CN115784152B - Laminated microchannel reforming hydrogen production reactor - Google Patents
Laminated microchannel reforming hydrogen production reactor Download PDFInfo
- Publication number
- CN115784152B CN115784152B CN202211468452.3A CN202211468452A CN115784152B CN 115784152 B CN115784152 B CN 115784152B CN 202211468452 A CN202211468452 A CN 202211468452A CN 115784152 B CN115784152 B CN 115784152B
- Authority
- CN
- China
- Prior art keywords
- plate
- reaction
- outlet
- evaporation
- inlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 80
- 239000001257 hydrogen Substances 0.000 title claims abstract description 80
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 79
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 65
- 238000002407 reforming Methods 0.000 title claims abstract description 37
- 238000006243 chemical reaction Methods 0.000 claims abstract description 183
- 238000001704 evaporation Methods 0.000 claims abstract description 87
- 230000008020 evaporation Effects 0.000 claims abstract description 78
- 238000009792 diffusion process Methods 0.000 claims abstract description 58
- 238000005485 electric heating Methods 0.000 claims abstract description 42
- 238000010438 heat treatment Methods 0.000 claims description 31
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 26
- 229910002804 graphite Inorganic materials 0.000 claims description 23
- 239000010439 graphite Substances 0.000 claims description 23
- 230000000149 penetrating effect Effects 0.000 claims description 6
- 230000007423 decrease Effects 0.000 claims description 3
- 239000012530 fluid Substances 0.000 abstract description 18
- 238000012546 transfer Methods 0.000 abstract description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 66
- 238000009826 distribution Methods 0.000 description 9
- 239000007789 gas Substances 0.000 description 6
- 230000009471 action Effects 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 238000011161 development Methods 0.000 description 3
- 230000010354 integration Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 239000002028 Biomass Substances 0.000 description 2
- 230000003321 amplification Effects 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 229910021389 graphene Inorganic materials 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000003199 nucleic acid amplification method Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000006057 reforming reaction Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical class [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000014509 gene expression Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Abstract
The invention provides a laminated microchannel reforming hydrogen production reactor, which comprises an upper cover plate, a reaction plate, an evaporation plate and a lower cover plate which are sequentially arranged from top to bottom; the lower cover plate inlet is communicated with the evaporation plate inlet, the evaporation plate outlet is communicated with the reaction plate inlet, and the reaction plate outlet is communicated with the upper cover plate outlet; the bottom of the evaporating plate is provided with an electric heating plate, the side wall of the reaction plate is provided with a thermocouple and an electric heating rod, the upper surface of the reaction plate is provided with a parting flow passage, a rear free diffusion chamber, a reaction flow passage, a front free diffusion chamber and an outlet flow passage, and fluid is uniformly diffused to the reaction flow passage at the rear free diffusion chamber and then is collected to the outlet of the reaction plate at the front free diffusion chamber and the outlet flow passage. The laminated microchannel reforming hydrogen production reactor provided by the invention effectively reduces pressure drop, enhances heat and mass transfer characteristics, has excellent hydrogen production performance, further reduces the overall size of the reforming hydrogen production reactor, and optimizes the space volume of the reactor.
Description
Technical Field
The invention relates to the technical field of reforming hydrogen production, in particular to a laminated microchannel reforming hydrogen production reactor.
Background
Today, environmental problems are increasingly serious, and energy conservation and emission reduction become one of important problems facing society. The hydrogen energy has the characteristics of high efficiency, cleanness, green, sustainable development and the like, and is regarded as one of the most potential clean energy sources in the new century. Along with the release of new energy policies in various places, hydrogen energy becomes a hot new energy source and has wide application prospect in the industrial field.
The current hydrogen production mode is mainly divided into traditional fossil energy hydrogen production and novel energy hydrogen production. The traditional fossil energy hydrogen production mainly comprises petroleum hydrogen production, coal hydrogen production and natural gas hydrogen production. Although fossil energy hydrogen production is still the main hydrogen production mode at present, the pollution to the environment is larger and the standard of green hydrogen is not met. The novel energy hydrogen production mainly comprises biomass hydrogen production, electrolytic water hydrogen production, solar hydrogen production and alcohol substance hydrogen production. The biomass hydrogen production can be carried out continuously and stably in a small amount, the hydrogen production cost is increased by water electrolysis, and the solar hydrogen production is greatly influenced by the environment. The hydrogen production of alcohols is mainly the hydrogen production by reforming methanol, and the methanol is cracked into H under certain temperature and pressure conditions 2 With carbon-containing gas such as CO, CO reacts with steam to generate H 2 With CO 2 CO is removed by pressure swing adsorption 2 Finally obtain high-purity H 2 . The methanol reforming hydrogen production process is simple, the raw materials are easy to obtain, the production mode is stable and reliable, and the method is suitable for small and medium-scale hydrogen production.
Because of the special physical and chemical properties of hydrogen, the storage and transportation of hydrogen become a serious problem for limiting the development of hydrogen. Compared with other hydrogen production modes, the methanol reforming hydrogen production is not influenced by external environmental factors, the raw materials are low, the hydrogen production is stable and safe, and the methanol reforming hydrogen production micro-reactor has the advantages of small volume, simple structure and convenient transportation. The methanol is used for on-site hydrogen production through the reforming micro-reactor, so that the hydrogen is timely supplied, the method is more suitable for a mobile on-line hydrogen production scene, and a new solution is provided for hydrogen storage and transportation.
The methanol reforming hydrogen production micro-reactor mainly comprises a cylindrical micro-reactor and a plate type micro-reactor. The cylindrical microreactor is simple to process and assemble, but the cylindrical structural design has high pressure drop, uneven temperature distribution and difficult integration and amplification; the plate-type microreactor is in a laminated assembly mode, each layer of the microreactor is relatively independent, the assembly is simple, the plate-type microreactor has a higher heat exchange area, the temperature distribution is uniform, and the integration and the amplification are easier. An excellent reforming hydrogen production microchannel reactor is important for hydrogen production performance.
The microchannel reactor with the flow rate and the concentration being uniformly distributed, which is proposed by the patent document of the publication No. CN111196596A, can lead the flow rate and the concentration of the fluid to be more uniform, but the parting flow passage at the front end of the reaction plate is too complicated, the space sacrifice of the reaction plate is larger, the utilization rate is lower, and the space volume of the reactor is enlarged; the hydrogen production micro-reformer with the fractal structure catalyst carrier proposed in the patent document of publication No. CN110155946B can realize good hydrogen production performance, but the structure of a reaction carrier plate is complex, and the manufacturing cost is increased.
The existing micro-channel reforming hydrogen production reactor only has partial excellent performances, and has the advantages of uniform flow velocity distribution, lower pressure drop, high hydrogen conversion rate, and no integration of the excellent performances such as the space utilization rate of a reaction plate. Therefore, the development of a microchannel reforming hydrogen production reactor with better performance is a problem in the art.
Disclosure of Invention
In accordance with the above-described technical problems, a stacked microchannel reforming hydrogen production reactor is provided. The novel microchannel reaction flow channel is designed on the reaction plate, and the structural characteristics of the parting flow channel and the A-type flow channel are combined, so that fluid firstly passes through the parting flow channels on two sides from an inlet to reach a diffusion port, and then the fluid is uniformly distributed in a cavity through the free diffusion action of the fluid, thereby reducing pressure drop, improving the uniformity of fluid distribution, enhancing the heat and mass transfer characteristics of the fluid and improving the conversion rate of methanol; the outlet of the reaction flow passage is in a contracted shape, and hydrogen and other gas products after chemical reaction are collected and amplified, so that the later gas treatment is facilitated. The heating mode of the laminated microchannel reforming hydrogen production reactor is that an electric heating rod is combined with a heating plate, the accurate temperature control of a reaction plate adopts the heating mode of the electric heating rod, the inaccurate temperature control of an evaporation plate adopts the heating mode of the electric heating plate, the height of the evaporation plate is greatly reduced, the overall size of the reforming hydrogen production reactor is further reduced, and the space volume of the reactor is optimized.
The invention adopts the following technical means:
a laminated microchannel reforming hydrogen production reactor comprises an upper cover plate, a reaction plate group, an evaporation plate and a lower cover plate which are sequentially arranged from top to bottom; the reaction plate group comprises one or more stacked reaction plates;
an upper cover plate outlet vertically penetrating through the upper cover plate is formed in the front end of the upper cover plate;
the upper surface of the reaction plate is provided with a reaction flow channel, and the front end and the rear end of the reaction flow channel are respectively provided with a reaction plate outlet and a reaction plate inlet which vertically penetrate through the reaction plate; the two sides of the inlet of the reaction plate are respectively provided with a parting runner communicated with the reaction plate, an outlet of the parting runner is communicated with the rear end inlet of the rear free diffusion chamber, and the front end outlet of the rear free diffusion chamber is opposite to the rear end of the reaction runner and is communicated with the rear end inlet of the rear free diffusion chamber; the size of the flow passage of the rear free diffusion chamber is gradually increased from the rear to the front; the two sides and the rear side of the reaction plate outlet are respectively provided with an outlet runner communicated with the reaction plate outlet, the inlet of the outlet runner is communicated with the front end outlet of the front free diffusion chamber, and the rear end inlet of the front free diffusion chamber is opposite to the front end of the reaction runner and is communicated with the front end outlet of the front free diffusion chamber; the size of the flow channel of the front free diffusion chamber gradually decreases from the back to the front; the side wall of the reaction plate is provided with at least one heating device mounting hole, and a first heating device is arranged in the heating device mounting hole;
the front end and the rear end of the evaporation plate are respectively provided with an evaporation plate inlet and an evaporation plate outlet which vertically penetrate through the evaporation plate, and the upper surface of the evaporation plate is provided with an evaporation chamber of which the two ends are respectively communicated with the evaporation plate inlet and the evaporation plate outlet; an electric heating groove is formed in the lower surface of the evaporation plate, and a second heating device is arranged in the electric heating groove;
the front end of the lower cover plate is provided with a lower cover plate inlet vertically penetrating through the lower cover plate, and the lower cover plate inlet is communicated with the evaporation plate inlet;
when one reaction plate is adopted, the inlet of the reaction plate is communicated with the outlet of the evaporation plate, and the outlet of the reaction plate is communicated with the outlet of the upper cover plate;
when a plurality of reaction plates are adopted, the inlets of the reaction plates are communicated with the outlets of the evaporation plates, and the outlets of the reaction plates are communicated with the outlets of the upper cover plate.
Preferably, graphite gaskets are respectively arranged between the upper cover plate and the reaction plate, between the reaction plate and the evaporation plate and between the evaporation plate and the lower cover plate, and the graphite gaskets between the upper cover plate and the reaction plate are provided with through holes for communicating the outlet of the reaction plate with the outlet of the upper cover plate; the graphite gasket between the reaction plate and the evaporation plate is provided with a through hole which is communicated with the inlet of the reaction plate and the outlet of the evaporation plate; the graphene gasket between the evaporation plate and the lower cover plate is provided with a through hole communicated with the evaporation plate inlet and the lower cover plate inlet;
when a plurality of reaction plates are adopted, graphite gaskets are also arranged between two adjacent reaction plates, and the graphite gaskets between the two adjacent reaction plates are provided with through holes for communicating the inlets of the two adjacent reaction plates and through holes for communicating the outlets of the two adjacent reaction plates.
Preferably, the length of the upper cover plate and the lower cover plate is 60-180 mm, the width is 35-95 mm, and the height is 2-20 mm;
the length of the reaction plate is 60-180 mm, the width is 35-95 mm, and the height is 5-30 mm;
the length of the evaporation plate is 60-180 mm, the width is 35-95 mm, and the height is 2-20 mm;
the length of the graphite gasket is 60-180 mm, the width is 35-95 mm, and the height is 0.2-2 mm.
Preferably, the first heating device is a thermocouple and a heating rod, the heating device mounting holes are thermocouple holes matched with the thermocouple and electric heating holes matched with the heating rod, the number of the electric heating holes is 2-6, the number of the thermocouple holes is 2-6, the diameters of the electric heating holes are 2-12 mm, and the center distance between two adjacent electric heating holes is 10-50 mm; the diameter of the thermocouple hole is 1-5 mm, and the center distance between two adjacent thermocouple holes is 10-50 mm.
Preferably, the second heating device is an electric heating plate.
Preferably, the diameter phi of the inlet and the outlet of the reaction plate is 0.2-5 mm; the rear free diffusion chamber is conical, the vertex angle theta 1 of the rear free diffusion chamber is 30-160 degrees, the included angle theta 2 between the diffusion edge of the rear free diffusion chamber and the edge of the reaction plate is 90-150 degrees, and the included angle theta 3 between the diffusion edges of two adjacent front free diffusion chambers is 30-160 degrees; the height of the reaction runner is 0.2-5 mm; the number of the reaction channels is 6-26, the length L of the channels is 40-160 mm, the width W1 of the channels is 0.2-5 mm, and the ridge width W2 between the channels is 0.2-5 mm.
Preferably, the reaction flow channel is a straight flow channel, a wavy flow channel, a zigzag flow channel or a concave flow channel; the concave flow channel is linear, the flow channel walls on two sides of the concave flow channel are respectively provided with a row of bulges uniformly distributed along the extending direction of the concave flow channel, and the bulges are arranged in two rows in a staggered way.
Compared with the prior art, the invention has the following advantages:
1. the laminated microchannel reforming hydrogen production reactor provided by the invention effectively reduces pressure drop, enhances heat and mass transfer characteristics, and has excellent hydrogen production performance.
2. The invention provides a novel stacked microchannel reforming hydrogen production reactor, which combines the heating modes of an electric heating rod and an electric heating plate, adopts the heating mode of the electric heating rod for precisely controlling the temperature of a reaction plate, adopts the heating mode of the electric heating plate for inaccurately controlling the temperature of an evaporation plate, greatly reduces the height of the evaporation plate, further reduces the overall size of the reforming hydrogen production reactor, and optimizes the space volume of the reactor.
3. The novel stacked microchannel reforming hydrogen production reactor provided by the invention has the advantages that the novel microchannel reaction flow channels utilize the two parting flow channels, so that the fluid can be fully diffused in the flow field, the uniformity of the fluid distribution is enhanced, and the fluid flow velocity distribution is more uniform.
4. According to the laminated novel microchannel reforming hydrogen production reactor provided by the invention, the parallel flow channel part of the middle part of the novel microchannel reaction flow channel is lengthened, so that the flow field flow is longer, the specific surface area is increased, and the methanol vapor fully performs chemical reaction, thereby improving the methanol conversion rate.
5. The tail end of the novel laminated microchannel reaction flow channel of the novel microchannel reforming hydrogen production reactor provided by the invention is in a contracted shape, so that the hydrogen produced after chemical reaction can be conveniently collected and amplified, and the post treatment of the gas is convenient.
6. Compared with the traditional flow channel, the novel laminated microchannel reforming hydrogen production reactor provided by the invention has higher space utilization rate, simple structure, easiness in processing, low manufacturing cost and good economical efficiency.
In conclusion, the technical scheme of the invention can increase the heat and mass transfer characteristics of the fluid, improve the conversion rate of methanol, and finally realize the preparation of high-purity hydrogen and realize the online hydrogen production.
Based on the reasons, the invention can be widely popularized in the fields of reforming hydrogen production and the like.
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 required in the embodiments or the description of the prior art will be briefly described, and it is obvious that the drawings in the following description are 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 stacked microchannel reforming hydrogen production reactor in accordance with an embodiment of the present invention.
Fig. 2 is a schematic structural view of an upper cover plate in an embodiment of the present invention.
FIG. 3 is a schematic view of the structure of a reaction plate according to an embodiment of the present invention.
FIG. 4 is a top view of a reaction plate in an embodiment of the invention.
Fig. 5 is a schematic top view three-dimensional view of an evaporating plate in an embodiment of the present invention.
Fig. 6 is a three-dimensional schematic view of a bottom view of an evaporating plate in accordance with an embodiment of the present invention.
FIG. 7 is a schematic view of a reaction channel in an embodiment of the invention.
FIG. 8 is a flow chart of the reaction fluid in an embodiment of the invention.
FIG. 9 is a flow chart of the reaction fluid in the reaction plate in an embodiment of the present invention.
In the figure: 1. an upper cover plate; 2. a reaction plate; 3. an evaporation plate; 4. a lower cover plate; 5. a graphite gasket; 6. a lower cover plate inlet; 7. an evaporation plate inlet; 8. an evaporation plate outlet; 9. an inlet of the reaction plate; 10. an outlet of the reaction plate; 11. an upper cover plate outlet; 12. an evaporation chamber; 13. a reaction flow channel; 14. an electric heating hole; 15. a thermocouple hole; 16. an electric heating tank; 17. parting flow channels; 18. a rear free diffusion chamber; 19. an outlet flow passage; 20. a front free diffusion chamber.
Detailed Description
It should be noted that, without conflict, the embodiments of the present invention and features of the embodiments may be combined with each other. The invention will be described in detail below with reference to the drawings in connection with embodiments.
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. The following description of at least one exemplary embodiment is merely exemplary in nature and is in no way intended to limit the invention, its application, or uses. 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.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the present invention. As used herein, the singular is also intended to include the plural unless the context clearly indicates otherwise, and furthermore, it is to be understood that the terms "comprises" and/or "comprising" when used in this specification are taken to specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof.
The relative arrangement of the components and steps, numerical expressions and numerical values set forth in these embodiments do not limit the scope of the present invention unless it is specifically stated otherwise. Meanwhile, it should be clear that the dimensions of the respective parts shown in the drawings are not drawn in actual scale for convenience of description. Techniques, methods, and apparatus known to one of ordinary skill in the relevant art may not be discussed in detail, but are intended to be part of the specification where appropriate. In all examples shown and discussed herein, any specific values should be construed as merely illustrative, and not a limitation. Thus, other examples of the exemplary embodiments may have different values. It should be noted that: like reference numerals and letters denote like items in the following figures, and thus once an item is defined in one figure, no further discussion thereof is necessary in subsequent figures.
In the description of the present invention, it should be understood that the azimuth or positional relationships indicated by the azimuth terms such as "front, rear, upper, lower, left, right", "lateral, vertical, horizontal", and "top, bottom", etc., are generally based on the azimuth or positional relationships shown in the drawings, merely to facilitate description of the present invention and simplify the description, and these azimuth terms do not indicate and imply that the apparatus or elements referred to must have a specific azimuth or be constructed and operated in a specific azimuth, and thus should not be construed as limiting the scope of protection of the present invention: the orientation word "inner and outer" refers to inner and outer relative to the contour of the respective component itself.
Spatially relative terms, such as "above … …," "above … …," "upper surface at … …," "above," and the like, may be used herein for ease of description to describe one device or feature's spatial location relative to another device or feature as illustrated in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations in use or operation in addition to the orientation depicted in the figures. For example, if the device in the figures is turned over, elements described as "above" or "over" other devices or structures would then be oriented "below" or "beneath" the other devices or structures. Thus, the exemplary term "above … …" may include both orientations of "above … …" and "below … …". The device may also be positioned in other different ways (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein interpreted accordingly.
In addition, the terms "first", "second", etc. are used to define the components, and are only for convenience of distinguishing the corresponding components, and the terms have no special meaning unless otherwise stated, and therefore should not be construed as limiting the scope of the present invention.
As shown in fig. 1 to 8, a stacked microchannel reforming hydrogen production reactor comprises an upper cover plate 1, a reaction plate group, an evaporation plate 3 and a lower cover plate 4 which are sequentially arranged from top to bottom; the reaction plate group comprises one or more stacked reaction plates 2; graphite gaskets 5 are respectively arranged between the upper cover plate 1 and the reaction plate 2, between the reaction plate 2 and the evaporation plate 3, and between the evaporation plate 3 and the lower cover plate 4, and when a plurality of reaction plates 2 are adopted, the graphite gaskets 5 are also arranged between two adjacent reaction plates 2; the upper cover plate 1, the reaction plate 2, the evaporation plate 3, the lower cover plate 4 and the graphite gasket 5 are equal in width and length, the length is 60-180 mm, the width is 35-95 mm, 8-16 bolt holes are machined in the periphery, the diameters of the bolt holes are 0.2-1.8 mm, and the bolts penetrate through the bolt holes to fix the components into a whole.
As shown in fig. 2, the front end of the upper cover plate 1 is provided with an upper cover plate outlet 11 vertically penetrating the upper cover plate 1; the length of the upper cover plate 1 is 60-180 mm, the width is 35-95 mm, and the height is 2-20 mm;
as shown in FIG. 3, the length of the reaction plate 2 is 60-180 mm, the width is 35-95 mm, and the height is 5-30 mm; the upper surface of the reaction plate 2 is provided with a reaction flow channel 13, and the front end and the rear end of the reaction flow channel 13 are respectively provided with a reaction plate outlet 10 and a reaction plate inlet 9 which vertically penetrate through the reaction plate 2; the two sides of the inlet 9 of the reaction plate are respectively provided with a parting runner 17 communicated with the reaction plate, the outlet of the parting runner 17 is communicated with the inlet at the rear end of the rear free diffusion chamber 18, and the outlet at the front end of the rear free diffusion chamber 18 is opposite to the rear end of the reaction runner 13 and is communicated with the rear end of the reaction runner; the size of the flow passage of the rear free diffusion chamber 18 gradually increases from the rear to the front; the two sides and the rear side of the reaction plate outlet 10 are respectively provided with an outlet runner 19 communicated with the reaction plate outlet, the inlet of the outlet runner 19 is communicated with the front end outlet of the front free diffusion chamber 20, and the rear end inlet of the front free diffusion chamber 20 is opposite to the front end of the reaction runner 13 and is communicated with the front end of the reaction runner 13; the flow channel of the front free diffusion chamber 20 gradually decreases from the back to the front; the side wall of the reaction plate 2 is provided with at least one heating device mounting hole, and a first heating device is arranged in the heating device mounting hole; the first heating device is a thermocouple (not shown) and an electric heating rod (not shown), the mounting holes of the heating device are a thermocouple hole 15 matched with the thermocouple and an electric heating hole 14 matched with the electric heating rod, the number of the electric heating holes is 2-6 (4 in the specific embodiment), the number of the thermocouple holes is 2-6 (4 in the specific embodiment), the diameter of the electric heating hole 14 is 2-12 mm, and the center-to-center distance between two adjacent electric heating holes 14 is 10-50 mm; the diameter of the thermocouple holes 15 is 1-5 mm, and the circle center distance between every two adjacent thermocouple holes 15 is 10-50 mm.
As shown in fig. 4, the diameter Φ of the reaction plate inlet 9 and the reaction plate outlet 10 is 0.2 to 5mm; the rear free diffusion chamber 18 is conical, the vertex angle theta 1 of the rear free diffusion chamber is 30-160 degrees, the included angle theta 2 between the diffusion edge of the rear free diffusion chamber 20 and the edge of the reaction plate 2 is 90-150 degrees, and the included angle theta 3 between the diffusion edges of two adjacent front free diffusion chambers 20 is 30-160 degrees; the height of the reaction runner 13 is 0.2-5 mm; the number of the reaction channels 13 is 6-26, the length L of the channels is 40-160 mm, the width W1 is 0.2-5 mm, and the ridge width W2 between the channels is 0.2-5 mm.
As shown in fig. 5, the length of the evaporating plate 3 is 60-180 mm, the width is 35-95 mm, and the height is 2-20 mm; an evaporation plate inlet 7 and an evaporation plate outlet 8 which vertically penetrate through the evaporation plate are respectively machined at the front end and the rear end of the evaporation plate 3, and an evaporation chamber 12 with two ends respectively communicated with the evaporation plate inlet 7 and the evaporation plate outlet 8 is arranged on the upper surface of the evaporation plate 3; as shown in fig. 6, the lower surface of the evaporating plate 3 is provided with an electric heating tank 16, and a second heating device is installed in the electric heating tank; the second heating device is an electric heating plate (not shown).
The length of the lower cover plate 4 is 60-180 mm, the width is 35-95 mm, and the height is 2-20 mm; a lower cover plate inlet 6 vertically penetrating through the lower cover plate 4 is arranged at the front end of the lower cover plate 4, and the lower cover plate inlet 6 is communicated with the evaporation plate inlet 7;
when one reaction plate 2 is adopted, the inlet 9 of the reaction plate is communicated with the outlet 7 of the evaporation plate, and the outlet 10 of the reaction plate is communicated with the outlet 11 of the upper cover plate; when a plurality of reaction plates 2 are adopted, a plurality of reaction plate inlets 9 are communicated with the evaporation plate outlets 7, and a plurality of reaction plate outlets 10 are communicated with the upper cover plate outlets 11.
The graphite gasket 5 between the upper cover plate 1 and the reaction plate 2 is provided with a through hole which is communicated with the reaction plate outlet 10 and the upper cover plate outlet 11; the graphite gasket 5 between the reaction plate 2 and the evaporation plate 3 has a through hole communicating the reaction plate inlet 9 and the evaporation plate outlet 8; the graphene gasket 5 between the evaporation plate 3 and the lower cover plate 4 is provided with a through hole which is communicated with the evaporation plate inlet 7 and the lower cover plate inlet 6; when a plurality of reaction plates 2 are adopted, the graphite gaskets 5 between two adjacent reaction plates 2 are provided with through holes communicated with two adjacent reaction plate inlets 9 and through holes communicated with two adjacent reaction plate outlets 10. In this embodiment, a single reaction plate 2 (shown in FIG. 1) is used. The length of the graphite gasket 5 is 60-180 mm, the width is 35-95 mm, and the height is 0.2-2 mm.
The reaction flow channel 13 may be a wavy flow channel, a zigzag flow channel or a concave flow channel as shown in fig. 7, besides being a straight flow channel as shown in fig. 3; the concave flow channel is linear, the flow channel walls on two sides of the concave flow channel are respectively provided with a row of bulges uniformly distributed along the extending direction of the concave flow channel, and the bulges are arranged in two rows in a staggered way.
As shown in fig. 8, the aqueous methanol solution enters the reactor from the lower cover plate inlet 6 and flows into the evaporation chamber 12 in the evaporation plate 3 through the evaporation plate inlet 7. An electric heating plate is arranged in an electric heating groove 16 in the lower surface of the evaporating plate 3, the evaporating plate is heated up under the action of the electric heating plate to reach the evaporating temperature of the aqueous methanol solution, and the aqueous methanol solution absorbs heat and evaporates in the evaporating chamber 12 to form methanol vapor. Due to the diffusion effect of the fluid, the methanol vapor reaches the tail end of the evaporation chamber 12, flows out of the evaporation chamber through the evaporation plate outlet 8, reaches the reaction plate inlet 9 and enters the reaction flow channel 13 in the reaction plate 2. The side wall of the reaction plate 2 is provided with an electric heating hole 14 and a thermocouple hole 15, an electric heating rod is arranged in the electric heating hole 14, a thermocouple is arranged in the thermocouple hole 15, and under the action of the electric heating rod and the thermocouple, the temperature of the reaction plate 2 is raised to reach the reforming reaction temperature of methanol vapor. The methanol vapor is distributed along the flow path in the reaction plate 2 and enters the catalytic region, and hydrogen and other products are generated under the action of the catalyst, wherein the specific equation is as follows:
reforming reaction:
and (3) decomposition reaction:
and (3) water vapor reverse reaction:
the hydrogen and other gas products after chemical reaction are diffused to the reaction plate outlet 10 due to the diffusion effect of the fluid, finally reach the upper cover plate outlet 11 and flow out of the reactor.
In the present embodiment, the reaction plate 2 is provided with a split flow path 17, a rear free diffusion chamber 18, a front free diffusion chamber 20, and an outlet flow path 19. At the beginning of the reaction, as shown in fig. 9, methanol vapor enters from the inlet 9 of the reaction plate, and flows to the diffusion port a and the diffusion port B respectively by the free flow and diffusion action of the fluid, and then diffuses to the reaction flow channel 13 for chemical reaction, and at this time, the methanol vapor is reformed to produce hydrogen and carbon oxides. When the fluid reaches the end of the parallel flow channels, the gas products are diffused to the C position, the D position and the E position respectively, finally are collected to the position of the reaction plate outlet 10 through the outlet flow channel 19, and concentrated and discharged out of the reaction plate 2 after being collected and amplified through the front free diffusion chamber 20 and the outlet flow channel 19. The reaction plate 2 has the characteristic of uniform flow distribution of parting flow passages 17, methanol vapor uniformly flows to the rear free diffusion chamber 18 for diffusion through the parting flow passages 17 at the two sides of the inlet 9 of the reaction plate, so that the uniformity of fluid flow distribution is improved, uniform flow velocity distribution is facilitated, and the reaction plate has the characteristics of low pressure drop and high methanol conversion rate of the A-type flow passages.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and not for limiting the same; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the invention.
Claims (7)
1. The laminated microchannel reforming hydrogen production reactor is characterized by comprising an upper cover plate, a reaction plate group, an evaporation plate and a lower cover plate which are sequentially arranged from top to bottom;
an upper cover plate outlet vertically penetrating through the upper cover plate is formed in the front end of the upper cover plate;
the reaction plate group comprises one or more stacked reaction plates;
the upper surface of the reaction plate is provided with a reaction flow channel, and the front end and the rear end of the reaction flow channel are respectively provided with a reaction plate outlet and a reaction plate inlet which vertically penetrate through the reaction plate; the two sides of the inlet of the reaction plate are respectively provided with a parting runner communicated with the reaction plate, an outlet of the parting runner is communicated with the rear end inlet of the rear free diffusion chamber, and the front end outlet of the rear free diffusion chamber is opposite to the rear end of the reaction runner and is communicated with the rear end inlet of the rear free diffusion chamber; the size of the flow passage of the rear free diffusion chamber is gradually increased from the rear to the front; the two sides and the rear side of the reaction plate outlet are respectively provided with an outlet runner communicated with the reaction plate outlet, the inlet of the outlet runner is communicated with the front end outlet of the front free diffusion chamber, and the rear end inlet of the front free diffusion chamber is opposite to the front end of the reaction runner and is communicated with the front end outlet of the front free diffusion chamber; the size of the flow channel of the front free diffusion chamber gradually decreases from the back to the front; the side wall of the reaction plate is provided with at least one heating device mounting hole, and a first heating device is arranged in the heating device mounting hole;
the front end and the rear end of the evaporation plate are respectively provided with an evaporation plate inlet and an evaporation plate outlet which vertically penetrate through the evaporation plate, and the upper surface of the evaporation plate is provided with an evaporation chamber of which the two ends are respectively communicated with the evaporation plate inlet and the evaporation plate outlet; an electric heating groove is formed in the lower surface of the evaporation plate, and a second heating device is arranged in the electric heating groove;
the front end of the lower cover plate is provided with a lower cover plate inlet vertically penetrating through the lower cover plate, and the lower cover plate inlet is communicated with the evaporation plate inlet;
when one reaction plate is adopted, the inlet of the reaction plate is communicated with the outlet of the evaporation plate, and the outlet of the reaction plate is communicated with the outlet of the upper cover plate;
when a plurality of reaction plates are adopted, the inlets of the reaction plates are communicated with the outlets of the evaporation plates, and the outlets of the reaction plates are communicated with the outlets of the upper cover plate.
2. The reactor for producing hydrogen by stack-type micro-channel reforming according to claim 1, wherein graphite gaskets are respectively arranged between the upper cover plate and the reaction plate, between the reaction plate and the evaporation plate, and between the evaporation plate and the lower cover plate, and the graphite gaskets between the upper cover plate and the reaction plate are provided with through holes for communicating the outlet of the reaction plate with the outlet of the upper cover plate; the graphite gasket between the reaction plate and the evaporation plate is provided with a through hole which is communicated with the inlet of the reaction plate and the outlet of the evaporation plate; the graphite gasket between the evaporation plate and the lower cover plate is provided with a through hole communicated with the evaporation plate inlet and the lower cover plate inlet;
when a plurality of reaction plates are adopted, graphite gaskets are also arranged between two adjacent reaction plates, and the graphite gaskets between the two adjacent reaction plates are provided with through holes for communicating the inlets of the two adjacent reaction plates and through holes for communicating the outlets of the two adjacent reaction plates.
3. The stacked microchannel reforming hydrogen production reactor as claimed in claim 2, wherein the upper cover plate and the lower cover plate are 60-180 mm long, 35-95 mm wide and 2-20 mm high;
the length of the reaction plate is 60-180 mm, the width of the reaction plate is 35-95 mm, and the height of the reaction plate is 5-30 mm;
the length of the evaporation plate is 60-180 mm, the width of the evaporation plate is 35-95 mm, and the height of the evaporation plate is 2-20 mm;
the length of the graphite gasket is 60-180 mm, the width of the graphite gasket is 35-95 mm, and the height of the graphite gasket is 0.2-2 mm.
4. The laminated microchannel reforming hydrogen production reactor according to claim 1, wherein the first heating device is a thermocouple and an electric heating rod, the heating device mounting holes are thermocouple holes matched with the thermocouple and electric heating holes matched with the electric heating rod, the number of the electric heating holes is 2-6, the number of the thermocouple holes is 2-6, the diameter of the electric heating holes is 2-12 mm, and the center-to-center distance between two adjacent electric heating holes is 10-50 mm; the diameter of each thermocouple hole is 1-5 mm, and the distance between the centers of two adjacent thermocouple holes is 10-50 mm.
5. The stacked microchannel reforming hydrogen reactor as defined in claim 1, wherein the second heating means is an electrical heating plate.
6. The stacked microchannel reforming hydrogen production reactor as defined in claim 1, wherein the diameter Φ of the reaction plate inlet and the reaction plate outlet is 0.2-5 mm; the rear free diffusion chamber is conical, the vertex angle theta 1 of the rear free diffusion chamber is 30-160 degrees, the included angle theta 2 between the diffusion edge of the rear free diffusion chamber and the edge of the reaction plate is 90-150 degrees, and the included angle theta 3 between the diffusion edges of two adjacent front free diffusion chambers is 30-160 degrees; the height of the reaction flow channel is 0.2-5 mm; the number of the reaction channels is 6-26, the length L of the channels is 40-160 mm, the width W1 of the channels is 0.2-5 mm, and the ridge width W2 between the channels is 0.2-5 mm.
7. The reactor for producing hydrogen by reforming a stacked microchannel of claim 1, wherein the reaction channel is a straight channel, a wavy channel, a zigzag channel or a concave channel; the concave flow channel is linear, two side flow channel walls of the concave flow channel are respectively provided with a row of bulges uniformly distributed along the extending direction of the concave flow channel, and the bulges are arranged in a staggered manner.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211468452.3A CN115784152B (en) | 2022-11-22 | 2022-11-22 | Laminated microchannel reforming hydrogen production reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211468452.3A CN115784152B (en) | 2022-11-22 | 2022-11-22 | Laminated microchannel reforming hydrogen production reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115784152A CN115784152A (en) | 2023-03-14 |
| CN115784152B true CN115784152B (en) | 2024-04-02 |
Family
ID=85440190
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211468452.3A Active CN115784152B (en) | 2022-11-22 | 2022-11-22 | Laminated microchannel reforming hydrogen production reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115784152B (en) |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1546217A (en) * | 2003-12-12 | 2004-11-17 | 华东理工大学 | Catalytic reforming and catalytic dehydrogenation centrifugal type fixed bed radial reactor |
| KR20060040176A (en) * | 2004-11-04 | 2006-05-10 | 한국에너지기술연구원 | The fabrication method of microchannel reactor, and the same |
| CN102923656A (en) * | 2012-11-12 | 2013-02-13 | 浙江大学 | Laminating type micro-convex-table array type micro-reactor for steam reforming of methanol |
| CN203540511U (en) * | 2013-08-19 | 2014-04-16 | 浙江大学 | Laminated microchannel reactor with evenly distributed channel flow velocity |
| CN104671204A (en) * | 2015-02-15 | 2015-06-03 | 浙江大学 | Laminated double-sided multi-serpentine microchannel reforming hydrogen production reactor |
| CN205182697U (en) * | 2015-10-30 | 2016-04-27 | 中国石油化工股份有限公司 | Range upon range of formula microchannel reactor |
| CN107244653A (en) * | 2017-06-09 | 2017-10-13 | 浙江大学 | Hydrogen manufacturing microreactor with equal aperture porosity gradual change catalyst carrier |
| CN107464793A (en) * | 2017-08-17 | 2017-12-12 | 中国电子科技集团公司第二十九研究所 | A kind of microchannel based on microchannel porous flat pipe integrates cold drawing and preparation method |
| CN111196596A (en) * | 2020-01-14 | 2020-05-26 | 哈尔滨工业大学(深圳)(哈尔滨工业大学深圳科技创新研究院) | Micro-channel methanol hydrogen production reactor with uniformly distributed flow velocity and concentration |
| CN212189044U (en) * | 2020-05-09 | 2020-12-22 | 杭州沈氏节能科技股份有限公司 | Micro-reaction channel, reaction substrate and micro-channel reactor |
| CN112387218A (en) * | 2020-11-04 | 2021-02-23 | 大连海事大学 | Self-heating type tubular reforming hydrogen production reactor |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6805846B2 (en) * | 2001-06-18 | 2004-10-19 | Honda Giken Kogyo Kabushiki Kaisha | Compact reactor capable of being charged with catalytic material for use in a hydrogen generation/fuel cell system |
| US7077643B2 (en) * | 2001-11-07 | 2006-07-18 | Battelle Memorial Institute | Microcombustors, microreformers, and methods for combusting and for reforming fluids |
| US8177868B2 (en) * | 2002-01-04 | 2012-05-15 | Meggitt (Uk) Limited | Reforming apparatus and method |
-
2022
- 2022-11-22 CN CN202211468452.3A patent/CN115784152B/en active Active
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1546217A (en) * | 2003-12-12 | 2004-11-17 | 华东理工大学 | Catalytic reforming and catalytic dehydrogenation centrifugal type fixed bed radial reactor |
| KR20060040176A (en) * | 2004-11-04 | 2006-05-10 | 한국에너지기술연구원 | The fabrication method of microchannel reactor, and the same |
| CN102923656A (en) * | 2012-11-12 | 2013-02-13 | 浙江大学 | Laminating type micro-convex-table array type micro-reactor for steam reforming of methanol |
| CN203540511U (en) * | 2013-08-19 | 2014-04-16 | 浙江大学 | Laminated microchannel reactor with evenly distributed channel flow velocity |
| CN104671204A (en) * | 2015-02-15 | 2015-06-03 | 浙江大学 | Laminated double-sided multi-serpentine microchannel reforming hydrogen production reactor |
| CN205182697U (en) * | 2015-10-30 | 2016-04-27 | 中国石油化工股份有限公司 | Range upon range of formula microchannel reactor |
| CN107244653A (en) * | 2017-06-09 | 2017-10-13 | 浙江大学 | Hydrogen manufacturing microreactor with equal aperture porosity gradual change catalyst carrier |
| CN107464793A (en) * | 2017-08-17 | 2017-12-12 | 中国电子科技集团公司第二十九研究所 | A kind of microchannel based on microchannel porous flat pipe integrates cold drawing and preparation method |
| CN111196596A (en) * | 2020-01-14 | 2020-05-26 | 哈尔滨工业大学(深圳)(哈尔滨工业大学深圳科技创新研究院) | Micro-channel methanol hydrogen production reactor with uniformly distributed flow velocity and concentration |
| CN212189044U (en) * | 2020-05-09 | 2020-12-22 | 杭州沈氏节能科技股份有限公司 | Micro-reaction channel, reaction substrate and micro-channel reactor |
| CN112387218A (en) * | 2020-11-04 | 2021-02-23 | 大连海事大学 | Self-heating type tubular reforming hydrogen production reactor |
Non-Patent Citations (2)
| Title |
|---|
| Simulation of a compact multichannel membrane reactor for the production of pure hydrogen via steam methane reforming;Vigneault, A et al;《Chemical Engineering & Technology》;第35卷(第8期);第1520-1533页 * |
| 基于树形分叉结构的微通道甲醇重整制氢;沈寅麒;张云芳;陈桂山;;《电力与能源》(第01期);第70-73页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115784152A (en) | 2023-03-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110155945B (en) | Self-heating methanol reforming hydrogen production reactor integrating CO selective methanation | |
| CN102910584B (en) | Self-heating laminated micro-channel reforming hydrogen production reactor | |
| CN102674246B (en) | Solar heating plate-type methanol reforming microreactor for producing hydrogen | |
| Zeng et al. | Fabrication and characteristics of cube-post microreactors for methanol steam reforming | |
| CN101580227B (en) | Self-heating type alcohol reforming hydrogen production micro channel reactor with micro-lug boss array structure | |
| CN113745562B (en) | Cathode flow field plate, bipolar plate and PEMFC for PEMFC | |
| CN105502287B (en) | The hydrogen manufacturing micro-reformer of belt surface porous micro-boss array structure catalyst carrier | |
| CN205668941U (en) | Utilize the ethanol reformation device of engine tail gas waste-heat hydrogen manufacturing | |
| CN107244653A (en) | Hydrogen manufacturing microreactor with equal aperture porosity gradual change catalyst carrier | |
| CN205527732U (en) | Area surface porousization dimpling platform array structure catalyst support's little reformer of hydrogen manufacturing | |
| CN111196596A (en) | Micro-channel methanol hydrogen production reactor with uniformly distributed flow velocity and concentration | |
| CN110143575B (en) | Corrugated substrate-porous metal self-heating methanol reforming hydrogen production reactor | |
| CN101531336B (en) | Small-sized high efficiency self-heating natural gas hydrogen-preparing device | |
| CN115784152B (en) | Laminated microchannel reforming hydrogen production reactor | |
| Chen et al. | A numerical comprehensive evaluation of a micro-type plate autothermal methanol steam reformer with different channel configurations | |
| CN110803679B (en) | Methanol reforming hydrogen production reactor with flow velocity distribution uniformity | |
| CN109761193B (en) | Methanol reforming hydrogen production reactor | |
| CN204454565U (en) | A kind of self-heating type reformation hydrogen production microreactor with function of recovering waste heat | |
| CN110155946B (en) | Hydrogen production micro-reformer with fractal structure catalyst carrier | |
| CN115845761B (en) | Microchannel reaction plate | |
| CN113735059B (en) | Alcohol reforming micro-reactor and hydrogen production method | |
| CN108002347B (en) | Methanol-steam reforming hydrogen production reactor with ultrasonic assistance | |
| CN115010087A (en) | HI decomposition hydrogen production membrane reactor and hydrogen production method and system thereof | |
| KR20150135561A (en) | Integrated Reformer for Fuel Cell System | |
| CN201427859Y (en) | Self-heating type microchannel reactor with micro-boss array structure for reforming alcohol to make hydrogen |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |