CN113735059B - Alcohol reforming micro-reactor and hydrogen production method - Google Patents
Alcohol reforming micro-reactor and hydrogen production method Download PDFInfo
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- CN113735059B CN113735059B CN202110966066.6A CN202110966066A CN113735059B CN 113735059 B CN113735059 B CN 113735059B CN 202110966066 A CN202110966066 A CN 202110966066A CN 113735059 B CN113735059 B CN 113735059B
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/323—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/085—Methods of heating the process for making hydrogen or synthesis gas by electric heating
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- C01B2203/10—Catalysts for performing the hydrogen forming reactions
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- C01B2203/1041—Composition of the catalyst
- C01B2203/1076—Copper or zinc-based catalysts
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- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1217—Alcohols
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- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
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- C01B2203/1223—Methanol
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- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
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- C01B2203/1229—Ethanol
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1288—Evaporation of one or more of the different feed components
Abstract
The application discloses an alcohol reforming micro-reactor and a hydrogen production method, aiming at improving the heat exchange capacity of a reactor on the premise of not influencing the flow capacity of the reactor. Therefore, the alcohol reforming micro-reactor provided by the embodiment of the application comprises an evaporation plate, a middle partition plate and a reforming plate which are sequentially overlapped from top to bottom, wherein an evaporation chamber is formed between the evaporation plate and the middle partition plate, a reforming chamber is formed between the middle partition plate and the reforming plate, an outlet of the evaporation chamber is communicated with an inlet of the reforming chamber, a hydrogen production catalyst is loaded on the reforming chamber, heating elements are further arranged on the evaporation plate, the middle partition plate and/or the reforming plate, the evaporation chamber is formed by a snake-shaped straight micro-channel or a snake-shaped ripple micro-channel, and the reforming chamber is formed by a plurality of straight-line channel sections which are sequentially connected end to end and are parallel to each other; the serpentine ripple micro-channel consists of a plurality of sine ripple sections which are connected end to end in sequence and are parallel to each other, and the straight-line channel section is provided with a T cell.
Description
Technical Field
The application belongs to the technical field of energy and power, and particularly relates to an alcohol reforming microreactor and a hydrogen production method.
Background
Hydrogen is a main carrier of hydrogen energy and is also a consumed direct raw material of PEMFC, and has the outstanding advantages of green cleaning, zero carbon emission, reproducibility, wide preparation route and the like, but the wide application of hydrogen is limited due to the problem of hydrogen storage and transportation. In order to solve the problem of hydrogen storage and transportation, one practical and effective solution is to replace hydrogen with other liquid hydrogen energy carriers (such as alcohols including methanol, ethanol, glycerol, etc.) to avoid the problem of hydrogen storage and transportation. The alcohols have high energy density and high energy conversion rate, are liquid at normal temperature and normal pressure, are easier to transport and store, and can prepare hydrogen to be supplied to the PEMFC through alcohol reforming reaction, so that the alcohols have wide application prospect.
While the technology of real-time hydrogen production by alcohol reforming currently has the limitation of poor performance of the reactor, recently emerging micro-reactors are attracting attention due to the micro-channel structure. However, the heat exchange capacity and the flow capacity of the traditional micro-channel are mutually limited to a certain extent, so that the hydrogen production performance of alcohol reforming in the micro-reactor is limited, and the micro-reactor needs to be further designed and optimized.
Disclosure of Invention
The application mainly aims to provide an alcohol reforming micro-reactor and a hydrogen production method, and aims to improve the heat exchange capacity of a reactor on the premise of not influencing the flow capacity of the reactor.
Therefore, the alcohol reforming micro-reactor provided by the embodiment of the application comprises an evaporation plate, a middle partition plate and a reforming plate which are sequentially overlapped from top to bottom, wherein an evaporation chamber is formed between the evaporation plate and the middle partition plate, and a reforming chamber is formed between the middle partition plate and the reforming plate;
the outlet of the evaporation chamber is communicated with the inlet of the reforming chamber, the reforming chamber is loaded with a hydrogen production catalyst, and the evaporation plate, the middle partition plate and/or the reforming plate are/is also provided with a heating element;
the evaporation chamber is formed by a serpentine straight micro-channel or a serpentine corrugated micro-channel, and the reforming chamber is formed by a serpentine straight micro-channel or a serpentine corrugated micro-channel; wherein, the liquid crystal display device comprises a liquid crystal display device,
the serpentine straight micro-channel consists of a plurality of straight channel sections which are connected end to end in sequence and are parallel to each other;
the serpentine ripple micro-channel is formed by a plurality of sine ripple sections which are connected end to end in sequence and are parallel to each other, and the straight-line channel section is provided with a T cell.
Specifically, a plurality of butyl cells are uniformly arranged on each sine ripple section.
Specifically, a plurality of the butyl cells are uniformly arranged on each straight line runner section.
Specifically, a temperature thermocouple is further arranged on the evaporation plate, the middle partition plate and/or the reforming plate.
Specifically, the hydrogen production catalyst is coated on the micro flow channel.
Specifically, the hydrogen production catalyst adopts a copper-based catalyst or a copper-based oxygen carrier.
Firstly, introducing alcohol substances into an evaporation chamber, and vaporizing the alcohol substances in the evaporation chamber under the action of a heat source provided by a heating element to obtain mixed steam; subsequently, the mixed steam enters a reforming chamber; finally, alcohol steam reforming reaction occurs under the action of a catalyst, so that on-site hydrogen production is realized.
Specifically, the alcohol is methanol, ethanol or glycerol
On the basis of researching the alcohol steam catalytic reforming reaction, the application summarizes the reaction characteristics and influence factors, and aims at increasing the heat exchange area and enhancing the fluid disturbance, three novel micro-channel micro-channels, namely a snake-shaped straight micro-channel (DMD) with butyl cells, a snake-shaped corrugated micro-channel (SM) and a snake-shaped corrugated micro-channel (SMD) with butyl cells, are designed based on the traditional snake-shaped straight micro-channel (DM) and by introducing sine waves and a butyl cell structure, and compared with the prior art, at least one embodiment of the application has the following beneficial effects:
1. on the basis of a snakelike straight micro-channel, sine waves are additionally designed: the sine wave design converts the straight micro-channel into the wave micro-channel, compared with the straight micro-channel, the cold and hot fluid in the sine micro-channel has extremely strong mixing effect, and the internal fluid has unstable flow along with the formation of the separation flow and the oscillating flow; in summary, the special sine ripple structure can greatly improve the heat exchange capacity of the micro-channel, and the resistance coefficient is little increased, so as to strengthen the transportation process of the micro-channel thermal mass and further improve the hydrogen production performance (hydrogen atom utilization rate, hydrogen relative concentration and hydrogen yield) of the micro-channel reactor;
2. on the basis of the serpentine straight micro-channel, a T cell structure is additionally designed, wherein the T cell structure is regularly or irregularly arranged and large-sized bulges and depressions in the channel, compared with the straight micro-channel, the T cell increases the heat exchange area, the local boundary layer instability phenomenon of fluid is caused by the formation of vortex and secondary flow, and even the T cell drag reduction effect can occur when the T cell structure is added into the serpentine corrugated micro-channel. In summary, the special butyl cell structure can also improve the heat exchange capacity, the resistance coefficient is slightly increased or even reduced, the transportation process of the micro-channel thermal mass is enhanced, and the hydrogen production performance of the micro-channel reactor is further improved.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings required for the description of the embodiments will be briefly described below, and it is apparent that the drawings in the following description are only some embodiments of the present application, 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 an alcohol reforming microreactor according to an embodiment of the present application;
FIG. 2 is a schematic diagram of an alcohol reforming microreactor according to an embodiment of the present application;
FIG. 3 is a schematic view of a micro flow channel structure according to an embodiment of the present application;
FIG. 4 is a schematic view of another micro flow channel structure according to an embodiment of the present application;
FIG. 5 is a schematic diagram illustrating the heat exchange capacity and flow capacity simulation of different types of microchannels according to an embodiment of the present application;
FIG. 6 is a simulated cloud image of the cross-sectional density and temperature distribution of a corrugated microchannel according to an embodiment of the application;
FIG. 7 is a schematic diagram of simulation of the distribution of main vortex cores of a micro-channel according to an embodiment of the present application;
FIG. 8 is a schematic diagram of velocity vector simulation of an inlet section of a serpentine straight micro-channel according to an embodiment of the present application;
FIG. 9 is a schematic diagram of velocity vector simulation of the outlet section of a straight serpentine microchannel with cells according to an embodiment of the application;
FIG. 10 is a schematic diagram of velocity vector simulation at a corner of a corrugated microchannel according to an embodiment of the application;
FIG. 11 is a schematic diagram of velocity vector simulation at a butyl cell of a corrugated microchannel with butyl cells according to an embodiment of the present application;
FIG. 12 is a graph showing hydrogen production performance of different similar alcohol reforming microreactors according to an embodiment of the present application;
wherein: 1. an evaporation plate; 2. a middle partition plate; 3. a reforming plate; 4. an evaporation chamber; 5. a reforming chamber; 6. serpentine straight micro-channel; 601. a straight flow path section; 7. a heating element; 8. a temperature thermocouple; 9. b, butyl cells; 10. serpentine corrugated micro-fluidic channels; 101. sinusoidal wave segments.
Detailed Description
The following description of the embodiments of the present application will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present application, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the application without making any inventive effort, are intended to be within the scope of the application.
In the description of the present application, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present application and simplifying the description, and do not indicate or imply that the device or element being referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present application.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present application, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
Referring to fig. 1-3, an alcohol reforming micro-reactor comprises an evaporation plate 1, a middle partition plate 2 and a reforming plate 3 which are sequentially overlapped from top to bottom, wherein an evaporation chamber 4 is formed between the evaporation plate 1 and the middle partition plate 2, a reforming chamber 5 is formed between the middle partition plate 2 and the reforming plate 3, an outlet of the evaporation chamber 4 is communicated with an inlet of the reforming chamber 5, a hydrogen production catalyst is loaded on the reforming chamber 5, the evaporation chamber 4 and the reforming chamber 5 are both composed of a snake-shaped straight micro-channel 6, a heating element 7 is further arranged on the reforming plate 3, a temperature thermocouple 8 is arranged on the middle partition plate 2, the snake-shaped straight micro-channel 6 is composed of a plurality of straight-line channel sections 601 which are sequentially connected end to end and are parallel to each other, a butyl cell 9 is arranged on the straight-line channel section 601, and hereinafter, the micro-channel of the type is simply called as a snake-shaped straight micro-channel 6 (DMD) with the butyl cell 9.
In this embodiment, on the basis of the serpentine straight micro-channel 6, the structure of the t cell 9 is additionally designed, and the t cell 9 is a protrusion and a recess which are regularly or irregularly arranged and sized and designed in the channel, compared with the straight micro-channel, the t cell 9 increases the heat exchange area, and the local boundary layer instability phenomenon of the fluid is caused by the formation of vortex and secondary flow, in addition, the special t cell 9 structure can also improve the heat exchange capability, but the resistance coefficient is only slightly increased or even reduced, as shown in fig. 5, the thermal mass transportation process of the micro-channel is enhanced, and the hydrogen production performance of the micro-channel reactor is further improved.
Referring to fig. 2, in particular, insertion holes penetrated by heating elements 7 such as industrial heating rods may be formed on the reforming plate 3, and heat generated by energizing the heating elements 7 may be conducted to the evaporation chamber 4 and the reforming chamber 5 through the reforming plate 3 and the middle partition plate 2, so as to provide a suitable reaction temperature for each process of the hydrogen production reaction; similarly, a jack for inserting the temperature thermocouple 8 can be arranged on the middle partition plate 2, and the reaction temperature can be measured through the temperature thermocouple 8 and fed back to the heating element 7 in real time. Of course, the heating element 7 may also be arranged on the evaporation plate 1 and/or the middle partition 2, and the temperature thermocouple 8 may also be arranged on the evaporation plate 1 and/or the reforming plate 3.
It can be understood that in practical design, a plurality of butyl cells 9 are uniformly arranged on each straight line runner section 601, the length x width x height of the evaporating plate 1 and the reforming plate 3 are 90mm x 10mm, the micro-runners are formed by carving continuous grooves on the evaporating plate 1 and the reforming plate 3, the length x width x depth of each straight line runner section 601 is 50mm x 1mm x 2mm, the distance between two adjacent straight line runner sections 601 is 1mm, 26 butyl cell 9 structural parameters are as follows: the radius x depth of the notch of each butyl cell 9 is 0.6mm x 0.2mm, 5 butyl cells 9 are equidistantly distributed on each straight line runner section 601, and the middle butyl cell 9 is positioned at the center of the straight line runner section 601, and the distance is 10mm. Specifically, the hydrogen production catalyst is coated on the micro-channel, and a copper-based catalyst or a copper-based oxygen carrier and other catalysts can be adopted.
Referring to fig. 4, in other embodiments, the evaporation chamber 4 and the reforming chamber 5 are each composed of a serpentine corrugated microchannel 10 (SM), the serpentine corrugated microchannel 10 being composed of a plurality of sinusoidal corrugated segments 101 connected end to end in sequence and parallel to each other. In this embodiment, on the basis of the serpentine straight micro-channel 6, sine waves are additionally designed: the sine ripple design converts the straight micro-channel into a ripple micro-channel; related researches show that compared with a straight micro-channel, cold and hot fluid in the sinusoidal micro-channel has extremely strong mixing effect, and the internal fluid of the sinusoidal micro-channel has unstable flow along with the formation of separation flow and oscillation flow; in summary, the special sine ripple structure can greatly improve the heat exchange capacity of the micro-channel, but the resistance coefficient is little increased, as shown in fig. 5, the thermal mass transportation process of the micro-channel is enhanced, and the hydrogen production performance (hydrogen atom utilization rate, hydrogen relative concentration and hydrogen yield) of the micro-channel reactor is further improved.
Referring to fig. 6, the simulation cloud chart of the section density and the temperature distribution of the corrugated micro-channel provided by the embodiment can be seen that the mechanism of sine corrugation enhanced heat and mass transfer can be summarized as follows: the special corrugated structure can enable the fluid to continuously change the flowing direction, directly conduct periodic mixing of the cooling fluid and the hot fluid, and particularly, the periodic transverse offset of the density and the temperature distribution is shown in fig. 6, so that the temperature distribution of the fluid is more uniform, the heat exchange temperature difference between the fluid and the constant temperature heating wall surface is increased, the heat exchange between the fluid and the constant temperature heating wall surface is further enhanced, but the friction between the fluid and the wall surface is increased, and the resistance coefficient is correspondingly increased. The cloud image in fig. 6 is taken from 5 different sections (i.e., 5 sections where the butyl cell may exist in the micro flow channel) on the same flow channel perpendicular to the flow direction, and is divided into x=0 mm, x=10 mm, x=20 mm, x=30 mm, and x=40 mm according to the flow direction and the position.
In a practical design, a plurality of butyl cells 9 may be provided on each sinusoidal wave segment 101 along the extending direction thereof, so as to form a serpentine wave micro-channel 10 (SMD) with the butyl cells 9. As shown in fig. 5, in this embodiment, by adding the t cell 9 structure into the serpentine corrugated micro-channel, even the drag reduction effect of the t cell 9 occurs, the heat exchange capability and the flow capability of the reactor can be simultaneously improved.
Referring to fig. 7, it can be seen from fig. 7 that vortex cores are mainly distributed at the inlet, outlet, corners and the butyl cells, i.e., in the micro-channel, these regions generate larger vorticity, belonging to the dense vorticity region. At the same time, this also means that there are a large number of secondary flows and vortices in these areas, so that the heat exchange is greatly enhanced and the drag coefficient is also increased.
Referring to fig. 8-11, the direction of gas flow in the inlet, outlet and corner regions is changed by 90 degrees, and the gas has a great scouring effect on the surrounding wall surfaces, so that the relative speed is greatly improved locally. And meanwhile, under the action of inertia, secondary flow or backflow can be generated in a local area, and the heat exchange intensity at the inlet, outlet and corner is higher than that at other places, so that a large number of vortex cores can be identified. In the case of the butyl cell structure, the formation of large vortex in the butyl cell structure can be directly observed in fig. 11, and the flow presents an irregular unstable form, which is also an embodiment of the mechanism of the butyl cell enhanced heat and mass transfer.
Specifically, sine ripple structural parameters: each sine wave section 101 has the width x depth of 1mm x 2mm, the waveform is a complete sine wave, the sine wave period is 50mm, the sine wave amplitude is 6.5% of the row period, the distance between two adjacent sine wave sections 101 is 1mm, 24 sine wave sections are 24 sine wave sections, and the structure parameters of the butyl cell 9 are as follows: the radius x depth of the notch of each butyl cell 9 is 0.8mm x 0.4mm, 3 butyl cells 9 are equidistantly distributed on each sine wave section 101, and the middle butyl cell 9 is positioned at the center of the sine wave section 101, and the distance is 15mm.
It can be understood that, in practical applications, the micro-channels of the evaporation chamber 4 and the reforming chamber 5 that constitute the alcohol reforming micro-reactor may be selected from any one of the serpentine straight micro-channel 6 (DMD) with the butyl cell 9, the serpentine corrugated micro-channel 10 (SM), and the serpentine corrugated micro-channel 10 (SMD) with the butyl cell 9, which are not described herein.
In the hydrogen production method using the alcohol reforming micro-reactor of the above embodiment, firstly, the aqueous methanol solution enters from the inlet of the evaporation chamber 4, absorbs heat while changing the flow in the corrugated micro-channel with the butyl cell 9, and evaporates to form mixed steam; then, the mixed steam enters a reforming chamber 5, alcohol reforming reaction is carried out in a straight micro-channel under the catalysis of a Cu/ZnO/Al2O3 catalyst, hydrogen is generated, the on-site hydrogen production of methanol steam reforming is realized, and the plates are sealed by high-temperature resistant fluorine rubber rings. By utilizing the relation of hydrogen production performance of the alcohol reforming micro-reactor provided by the embodiment, as shown in fig. 12, the reaction conditions are that the flow rate of N2, the reaction temperature, the S/C molar ratio, the feeding flow rate of methanol aqueous solution and the coating amount of Cu/ZnO/Al2O3 catalyst are respectively 10mL/min, 210 ℃, 1.2, 0.005mL/min and 0.200g, the micro-channels forming the evaporation chamber 4 are all in the form of DMD, the micro-channels forming the reforming chamber 5 are respectively in the form of DM, DMD, SM and SMD, no CO is generated in the experimental process, and as can be seen from fig. 12, the micro-channels forming the reforming chamber 5 are in the form of SMD, and the hydrogen production effect is the worst by adopting the conventional DM-type flow channel, which further proves that the reactor provided by the application has excellent hydrogen production effect.
Any of the above-described embodiments of the present application disclosed herein, unless otherwise stated, if they disclose a numerical range, then the disclosed numerical range is the preferred numerical range, as will be appreciated by those of skill in the art: the preferred numerical ranges are merely those of the many possible numerical values where technical effects are more pronounced or representative. Since the numerical values are more and cannot be exhausted, only a part of the numerical values are disclosed to illustrate the technical scheme of the application, and the numerical values listed above should not limit the protection scope of the application.
Meanwhile, if the above application discloses or relates to parts or structural members fixedly connected with each other, the fixed connection may be understood as follows unless otherwise stated: detachably fixed connection (e.g. using bolts or screws) can also be understood as: the non-detachable fixed connection (e.g. riveting, welding), of course, the mutual fixed connection may also be replaced by an integral structure (e.g. integrally formed using a casting process) (except for obviously being unable to use an integral forming process).
In addition, terms used in any of the above-described aspects of the present disclosure to express positional relationship or shape have meanings including a state or shape similar to, similar to or approaching thereto unless otherwise stated. Any part provided by the application can be assembled by a plurality of independent components, or can be manufactured by an integral forming process.
The above examples are only illustrative of the application and are not intended to be limiting of the embodiments. Other variations or modifications of the above teachings will be apparent to those of ordinary skill in the art. Nor is it necessary or impossible to exhaust all embodiments herein. And obvious variations or modifications thereof are contemplated as falling within the scope of the present application.
Claims (7)
1. An alcohol reforming microreactor is characterized in that: the device comprises an evaporation plate (1), a middle partition plate (2) and a reforming plate (3) which are sequentially overlapped from top to bottom, wherein an evaporation chamber (4) is formed between the evaporation plate (1) and the middle partition plate (2), and a reforming chamber (5) is formed between the middle partition plate (2) and the reforming plate (3);
the outlet of the evaporation chamber (4) is communicated with the inlet of the reforming chamber (5), a hydrogen production catalyst is loaded on the reforming chamber (5), a heating element (7) is further arranged on the evaporation plate (1), the middle partition plate (2) and/or the reforming plate (3), the evaporation chamber (4) is formed by a snake-shaped straight micro-channel (6) or a snake-shaped corrugated micro-channel (10), and the reforming chamber (5) is formed by the snake-shaped straight micro-channel (6) or the snake-shaped corrugated micro-channel (10); wherein, the liquid crystal display device comprises a liquid crystal display device,
the serpentine straight micro-channel (6) consists of a plurality of straight-line channel sections (601) which are connected end to end in sequence and are parallel to each other, the serpentine corrugated micro-channel (10) consists of a plurality of sine corrugated sections (101) which are connected end to end in sequence and are parallel to each other, and the straight-line channel sections (601) are provided with T cells (9);
a plurality of butyl cells (9) are uniformly arranged on each sine wave section (101).
2. The alcohol reforming microreactor of claim 1, wherein: a plurality of the butyl cells (9) are uniformly arranged on each straight line runner section (601).
3. The alcohol reforming microreactor according to claim 1 or 2, characterized in that: and a temperature thermocouple (8) is further arranged on the evaporation plate (1), the middle partition plate (2) and/or the reforming plate (3).
4. The alcohol reforming microreactor according to claim 1 or 2, characterized in that: the hydrogen production catalyst is coated on the micro-flow channel.
5. The alcohol reforming microreactor according to claim 1 or 2, characterized in that: the hydrogen production catalyst adopts a copper-based catalyst or a copper-based oxygen carrier.
6. A process for producing hydrogen using the alcohol reforming microreactor according to any one of claims 1 to 5, characterized in that: firstly, introducing alcohol substances into an evaporation chamber (4), and vaporizing in the evaporation chamber (4) under the action of a heat source provided by a heating element (7) to obtain mixed steam; subsequently, the mixed steam enters a reforming chamber (5); finally, alcohol steam reforming reaction occurs under the action of a catalyst, so that on-site hydrogen production is realized.
7. The method of producing hydrogen as claimed in claim 6, wherein: the alcohol is methanol, ethanol or glycerol.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110966066.6A CN113735059B (en) | 2021-08-23 | 2021-08-23 | Alcohol reforming micro-reactor and hydrogen production method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110966066.6A CN113735059B (en) | 2021-08-23 | 2021-08-23 | Alcohol reforming micro-reactor and hydrogen production method |
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