CN115784152A - Stacked microchannel reforming hydrogen production reactor - Google Patents
Stacked microchannel reforming hydrogen production reactor Download PDFInfo
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- CN115784152A CN115784152A CN202211468452.3A CN202211468452A CN115784152A CN 115784152 A CN115784152 A CN 115784152A CN 202211468452 A CN202211468452 A CN 202211468452A CN 115784152 A CN115784152 A CN 115784152A
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- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 81
- 239000001257 hydrogen Substances 0.000 title claims abstract description 81
- 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 68
- 238000002407 reforming Methods 0.000 title claims abstract description 37
- 238000006243 chemical reaction Methods 0.000 claims abstract description 181
- 230000008020 evaporation Effects 0.000 claims abstract description 86
- 238000001704 evaporation Methods 0.000 claims abstract description 86
- 238000009792 diffusion process Methods 0.000 claims abstract description 55
- 238000005485 electric heating Methods 0.000 claims abstract description 40
- 238000010438 heat treatment Methods 0.000 claims description 32
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 24
- 229910002804 graphite Inorganic materials 0.000 claims description 20
- 239000010439 graphite Substances 0.000 claims description 20
- 229910021389 graphene Inorganic materials 0.000 claims description 3
- 230000000149 penetrating effect Effects 0.000 claims description 3
- 239000012530 fluid Substances 0.000 abstract description 17
- 238000012546 transfer Methods 0.000 abstract description 4
- 230000002708 enhancing effect Effects 0.000 abstract description 2
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 60
- 238000009826 distribution Methods 0.000 description 9
- 239000007789 gas Substances 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- 230000009471 action Effects 0.000 description 4
- 238000011161 development Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 239000002028 Biomass Substances 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 230000003321 amplification Effects 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 150000002431 hydrogen Chemical class 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
- 230000009467 reduction Effects 0.000 description 2
- 238000006057 reforming reaction Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical class [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 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
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000014509 gene expression Effects 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
- 238000001179 sorption measurement Methods 0.000 description 1
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Abstract
The invention provides a stacked 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 inlet of the lower cover plate is communicated with the inlet of the evaporation plate, the outlet of the evaporation plate is communicated with the inlet of the reaction plate, and the outlet of the reaction plate is communicated with the outlet of the upper cover plate; the bottom of the evaporation plate is provided with an electric heating plate, the side wall of the reaction plate is provided with an electric thermocouple and an electric heating rod, the upper surface of the reaction plate is provided with a parting flow channel, a rear free diffusion chamber, a reaction flow channel, a front free diffusion chamber and an outlet flow channel, and fluid is uniformly diffused to the reaction flow channel at the rear free diffusion chamber and then is converged to an outlet of the reaction plate at the positions of the front free diffusion chamber and the outlet flow channel. The laminated microchannel reforming hydrogen production reactor provided by the invention has the advantages of effectively reducing pressure drop, enhancing heat and mass transfer characteristics, having excellent hydrogen production performance, further reducing the overall size of the reforming hydrogen production reactor and optimizing the space volume of the reactor.
Description
Technical Field
The invention relates to the technical field of reforming hydrogen production, in particular to a stacked microchannel reforming hydrogen production reactor.
Background
Nowadays, environmental problems are becoming more severe, and energy conservation and emission reduction become one of the major problems facing society. The hydrogen energy has the characteristics of high efficiency, cleanness, green and sustainable development and the like, and is regarded as one of clean energy sources with the most development potential in the new century. With the promulgation of new energy policies in various regions, hydrogen energy becomes a popular novel energy source, and has wide application prospects in the industrial field.
At present, the hydrogen production modes are mainly divided into the traditional hydrogen production by fossil energy and the hydrogen production by novel energy. The traditional fossil energy hydrogen production mainly comprises petroleum hydrogen production, coal hydrogen production and natural gas hydrogen production. Although the hydrogen production by fossil energy is still the main hydrogen production mode at present, the pollution to the environment is large and the standard of 'green hydrogen' is not met. The novel energy source hydrogen production mainly comprises biomass hydrogen production, water electrolysis hydrogen production, solar hydrogen production and alcohol substance hydrogen production. Wherein, the biomass hydrogen production can be operated continuously and stably, the hydrogen production cost is increased by electrolyzing water to produce hydrogen, and the solar hydrogen production is greatly influenced by the environment. The alcohol substance hydrogen production mainly comprises methanol reforming hydrogen production, and methanol is cracked into H under certain temperature and pressure conditions 2 Reacting with carbon-containing gas such as CO, CO and steam to generate H 2 With CO 2 And then removing CO by pressure swing adsorption 2 Finally obtaining high-purity H 2 . The hydrogen production process by methanol reforming is simple, raw materials are easy to obtain, the production mode is stable and reliable, and the method is suitable for medium and small scale hydrogen production.
Due to the special physical and chemical properties of hydrogen, the storage and transportation of hydrogen become a significant challenge 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 in price, the hydrogen production is stable and safe, and the methanol reforming hydrogen production micro-reactor is small in size, simple in structure and convenient to transport. The methanol is used for on-site hydrogen production through the reforming microreactor, so that the hydrogen is supplied in time, the method is more suitable for a mobile on-line hydrogen production scene, and a new solution is provided for the storage and transportation of the hydrogen.
The methanol reforming hydrogen production micro-reactor mainly comprises a cylindrical micro-reactor and a plate micro-reactor. The cylindrical microreactor is simple to process and assemble, but the cylindrical microreactor has the defects of high pressure drop, uneven temperature distribution and difficulty in integrated amplification due to the cylindrical structural design; the plate-type microreactor is a stacked assembly mode, each layer of the microreactor is relatively independent, the assembly is simple, the microreactor has a higher heat exchange area, the temperature distribution is uniform, and the integrated amplification is easier. An excellent reforming hydrogen production micro-channel reactor is very important to the hydrogen production performance.
The microchannel reactor with uniformly distributed flow velocity and concentration, which is proposed in patent document No. CN111196596A, can make the flow velocity and concentration of fluid more uniform, but the parting flow channel at the front end of the reaction plate is too complicated, the space sacrifice on the reaction plate is large, the utilization rate is low, and the space volume of the reactor is enlarged; the hydrogen production micro-reformer with the fractal structure catalyst carrier, which is proposed in the patent document with the publication number of CN110155946B, can realize good hydrogen production performance, but the structure of the reaction carrier plate is more complex, and the manufacturing cost is increased.
The existing microchannel reforming hydrogen production reactor can only achieve partial excellent performances, and the excellent performances such as flow velocity distribution uniformity, lower pressure drop, high hydrogen conversion rate, utilization rate of a reaction plate space and the like are not integrated. Therefore, the development of a microchannel reforming hydrogen production reactor with better performance is a problem to be solved in the field.
Disclosure of Invention
According to the technical problem, a stacked microchannel reforming hydrogen production reactor is provided. The novel microchannel reaction flow channel is designed on the reaction plate, and combines the structural characteristics of the parting flow channel and the A-type flow channel, so that fluid reaches a diffusion port from an inlet through the parting flow channels on two sides and is uniformly distributed in a cavity under 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 channel is in a shrinkage shape, and hydrogen and other gas products after chemical reaction are collected and amplified, so that the later-stage gas treatment is facilitated. The heating mode of the stacked microchannel reforming hydrogen production reactor is that an electric heating rod is combined with a heating plate, the heating mode of the electric heating rod is adopted for accurate temperature control of a reaction plate, the heating mode of the electric heating plate is adopted for non-accurate temperature control of an evaporation 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 technical means adopted by the invention are as follows:
a stacked 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 set 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;
a reaction flow channel is arranged on the upper surface of the reaction plate, and a reaction plate outlet and a reaction plate inlet which vertically penetrate through the reaction plate are respectively arranged at the front end and the rear end of the reaction flow channel; the two sides of the inlet of the reaction plate are respectively provided with a parting flow channel communicated with the inlet of the reaction plate, the outlet of the parting flow channel is communicated with the inlet of the rear end of the rear free diffusion chamber, and the outlet of the front end of the rear free diffusion chamber is opposite to and communicated with the rear end of the reaction flow channel; the size of the flow channel 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 flow channel communicated with the reaction plate outlet, the inlet of the outlet flow channel 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 and communicated with the front end of the reaction flow channel; the size of the flow channel of the front free diffusion chamber is gradually reduced from back to front; the side wall of the reaction plate is provided with at least one heating device mounting hole, and a first heating device is mounted in the heating device mounting hole;
an evaporation plate inlet and an evaporation plate outlet which vertically penetrate through the evaporation plate are respectively machined at the front end and the rear end of the evaporation plate, and an evaporation chamber with two ends respectively communicated with the evaporation plate inlet and the evaporation plate outlet is arranged on the upper surface of the evaporation plate; the lower surface of the evaporation plate is provided with an electric heating groove, 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 which vertically penetrates 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, a plurality of reaction plate inlets are communicated with the evaporation plate outlet, and a plurality of reaction plate outlets are communicated with the upper cover plate outlet.
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 reaction plate outlet and the upper cover plate outlet; the graphite gasket between the reaction plate and the evaporation plate is provided with a through hole for communicating 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 for communicating the inlet of the evaporation plate with the inlet of the lower cover plate;
when a plurality of reaction plates are adopted, the graphite gasket is also arranged between two adjacent reaction plates, and the graphite gasket between two adjacent reaction plates is provided with a through hole for communicating the inlets of two adjacent reaction plates and a through hole for communicating the outlets of two adjacent reaction plates.
Preferably, the upper cover plate and the lower cover plate have a length of 60-180 mm, a width of 35-95 mm and a height of 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 graphite gasket has a length of 60-180 mm, a width of 35-95 mm and a height of 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 diameter of each electric heating hole is 2-12 mm, and the distance between the centers of 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.
Preferably, the second heating means is an electric heating plate.
Preferably, the diameter phi of the reaction plate inlet and the reaction plate outlet is 0.2-5 mm; the back free diffusion chamber is conical, the vertex angle theta 1 of the back free diffusion chamber is 30-160 degrees, the included angle theta 2 between the diffusion edge of the back 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 flow channels is 6-26, the length L of the flow channels is 40-160 mm, the width W1 is 0.2-5 mm, and the ridge width W2 between the flow channels is 0.2-5 mm.
Preferably, the reaction flow channel is a straight flow channel, a wave-shaped flow channel, a fold line-shaped flow channel or an inward 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 which are uniformly distributed along the extending direction of the concave flow channel, and the two rows of bulges are arranged in a staggered manner.
Compared with the prior art, the invention has the following advantages:
1. the stacked microchannel reforming hydrogen production reactor provided by the invention effectively reduces the pressure drop, enhances the heat and mass transfer characteristics and has excellent hydrogen production performance.
2. The novel stacked microchannel reforming hydrogen production reactor provided by the invention adopts the combination of the heating modes of the electric heating rod and the electric heating plate, adopts the heating mode of the electric heating rod for the accurate temperature control of the reaction plate, and adopts the heating mode of the electric heating plate for the non-accurate temperature control of the evaporation plate, so that 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.
3. According to the novel laminated microchannel reforming hydrogen production reactor, the novel microchannel reaction channel utilizes the two parting channels, so that the sufficient diffusion of fluid in a flow field is facilitated, the uniformity of fluid distribution is enhanced, and the flow velocity distribution of the fluid is more uniform.
4. According to the novel stacked microchannel reforming hydrogen production reactor provided by the invention, the novel microchannel reaction flow channel lengthens the parallel flow channel part at the middle part, so that the flow field flow is longer, the specific surface area is increased, and the methanol steam fully carries out chemical reaction, thereby improving the conversion rate of methanol.
5. According to the novel stacked microchannel reforming hydrogen production reactor provided by the invention, the tail end of the novel microchannel reaction flow channel is in a shrinkage shape, so that the hydrogen generated after chemical reaction is conveniently collected and amplified, and the post-treatment of the gas is conveniently carried out.
6. Compared with the traditional flow channel, the novel micro-channel reaction flow channel of the stacked novel micro-channel reforming hydrogen production reactor provided by the invention has the advantages of higher space utilization rate, simple structure, easiness in processing, reduction in manufacturing cost and good economy.
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, finally realize the preparation of high-purity hydrogen and realize the on-line hydrogen production.
Based on the reasons, the method can be widely popularized in the fields of hydrogen production by reforming 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 used in the description of the embodiments or the prior art will be briefly introduced below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
Fig. 1 is a schematic structural diagram of a stacked microchannel reforming hydrogen production reactor according to an embodiment of the present invention.
Fig. 2 is a schematic structural diagram of an upper cover plate according to an embodiment of the present invention.
FIG. 3 is a schematic view of a reaction plate according to an embodiment of the present invention.
FIG. 4 is a top view of a reaction plate according to an embodiment of the present invention.
FIG. 5 is a top view three-dimensional schematic view of an evaporation plate according to an embodiment of the present invention.
FIG. 6 is a bottom view three-dimensional schematic view of an evaporation plate according to an embodiment of the present invention.
FIG. 7 is a schematic view of a reaction channel in accordance with an embodiment of the present invention.
FIG. 8 is a flow diagram of the reaction fluid in an embodiment of the present invention.
FIG. 9 is a flow diagram of the reaction fluid within the reaction plate in accordance with 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. a reaction plate inlet; 10. a reaction plate outlet; 11. an upper cover plate outlet; 12. an evaporation chamber; 13. a reaction flow channel; 14. electrically heating the hole; 15. a thermocouple hole; 16. an electrical 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 the embodiments and features of the embodiments may be combined with each other without conflict. The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, 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 the embodiments. The following description of at least one exemplary embodiment is merely illustrative in nature and is in no way intended to limit the invention, its application, or uses. 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.
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 invention. As used herein, the singular forms "a", "an", and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
The relative arrangement of the components and steps, the numerical expressions and numerical values set forth in these embodiments do not limit the scope of the present invention unless specifically stated otherwise. Meanwhile, it should be understood that the sizes of the respective portions shown in the drawings are not drawn in an actual proportional relationship for the convenience of description. Techniques, methods, and apparatus known to those 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 particular value should be construed as exemplary only and not as limiting. Thus, other examples of the exemplary embodiments may have different values. It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, further discussion thereof is not required in subsequent figures.
In the description of the present invention, it is to be understood that the orientation or positional relationship indicated by the directional terms such as "front, rear, upper, lower, left, right", "lateral, vertical, horizontal" and "top, bottom", etc., are generally based on the orientation or positional relationship shown in the drawings, and are used for convenience of description and simplicity of description only, and in the absence of any contrary indication, these directional terms are not intended to indicate and imply that the device or element so referred to must have a particular orientation or be constructed and operated in a particular orientation, and therefore should not be considered as limiting the scope of the present invention: the terms "inner and outer" refer to the inner and outer relative to the profile of the respective component itself.
For ease of description, spatially relative terms such as "over 8230 \ 8230;,"' over 8230;, \8230; upper surface "," above ", etc. may be used herein to describe the spatial relationship of one device or feature to another device or feature as shown in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. For example, if a device in the figures is turned over, devices described as "above" or "on" other devices or configurations would then be oriented "below" or "under" the other devices or configurations. Thus, the exemplary terms "at 8230; \8230; above" may include both orientations "at 8230; \8230; above" and "at 8230; \8230; below". The device may be otherwise variously oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein interpreted accordingly.
It should be noted that the terms "first", "second", and the like are used to define the components, and are only used for convenience of distinguishing the corresponding components, and the terms have no special meanings unless otherwise stated, and therefore, the scope of the present invention should not be construed as being limited.
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 on the periphery of the upper cover plate, the diameter of each bolt hole is 0.2-1.8 mm, and the bolts penetrate through the bolt holes to fix the upper cover plate, the reaction plate, the evaporation plate and the lower cover plate 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 through 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 reaction plate 2 has a length of 60 to 180mm, a width of 35 to 95mm and a height of 5 to 30mm; a reaction flow channel 13 is arranged on the upper surface of the reaction plate 2, and a reaction plate outlet 10 and a reaction plate inlet 9 which vertically penetrate through the reaction plate 2 are respectively arranged at the front end and the rear end of the reaction flow channel 13; the two sides of the reaction plate inlet 9 are respectively provided with a parting flow channel 17 communicated with the reaction plate inlet, the outlet of the parting flow channel 17 is communicated with the rear end inlet of a rear free diffusion chamber 18, and the front end outlet of the rear free diffusion chamber 18 is opposite to and communicated with the rear end of the reaction flow channel 13; the rear free diffusion chamber 18 gradually increases in flow passage size from rear to front; the two sides and the rear side of the reaction plate outlet 10 are respectively provided with an outlet flow channel 19 communicated with the reaction plate outlet, the inlet of the outlet flow channel 19 is communicated with the front end outlet of a front free diffusion chamber 20, and the rear end inlet of the front free diffusion chamber 20 is opposite to and communicated with the front end of the reaction flow channel 13; the front free diffusion chamber 20 gradually decreases in flow passage size from back to 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 mounted in the heating device mounting hole; the first heating device is a thermocouple (not shown) and an electric heating rod (not shown), the heating device mounting holes are thermocouple holes 15 matched with the thermocouple and electric heating holes 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 each electric heating hole 14 is 2-12 mm, and the distance between the centers of two adjacent electric heating holes 14 is 10-50 mm; the diameter of each thermocouple hole 15 is 1-5 mm, and the distance between the centers of 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 flow channel 13 is 0.2-5 mm; the number of the reaction flow channels 13 is 6-26, the length L of the flow channels is 40-160 mm, the width W1 is 0.2-5 mm, and the width W2 of the ridge between the flow channels is 0.2-5 mm.
As shown in fig. 5, the length of the evaporation 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 evaporation plate 3 is provided with an electric heating groove 16, and a second heating device is installed in the electric heating groove; 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; the front end of the lower cover plate 4 is provided with a lower cover plate inlet 6 which vertically penetrates through 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 reaction plate inlet 9 is communicated with the evaporation plate outlet 7, and the reaction plate outlet 10 is communicated with the upper cover plate outlet 11; when a plurality of reaction plates 2 are used, the plurality of reaction plate inlets 9 are all communicated with the evaporation plate outlet 7, and the plurality of reaction plate outlets 10 are all communicated with the upper cover plate outlet 11.
The graphite gasket 5 between the upper cover plate 1 and the reaction plate 2 is provided with a through hole for communicating 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 is provided with a through hole for 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 used, the graphite gasket 5 between two adjacent reaction plates 2 has a through hole for communicating the inlets 9 of two adjacent reaction plates and a through hole for communicating the outlets 10 of two adjacent reaction plates. In this example, a 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 wave-shaped flow channel, a fold-line-shaped flow channel or an inward concave flow channel as shown in fig. 7, in addition to the straight flow channel 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 which are uniformly distributed along the extending direction of the concave flow channel, and the two rows of bulges are arranged in a staggered manner.
As shown in fig. 8, the aqueous methanol solution enters the reactor through 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 evaporation plate 3, under the action of the electric heating plate, the temperature of the evaporation plate rises to reach the evaporation temperature of the methanol water solution, and the methanol water solution is absorbed and evaporated in the evaporation chamber 12 to form methanol water vapor. Due to diffusion of the fluid, the methanol vapor reaches the 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 steam. The methanol vapor is distributed along the flow channel in the reaction plate 2 and enters the catalytic area, and hydrogen and other products are generated under the action of the catalyst, and the specific equation is as follows:
reforming reaction:
and (3) decomposition reaction:
water vapor reverse reaction:
due to the diffusion effect of the fluid, the hydrogen and other gas products after the chemical reaction diffuse to the reaction plate outlet 10, and finally flow out of the reactor after reaching the upper cover plate outlet 11.
In this embodiment, the reaction plate 2 is provided with a typing channel 17, a rear free diffusion chamber 18, a front free diffusion chamber 20, and an outlet channel 19. At the beginning of the reaction, as shown in fig. 9, methanol vapor enters from the inlet 9 of the reaction plate, and through the free flow and diffusion of the fluid, the methanol vapor flows to the diffusion port a and the diffusion port B, respectively, and then diffuses to the reaction flow channel 13 to undergo a chemical reaction, at which time the methanol vapor reforms to produce hydrogen and carbon oxides. When the fluid reaches the end of the parallel flow channel, the gas products are diffused to the positions C, D and E, and finally are collected to the reaction plate outlet 10 through the outlet flow channel 19, and then flow out of the reaction plate 2 after being collected and amplified by the front free diffusion chamber 20 and the outlet flow channel 19. The reaction plate 2 has the characteristic of uniform flow distribution of the parting flow channels 17, methanol vapor uniformly flows to the rear free diffusion chamber 18 for diffusion through the parting flow channels 17 on 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 characteristics of low pressure drop and high methanol conversion rate of the A-type flow channel are realized.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and these modifications or substitutions do not depart from the spirit of the corresponding technical solutions of the embodiments of the present invention.
Claims (7)
1. A stacked 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;
a reaction flow channel is arranged on the upper surface of the reaction plate, and a reaction plate outlet and a reaction plate inlet which vertically penetrate through the reaction plate are respectively arranged at the front end and the rear end of the reaction flow channel; the two sides of the inlet of the reaction plate are respectively provided with a parting flow channel communicated with the inlet of the reaction plate, the outlet of the parting flow channel is communicated with the inlet of the rear end of the rear free diffusion chamber, and the outlet of the front end of the rear free diffusion chamber is opposite to and communicated with the rear end of the reaction flow channel; the size of the flow channel 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 flow channel communicated with the reaction plate outlet, the inlet of the outlet flow channel 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 and communicated with the front end of the reaction flow channel; the size of the flow channel of the front free diffusion chamber is gradually reduced from back to front; the side wall of the reaction plate is provided with at least one heating device mounting hole, and a first heating device is mounted in the heating device mounting hole;
an evaporation plate inlet and an evaporation plate outlet which vertically penetrate through the evaporation plate are respectively machined at the front end and the rear end of the evaporation plate, and an evaporation chamber with two ends respectively communicated with the evaporation plate inlet and the evaporation plate outlet is arranged on the upper surface of the evaporation plate; the lower surface of the evaporation plate is provided with an electric heating groove, 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 which vertically penetrates 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, a plurality of reaction plate inlets are communicated with the evaporation plate outlet, and a plurality of reaction plate outlets are communicated with the upper cover plate outlet.
2. The stacked microchannel reforming hydrogen production reactor according to claim 1, wherein graphite gaskets are respectively disposed 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 have through holes communicating the reaction plate outlet and the upper cover plate outlet; the graphite gasket between the reaction plate and the evaporation plate is provided with a through hole for communicating the inlet of the reaction plate with the outlet of the evaporation plate; the graphene gasket between the evaporation plate and the lower cover plate is provided with a through hole for communicating the inlet of the evaporation plate with the inlet of the lower cover plate;
when a plurality of reaction plates are adopted, the graphite gasket is also arranged between two adjacent reaction plates, and the graphite gasket between two adjacent reaction plates is provided with a through hole for communicating inlets of two adjacent reaction plates and a through hole for communicating outlets of two adjacent reaction plates.
3. The stacked microchannel reforming hydrogen production reactor of claim 2, wherein the upper cover plate and the lower cover plate have a length of 60 to 180mm, a width of 35 to 95mm, and a height of 2 to 20mm;
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 graphite gasket has a length of 60-180 mm, a width of 35-95 mm and a height of 0.2-2 mm.
4. The stacked 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 a thermocouple hole matched with the thermocouple and an electric heating hole matched with the electric heating rod, the number of the electric heating holes is 2 to 6, the number of the thermocouple holes is 2 to 6, the diameter of the electric heating hole is 2 to 12mm, and the distance between the centers of two adjacent electric heating holes is 10 to 50mm; 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 production reactor of claim 1, wherein the second heating device is an electrically heated plate.
6. The stacked microchannel reforming hydrogen production reactor of claim 1, wherein the diameter Φ of the reaction plate inlet and the reaction plate outlet is 0.2-5 mm; the back free diffusion chamber is conical, the vertex angle theta 1 of the back free diffusion chamber is 30-160 degrees, the included angle theta 2 between the diffusion edge of the back 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 flow channels is 6-26, the length L of the flow channels is 40-160 mm, the width W1 is 0.2-5 mm, and the ridge width W2 between the flow channels is 0.2-5 mm.
7. The stacked microchannel reforming hydrogen production reactor according to claim 1, wherein the reaction flow channel is a straight flow channel, a wave-shaped flow channel, a fold line-shaped flow channel or an inward 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 which are uniformly distributed along the extending direction of the concave flow channel, and the two rows of bulges are arranged in a staggered manner.
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