that the conversion rate, selectivity and operation safety of the reaction can be obviously improved by the microchannel reactor. The microchannel reactor can perform homogeneous catalytic reaction, and can load a catalyst on the tube 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 a plurality of reactors according to the actual reaction requirement. The increasing effect can save a pilot test 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 production, study and research. In addition, because the reaction units of the microchannel reactor are mutually independent, the microchannel reactor has simple structure and easy control of operation conditions, and is convenient to split, check and clean in the application process.
However, the existing microchannel reactor has low utilization rate of internal space, 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 present various disadvantages, such as the chemical etching method can generate acid-base waste liquid which pollutes the environment; the laser etching production efficiency is low, and the micro-fluidic chip is limited to be processed in a small size; the ion etching is limited to silicon-based materials and polymers, and the processing quality is also influenced by the depth-to-width ratio; the die pressing method needs to manufacture a high-cost precise micro-channel grinding tool; the special micro machining technology such as micro electric discharge machining is complex in process and long in period; micro-injection molding is prone to forming small cracks and the like.
Therefore, there is a high demand for a new reactor in the market to solve 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 purpose, the invention provides the following scheme:
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, 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 both penetrate through the heat exchange shell, and the reaction device is internally provided with a reaction layer.
Preferably, the fiber module is sintered or compression molded.
Preferably, the fiber module is formed by stacking fiber woven wire nets.
Preferably, the fiber module is formed by winding or folding a fiber sintered fiber felt.
Preferably, the fiber module comprises one or more of basalt fibers, ceramic fibers, glass fibers, metal fibers or asbestos fibers, the basalt fibers having a diameter of 0.1 μm to 200 μm, the ceramic fibers having a diameter in the range of 0.01 μm to 50 μm, the glass fibers having a diameter of 0.01 μm to 5mm, and the metal fibers having a diameter of 1 μm to 500 μm.
Preferably, the fiber module is subjected to one or more of spray pyrolysis, impregnation, 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 housing includes a first casing, 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 casing, the first reaction layer is fixed in the reaction chamber, a first heat exchange cavity is provided between the reaction chamber and the first casing, the first heat exchange inlet and the first end of the first heat exchange outlet are both communicated with the first heat exchange cavity, the second ends of the first heat exchange inlet and the first heat exchange outlet are located outside the first casing, the first ends of the first reaction inlet and the first reaction outlet are both communicated with an inner cavity of the reaction chamber, the second ends of the first reaction inlet and the first reaction outlet are located outside the first casing, the first reaction layer, the first shell and the reaction chamber are cylinders, the first heat exchange inlet and the first heat exchange outlet are located on the side wall of the first shell, the first heat exchange inlet and the first heat exchange outlet are diagonally arranged, the first reaction inlet is located on an end plane of the first shell, and the first reaction outlet is located on the side wall of the first shell.
Preferably, still include a plurality of bracing pieces, reaction unit is the reaction pipeline, the reaction pipeline has set gradually second reaction entry, second reaction entry collecting tank, a plurality of branch pipes, second reaction export collecting tank and second reaction export, the heat transfer casing includes the second shell, the second reaction entry with the second reaction export passes respectively the corresponding both ends of second shell, the first end of bracing piece is fixed in on the inner wall of second shell, the second end of bracing piece is fixed in on the outer wall of branch pipe, the reaction layer is the second reaction layer, the second reaction layer is fixed in the branch pipe.
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, a third heat exchange inlet liquid collecting tank and a third heat exchange outlet heat collecting tank 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 tank and the third heat exchange outlet heat collecting tank, the two third heat exchange inlet liquid collecting tanks are opposite, 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, 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, and 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 liquid collecting tank of the third heat exchange inlet 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 reaction 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 substrate and between the bottom heat exchange layer and the substrate, a plurality of through holes are formed in the positions, corresponding to the top heat exchange layer, the substrate and the bottom heat exchange layer, of the top 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 using the precise processing technologies such as chemical etching, laser etching, injection molding, linear cutting, electric spark processing and the like to manufacture the micro-channel when preparing the reactor, and has low processing and manufacturing cost; the fiber and the fiber are stacked and staggered to form a three-dimensional pore microchannel, so that an ultrahigh mixing effect can be realized in a short time, and the mass transfer and heat transfer performances are good. The fiber product has wide material selection range, can select proper fiber materials according to specific reaction requirements, and has good universality. 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 a subsequent catalyst. The reaction efficiency is high, and the selectivity is high, simple structure, and the operation is convenient, accurate control, and the security is high, can mass production.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings 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 it is obvious for those skilled in the art to obtain other drawings without creative efforts.
FIG. 1 is a schematic view of a high efficiency reactor according to an embodiment;
FIG. 2 is a sectional view of a high efficiency reactor according to an embodiment;
FIG. 3 is a schematic structural diagram according to a second embodiment;
FIG. 4 is a schematic view of a third structure of the embodiment;
FIG. 5 is a schematic structural view of a top heat exchange layer in the third embodiment;
FIG. 6 is a schematic structural view of a bottom heat transfer layer in the third embodiment;
FIG. 7 is a schematic view of a third substrate and a third reaction layer according to an embodiment;
FIG. 8 is a schematic view of a fiber module construction;
in the figure: 1-a first housing; 2-a first heat exchange chamber; 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 bar; 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 technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present 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 make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in further detail below.
The first embodiment,
As shown in fig. 1-2, the present embodiment provides a high efficiency reactor comprising a reaction apparatus, a heat exchange shell and a heat exchange layer. The reaction device is fixed in the heat exchange shell and used for carrying out chemical reaction, and the heat exchange shell ensures the required temperature in the reaction process. The heat exchange layer is arranged between the reaction device and the heat exchange shell and provided with a heat exchange inlet and a heat exchange outlet, a heat exchange medium flows in from the heat exchange inlet and 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. Aiming at the reaction needing heating, the heat exchange medium flowing through the reaction can be constant-temperature hot water, hot oil and the like; for the reaction needing heat dissipation, the medium flowing through the reaction needing heat dissipation 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 both 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 varies according to the reaction apparatus, and the fiber module is sintered or compression molded in this embodiment. Thus, the reaction layer can be directly sintered or molded by pressing according to the shape of the inner cavity of the reaction device, and then the reaction layer is filled into the reaction device.
Similarly, the fiber module in this embodiment is formed by stacking silk screens woven by fibers. Then the mixture is loaded into a reaction device with different shapes.
Similarly, the fiber module in this embodiment is formed by winding or folding a fiber felt sintered by fibers. The fibers are now sintered into a fiber mat which is then formed into a specific three-dimensional structure by wrapping, folding or otherwise forming (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 staggering fibers, and extend irregularly from 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 in 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 zigzag heat exchange layer built by the fibers is beneficial to fluid mixing, and the mass transfer and heat transfer performances are more excellent.
The specific material of the fiber module comprises inorganic fiber and organic fiber. 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 this embodiment may be a modified material of the above materials, or may be any combination of the above materials. The fibrous material may be selected as appropriate for the particular application.
The material suitable for the fiber module microstructure can be basalt fiber belonging to aluminosilicate systems. Can be basalt fiber or continuous basalt fiber composite material. Can be chopped basalt fiber or continuous basalt fiber. The diameter range of the basalt fiber is 0.1-200 mu m, and the density range is 0.01g/cm3-5g/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 fiber module microstructure can be ceramic fiber, including aluminum silicate, silicon carbide, boron nitride, zirconium oxide, aluminum oxide and other ceramic fibers. The fiber may be in the form of filament or staple fiber. The ceramic fibers have a diameter in the range of 0.01 μm to 50 μm. The porous ceramic fiber module microstructure has the advantages of large specific surface area, easy coating of a catalyst, high strength, high thermal stability, light weight and the like. The concrete example is a ceramic fiber whose main components are 0.67% of ferric oxide, 0.3% of silicon oxide and the balance of aluminum oxide.
The material suitable for the fiber module microstructure can be glass fiber, and the chemical composition of the glass fiber is mainly silicon dioxide and boron trioxide. Comprises alkali-free glass fiber, medium-alkali glass fiber, high-alkali glass fiber, alkali-resistant glass fiber, acid-resistant glass fiber, high-temperature-resistant glass fiber, high-strength glass fiber and high-modulus glass fiber. May be continuous long fibers or discontinuous short fibers. The diameter of the glass fiber is in the range of 0.01 μm to 5 mm. 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 fiber module microstructure can 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, phenylene sulfide fibers, polytetrafluoroethylene fibers, polyvinylidene fluoride fibers. Any combination of the above fibers is also possible. The polymer fiber has the excellent performances of ultrahigh strength, high modulus, high temperature resistance, acid resistance, alkali resistance, light weight and the like,
suitable materials for the fiber module microstructure may be metal fibers including, but not limited to, stainless steel, nickel, copper, titanium, aluminum, hastelloy, Inconel, Fecralloy, and titanium alloys. The diameter of the metal fiber ranges from 1 μm to 500 μm. The fiber can be bundle drawn fiber or cut fiber. The fiber prepared by the cutting method has rough surface structure and large specific surface area, and is beneficial to the adhesion of a catalyst carrier and a catalyst. The metal fiber has high heat conductivity coefficient and good mechanical property, and a proper metal fiber material can be selected 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 properties 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. Technical means for growing the coating include, but are not limited to, spray pyrolysis, dipping, non-plasma deposition, anodization, atomic layer deposition, electroless plating, chemical vapor deposition, galvanic deposition, and the like. Surface treatment methods include, but are 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 in an integrated mode, and the reaction chamber and the first shell 1 cannot be communicated with each other. The first reaction layer 4 is fixed in the reaction chamber, and the first reaction layer 4 allows the reactants to be mixed well. A first heat exchange cavity 2 is arranged between the reaction chamber and the first shell 1, the first ends of the first heat exchange inlet 7 and the 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 located outside the first casing 1, thereby facilitating the introduction and the discharge of the heat exchange medium. 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 at the outer side of the first shell 1, so that the introduction and the derivation of reactants are facilitated.
In use, reactants enter the first reaction inlet 5. Simultaneously as required, leading-in from first heat transfer entry 7 with suitable heat transfer medium, heat transfer medium and the shells inner wall 3 of reaction chamber fully contact to carry out the heat exchange after, derive from first heat transfer export 8 again, thereby guarantee the constancy of temperature in the reaction chamber. The reactants are sufficiently mixed after passing through the first reaction layer 4, thereby improving the reaction efficiency. And the product after the reaction flows out from the first reaction outlet 6 and is collected.
Further, in this embodiment, the first reaction layer 4, the first housing 1 and the reaction chamber are all cylinders. First heat transfer entry 7 and first heat transfer export 8 all are located the lateral wall of first shell 1, and first heat transfer entry 7 and first heat transfer export 8 are the diagonal angle setting, and the setting can make heat transfer medium abundant carry out the heat transfer effect in first heat transfer chamber 2 after again derived like this. 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 is far away from the first reaction inlet 5, so that reactants can be fully reacted and then led out, and incomplete reaction is avoided.
Example II,
As shown in fig. 3, this embodiment is an improvement on the first embodiment, and the improvement is that: still include a plurality of bracing pieces 13, reaction unit is the reaction pipeline, and the reaction pipeline has set gradually second reaction entry 14, second reaction entry collecting tank 16, a plurality of branch pipes, second reaction export collecting tank 17 and second reaction export 15, and the design of reaction pipeline formula as an organic whole. The heat exchange shell comprises a second shell 9, the second shell 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 shell 9. A second heat exchange chamber 10 is formed between the second shell 9 and the reaction pipeline, and the second heat exchange chamber 10 is provided with a second heat exchange inlet 19 and a second heat exchange outlet 18. On the first end of bracing piece 13 was fixed in the inner wall of second shell 9, the second end of bracing piece 13 was fixed in branch pipe outer wall 12, set up the stability that can ensure the reaction pipeline like this, avoided taking place to rock at the reaction pipeline. 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 is fully mixed and reacted in the second reaction layer 11.
During the use, the reactant gets into from second reaction entry 14, enters into second reaction entry collecting tank 16, then gets into a plurality of branch pipes respectively, and the mixed effect of improvement reactant that like this can be further, after the reactant reaction converge at second reaction export collecting tank 17 and derive from second reaction export 15 again can, and second heat exchange chamber 10 ensures the reaction pipeline constant temperature.
Example III,
As shown in fig. 4-7, this embodiment is an improvement on the first embodiment, and the improvement is 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 base plate 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 with no object or a plurality of fiber modules, so that the heat exchange effect is improved. The two third heat exchange inlet sumps 28 are opposite in position, the two third heat exchange inlet sumps 28 are communicated through a first connecting channel, the two third heat exchange outlet sumps 29 are opposite in position, and the two third heat exchange outlet sumps 29 are communicated through a second connecting channel. The first connection channel and the second connection channel both penetrate 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 located in the reaction groove and fixed on the upper surface of the substrate 31. The upper surface of the substrate 31 is fixed to the lower surface of the top heat exchange layer 21, the lower surface of the substrate 31 is fixed to the upper surface of the bottom heat exchange layer 23, and the top heat exchange layer 21, the substrate 31 and the bottom heat exchange layer 23 are all rectangular solids and have the same cross section size. The reaction inlet is a third reaction inlet 24, the reaction outlet is a third reaction outlet 25, the first end of the third reaction inlet 24 is located at the first side of the third reaction layer 22, the second end of the third reaction inlet 24 is located above the top heat exchange layer 21, the first end of the third reaction outlet 25 is located at the second side of the third reaction layer 22, and the second end of the third reaction outlet 25 is located above the top heat exchange layer 21, so that the reactant can be fully contacted with the third reaction layer 22, and the mixing effect of the reactant is improved. The heat exchange inlets and the heat exchange outlets are respectively a third heat exchange inlet 26 and a third heat exchange outlet 27, a first end of the third heat exchange inlet 26 is located at a third heat exchange inlet header tank 28 of the top heat exchange layer 21, a second end of the third heat exchange inlet 26 is located above the top heat exchange layer 21, a first end of the third heat exchange outlet 27 is located in a third heat exchange outlet header tank 29 on the bottom heat exchange layer 23, and a second end of the third heat exchange outlet 27 is located outside the bottom heat exchange layer 23, and those skilled in the art can set the number of the third heat exchange inlets 26 and the third heat exchange outlets 27 according to actual needs.
In use, reactants enter through the third reaction inlet 24, pass through the third reaction layer 22, and exit through 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 header tank 28 flows from the heat exchange flow field 30 of the top heat exchange layer 21 to the third heat exchange outlet header tank 29 of the top heat exchange layer 21, then the third heat exchange outlet header tank 29 of the top heat exchange layer 21 flows into the third heat exchange outlet header 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 header tank 28 flows into the third heat exchange inlet header tank 28 of the bottom heat exchange layer 23 from the first connecting channel, then flows to the third heat exchange outlet header 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 substrate 31, the heat exchange layer further comprises a plurality of sealing rings, bolts and nuts in the embodiment, a plurality of through holes are arranged at corresponding positions of the top heat exchange layer 21, the substrate 31 and the bottom heat exchange layer 23, and the bolts penetrate through the through holes and are in threaded connection with the nuts. 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 substrate 31, and between the bottom heat exchange layer 23 and the substrate 31. This arrangement can effectively prevent the reaction layer in the third reaction layer 22 from leaking.
The principle and the implementation mode of the present invention are explained by applying specific examples in the present specification, and the above descriptions of the examples are only used to help understanding the method and the core idea of the present invention; meanwhile, for a person skilled in the art, according to the idea of the present invention, the specific embodiments and the application range may be changed. In view of the above, the present disclosure should not be construed as limiting the invention.
Claims (10)
1. A high efficiency reactor, characterized by: the device 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 both penetrate through the heat exchange shell, a reaction layer is arranged in the reaction device, and the reaction layer is a fiber module.
2. The high efficiency reactor of claim 1, wherein: and the fiber module is formed by sintering or compression molding.
3. The high efficiency reactor of claim 1, wherein: the fiber module is formed by stacking silk screens woven by fibers.
4. The high efficiency reactor of claim 1, wherein: the fiber module is formed by winding or folding fiber felts sintered by fibers.
5. The high efficiency reactor of claim 1, wherein: the fiber module comprises one or more of basalt fibers, ceramic fibers, glass fibers, metal fibers or asbestos fibers, the diameter of the basalt fibers is 0.1-200 mu m, the diameter of the ceramic fibers ranges from 0.01-50 mu m, the diameter of the glass fibers is 0.01-5 mm, and the diameter of the metal fibers is 1-500 mu m.
6. 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, electroless plating, chemical vapor deposition, galvanic deposition, acid-base treatment, oxidation treatment, low-temperature plasma treatment, coupling agent treatment, or adhesive treatment.
7. The high efficiency reactor of claim 1, wherein: the heat exchange shell is 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, the first ends of the first heat exchange inlet and the first heat exchange outlet are both communicated with the first heat exchange cavity, the second ends of the first heat exchange inlet and the first heat exchange outlet are positioned outside the first shell, the first ends of the first reaction inlet and the first reaction outlet are both communicated with an inner cavity of the reaction chamber, and the second ends of the first reaction inlet and the first reaction outlet are positioned outside the first shell, the first reaction layer, the first shell and the reaction chamber are cylinders, the first heat exchange inlet and the first heat exchange outlet are located on the side wall of the first shell, the first heat exchange inlet and the first heat exchange outlet are diagonally arranged, the first reaction inlet is located on an end plane of the first shell, and the first reaction outlet is located on the side wall of the first shell.
8. The high efficiency reactor of claim 1, wherein: still include a plurality of bracing pieces, reaction unit is the reaction pipeline, the reaction pipeline has set gradually second reaction entry, second reaction entry collecting tank, a plurality of branch pipes, second reaction export collecting tank and second reaction export, the heat transfer casing is the second shell, the second reaction entry with the second reaction export passes respectively the corresponding both ends of second shell, the first end of bracing piece is fixed in on the inner wall of second shell, the second end of bracing piece is fixed in on the outer wall of branch pipe, the reaction layer is the second reaction layer, the second reaction layer is fixed in the branch pipe.
9. The high efficiency reactor of claim 1, wherein: 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, a third heat exchange inlet liquid collecting tank and a third heat exchange outlet heat collecting tank are respectively arranged at two ends of the top heat exchange layer and the bottom heat exchange layer, a heat exchange flow field is formed 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, 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, the two third heat exchange outlet heat collecting tanks are communicated through a second connecting channel, a reaction groove is formed in the lower surface of the top heat exchange layer, the upper sealing plate is fixed on the upper surface of the top heat exchange layer, and 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 liquid collecting tank of the third heat exchange inlet 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.
10. The high efficiency reactor of claim 9, wherein: the heat exchange structure is characterized by further comprising 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, a plurality of through holes are formed in the positions, corresponding to the top heat exchange layer, the substrate and the bottom heat exchange layer, of the top heat exchange layer, and the bolts penetrate through the through holes and are in threaded connection with the nuts.
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