CN109694042B

CN109694042B - Reforming hydrogen production reactor, reforming furnace thereof and reforming hydrogen production reaction method

Info

Publication number: CN109694042B
Application number: CN201710987381.0A
Authority: CN
Inventors: 张旭; 戴文松
Original assignee: Sinopec Engineering Inc; Sinopec Engineering Group Co Ltd
Current assignee: Sinopec Engineering Inc; Sinopec Engineering Group Co Ltd
Priority date: 2017-10-20
Filing date: 2017-10-20
Publication date: 2021-03-05
Anticipated expiration: 2037-10-20
Also published as: CN109694042A

Abstract

The reforming hydrogen production reactor adopts a multistage catalytic reaction module containing a micro-catalytic reaction plate, and active components required by hydrogen production reaction are loaded on the reaction plate, so that the using amount of catalytic active metals is reduced, the catalyst is not easy to deposit carbon and inactivate, the distance from reaction gas to a catalytic active center is shortened, the mass transfer resistance and the pressure drop of the reactor are reduced, and the conversion rate of the hydrogen production reaction is improved; the reaction gas flows through the multistage catalytic reaction modules in sequence, can be fully contacted with the catalyst on the catalytic reaction plate, and can effectively improve the reaction conversion rate; the reforming hydrogen production reactor has wide application range, and can be suitable for different types of reforming furnaces as a furnace tube of a hydrogen production reforming furnace. The hydrogen production method adopting the reforming hydrogen production converter has the advantages of reduced furnace tube pressure, high space-time yield of the catalyst in unit volume in the furnace tube, high conversion rate of raw material gas treatment capacity, and capability of meeting the requirements of hydrogen production reaction.

Description

Reforming hydrogen production reactor, reforming furnace thereof and reforming hydrogen production reaction method

Technical Field

The disclosure relates to the field of hydrogen production by reforming, in particular to a hydrogen production by reforming reactor, a reformer thereof and a hydrogen production by reforming reaction method.

Background

Hydrogen is not only an important chemical raw material, but also a clean fuel. Hydrogen plays an increasingly important role in modern industries, especially the petrochemical industry, fuel cells and other national economy. Under the multiple pressure of the global crude oil with the trend of increasing the weight and the deterioration of crude oil, the increasing demand of people on the quantity of clean oil products, the increasing quality standard and the stricter environmental regulations, the demand on hydrogen is also increasing, and then the higher demand on a hydrogen production device is also provided.

The hydrogen production process mainly comprises a water electrolysis method, a light hydrocarbon steam conversion method, a partial oxidation method, a methanol cracking method and the like, and the light hydrocarbon steam conversion method is most widely applied at present. The raw material for hydrogen production by the light hydrocarbon steam reforming method mainly comprises carbon-containing light hydrocarbons such as natural gas, naphtha, refinery gas and the like. The conversion process comprises the following steps: the light hydrocarbons react with water vapor under certain temperature, pressure and catalyst action to generate hydrogen and carbon monoxide, and the carbon monoxide further generates hydrogen through water gas shift reaction, so that the yield of the target product of the light hydrocarbons is further improved.

The main chemical reactions that occur during the hydrogen production reaction are:

conversion reaction C_nH_m+n H₂O→n CO+(n+m/2)H₂△H＝206kJ/mol

Shift reaction of CO + H₂O→CO₂+H₂△H＝-36kJ/mol

The reforming reaction is a strong endothermic reaction, and in a traditional hydrogen production furnace, the reforming furnace tube filled with the reforming catalyst is heated to 900-1000 ℃ through fuel combustion to carry out the hydrogen production reaction. Common reforming hydrogen production active components comprise group V III transition elements such as Pt, Pd, Ir, Rh and the like, and the industrial application is limited due to the high price of the elements. Currently, the most widely used active component in the hydrogen production industry by reforming is nickel. The activity of the catalyst is directly related to the axial size of the specific surface of the catalyst, and relatively, the larger the specific surface is, the better the dispersion degree of the active components is, and the more the number of active centers is, so that the catalytic activity of the catalyst is improved.

The existing hydrogen production converter is filled with a nickel-based catalyst with a certain particle size and shape in a furnace tube, so that the uneven filling often occurs, the bias flow of raw material gas is caused, the conversion rate of the raw material is low, the catalyst is easy to deposit carbon and deactivate, and the operation period of the device is shortened. In addition, the catalyst with smaller particle size is filled in the furnace tube, although the filling amount of the catalyst can be increased, the number of active centers of the catalyst is increased, and the processing capacity and the conversion rate of the raw material are improved to a certain extent.

Disclosure of Invention

The purpose of the present disclosure is to provide a reforming hydrogen production reactor, a reformer thereof and a method of reforming hydrogen production reaction, the reforming hydrogen production reactor and the reformer employing the reforming hydrogen production reactor having reduced pressure, no gas bias flow and no short circuit phenomena; the hydrogen production method using the reforming hydrogen production converter has high conversion rate.

In order to achieve the above object, a first aspect of the present disclosure provides a reforming hydrogen production reactor, which includes a cylindrical sealed pressure-bearing shell, an air inlet, an air outlet, a first straight pipe extending from the top of the shell into the shell, a second straight pipe extending from the bottom of the shell into the shell, and a catalytic reaction zone disposed in the shell below the first straight pipe and above the second straight pipe; the air inlet is communicated with the first straight pipe, and the air outlet is communicated with the second straight pipe; the top and the bottom of the catalytic reaction zone are respectively sealed by a top sealing plate and a bottom sealing plate, the catalytic reaction zone comprises a plurality of cylindrical catalytic reaction modules which are coaxially overlapped, each catalytic reaction module comprises a central pipe, a catalytic reaction unit and an annular gap which are arranged from inside to outside, and the catalytic reaction units and the annular gaps of two adjacent catalytic reaction modules are separated by a sealing partition plate; the central pipe comprises a first central pipe and a second central pipe which are separated by an intermediate sealing plate, and the second central pipe of the previous catalytic reaction module is communicated with the first central pipe of the next catalytic reaction module; the catalytic reaction unit comprises a first catalytic reaction unit and a second catalytic reaction unit which are separated by the middle sealing plate; the side wall of the central pipe and the side wall of the catalytic reaction unit are respectively provided with an opening; a gas collecting cavity is formed between the bottom sealing plate and the inner wall of the lower part of the shell; the top end of the central pipe of the uppermost catalytic reaction module penetrates through the top sealing plate to be communicated with the first straight pipe, and the bottom end of the central pipe of the lowermost catalytic reaction module penetrates through the bottom sealing plate to be communicated with the gas collecting cavity; micro-catalytic reaction plates are respectively arranged in the first catalytic reaction unit and the second catalytic reaction unit, and reforming hydrogen production catalysts are loaded on the surfaces of the micro-catalytic reaction plates.

Optionally, the micro-catalytic reaction plates of the first catalytic reaction unit are radially distributed around the first central tube, the top end of the micro-catalytic reaction plate of the first catalytic reaction unit is hermetically connected with the top sealing plate or the sealing partition plate, and the bottom end of the micro-catalytic reaction plate of the first catalytic reaction unit is hermetically connected with the middle sealing plate; the micro-catalytic reaction plates of the second catalytic reaction unit are radially distributed around the second central pipe, the top ends of the micro-catalytic reaction plates of the second catalytic reaction unit are hermetically connected with the middle sealing plate, and the bottom ends of the micro-catalytic reaction plates of the second catalytic reaction unit are hermetically connected with the bottom sealing plate or the sealing partition plate.

Optionally, the micro-catalytic reaction plate extends axially and is spirally distributed around the first central tube or the second central tube, the top end of the micro-catalytic reaction plate of the first catalytic reaction unit is connected with the top sealing plate in a sealing manner or connected with the sealing partition plate in a sealing manner, and the bottom end of the micro-catalytic reaction plate of the first catalytic reaction unit is connected with the middle sealing plate in a sealing manner; the top end of the micro-catalytic reaction plate of the second catalytic reaction unit is hermetically connected with the middle sealing plate, and the bottom end of the micro-catalytic reaction plate of the second catalytic reaction unit is hermetically connected with the bottom sealing plate or the sealing partition plate.

Optionally, the micro-catalytic reaction plate is one or a plurality of annular plates arranged at intervals along the axial direction, the inner edge of the micro-catalytic reaction plate is fixedly connected with the outer side of the central pipe wall in a sealing manner, and the outer edge of the micro-catalytic reaction plate is fixedly connected with the inner side of the side wall of the catalytic reaction unit in a sealing manner.

Optionally, the micro-catalytic reaction plate is at least one selected from the group consisting of a flat plate, a toothed plate, a corrugated plate and a corrugated plate.

The second aspect of the present disclosure provides a reforming hydrogen production reformer, which includes an air inlet pipe, an air outlet pipe, a burner and a combustion chamber, and the reformer further includes the reforming hydrogen production reactor of the first aspect of the present disclosure, the reforming hydrogen production reactor is located in the combustion chamber, an air inlet of the reforming hydrogen production reactor is communicated with the air inlet pipe, and an air outlet of the reforming hydrogen production reactor is communicated with the air outlet pipe.

A third aspect of the present disclosure provides a method for performing a reforming hydrogen production reaction using the reforming hydrogen production converter of the second aspect of the present disclosure, the method comprising the steps of: (1) fuel gas and air are sprayed into the combustion chamber through the burner for combustion; (2) and enabling feed gas and steam to enter the reforming hydrogen production reactor through the air inlet pipe of the reformer, and carrying out reforming hydrogen production reaction in the catalytic reaction zone to obtain reformed gas rich in hydrogen.

Optionally, the conditions of the reforming hydrogen production reaction include: the reaction temperature is 700-1100 ℃, the reaction pressure is 1.8-5.5 MPaG, and H in the steam₂The molar ratio of O to carbon atoms in the raw material gas is (2.5-5): 1, the airspeed is 1000-100000 h^-1。

Optionally, the average flow velocity of the feed gas in the catalytic reaction zone is 0.5-85 m/s.

Optionally, the feed gas is at least one of natural gas, liquefied petroleum gas, refinery gas, a resolved gas of reformed hydrogen-enriched PSA, and naphtha; the reforming hydrogen production reaction catalyst comprises a reforming hydrogen production active component, and the reforming hydrogen production active component comprises at least one of nickel, ruthenium, platinum, palladium, iridium and rhodium.

Compared with the prior art, the invention has the beneficial effects that:

(1) the catalytic reaction zone of the reforming hydrogen production reactor comprises a multi-stage catalytic reaction module provided with a micro-catalytic reaction plate, catalytic active components for hydrogen production reaction are loaded on the reaction plate, the distance from the reaction gas to the catalytic active center through diffusion from a gas phase main body is shortened, and the mass transfer resistance (the diffusion resistance is almost zero) is greatly reduced.

(2) The reaction gas flows through the multistage catalytic reaction modules in sequence, can fully contact and react with the catalyst on the micro-catalytic reaction plate, and meanwhile, the generated product can be quickly diffused to the fluid main body, so that the retention time of the product in the reactor is short, and the conversion efficiency of the hydrogen production reaction and the space-time yield of the product of the catalyst in unit volume are fundamentally improved.

(3) Compared with the reforming hydrogen production reactor filled with particles, the micro-catalytic reaction plate is adopted, the total amount of active metal used by the reactor is obviously reduced, and the pressure drop is low. Under the condition of the same treatment scale, the reforming hydrogen production reactor and the reformer equipment formed by the reforming hydrogen production reactor have the advantages that the size is 5-30% smaller than that of the traditional reforming reactor, and the pressure drop is 3-55% lower.

(4) Compared with a reforming hydrogen production reactor filled with particles, the micro-catalytic reaction plate of the reforming hydrogen production reactor disclosed by the invention is not easy to deposit carbon and deactivate, the service life is long, the pressure is reduced, and the bed pressure drop is lower (15-90%) than that of a reactor with the same treatment capacity;

(5) the catalytic reaction zone is composed of micro-catalytic reaction plates, so that the number of active centers is increased, the uniformity of reaction gas in the catalytic reaction active centers is improved, the phenomena of reaction dead zones and gas bias flow are avoided, and the long-term stable operation of the hydrogen production reaction device can be fully ensured.

(6) The reforming hydrogen production reforming furnace tube can be suitable for reforming furnaces of different types, has wide application range, can achieve control and regulation production through an integration mode with functionalized catalytic reaction modules and increase and decrease of the number according to actual industrial production requirements, is beneficial to realizing the maximum utilization efficiency of equipment, has no obvious amplification effect, shortens the processing time of the equipment and further reduces the production cost of a reactor.

Additional features and advantages of the disclosure will be set forth in the detailed description which follows.

Drawings

The accompanying drawings, which are included to provide a further understanding of the disclosure and are incorporated in and constitute a part of this specification, illustrate embodiments of the disclosure and together with the description serve to explain the disclosure without limiting the disclosure. In the drawings:

FIG. 1 is a schematic diagram of the structure of one embodiment of a reforming hydrogen production reactor of the present disclosure;

figure 2 is a cross-sectional view of one embodiment of a reforming hydrogen production reactor of the present disclosure (i.e., a cross-sectional view on the a-a plane of figure 1);

fig. 3 is a schematic structural diagram of a catalytic reaction module of an embodiment of the reforming hydrogen production reactor of the present disclosure (i.e., a schematic structural diagram of catalytic reaction module 13 in fig. 1);

FIG. 4 is a schematic structural diagram of a second embodiment of a reforming hydrogen production reactor of the present disclosure;

fig. 5 is a schematic structural diagram of a third embodiment of a reforming hydrogen production reactor of the present disclosure;

fig. 6 is a schematic structural view of a catalytic reaction module of a third embodiment of a reforming hydrogen production reactor of the present disclosure (i.e., a schematic structural view of catalytic reaction module 13 in fig. 5);

fig. 7 is a schematic structural diagram of a fourth embodiment of a reforming hydrogen production reactor of the present disclosure;

FIG. 8 is a schematic structural view of a toothed micro-catalytic reaction plate of one embodiment of the reforming hydrogen production reactor of the present disclosure;

FIG. 9 is a schematic structural view of a corrugated micro-catalytic reaction plate of one embodiment of the reforming hydrogen production reactor of the present disclosure;

FIG. 10 is a schematic structural view of a corrugated micro-catalytic reaction plate of one embodiment of a reforming hydrogen production reactor of the present disclosure;

FIG. 11 is a schematic structural view of an embodiment of a reformer for reforming hydrogen production according to the present disclosure;

FIG. 12 is a schematic block diagram of another embodiment of a reformer for reforming hydrogen production according to the present disclosure;

figure 13 is a schematic center tube view of one embodiment of a reforming hydrogen production reactor of the present disclosure;

figure 14 is a schematic center cylinder view of another embodiment of a reforming hydrogen production reactor of the present disclosure.

Description of the reference numerals

1 air inlet and 2 air outlet

3 upper end socket and 4 lower end socket

5 top seal plate 6 center tube

7 annular gap 8 bottom sealing plate

9 gas-collecting cavity 10 micro-catalytic reaction plate

11 first straight pipe 12 shell

13 catalytic reaction module 13a first catalytic reaction unit

13b second catalytic reaction unit 14 second straight tube

15 intermediate seal plate

20 reforming hydrogen production reformer and 21 reforming hydrogen production reactor

22 combustion chamber 23 burner

24 to the inlet and 25 to the outlet.

Detailed Description

The following detailed description of specific embodiments of the present disclosure is provided in connection with the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present disclosure, are given by way of illustration and explanation only, not limitation.

In the present disclosure, unless otherwise specified, use of directional words such as "upper, lower, top, bottom" generally refers to upper and lower, top and bottom of the device in normal use, and specifically refers to the orientation of the drawing in fig. 1. The "inner and outer" are with respect to the outline of the device itself. Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present disclosure, "a plurality" means two or more unless specifically limited otherwise.

As shown in fig. 1, a first aspect of the present disclosure provides a reforming hydrogen production reactor, which includes a cylindrical sealed pressure-bearing shell 12, an air inlet 1, an air outlet 2, a first straight pipe 11 extending from the top of the shell 12 into the shell, a second straight pipe 14 extending from the bottom of the shell 12 into the shell, and a catalytic reaction zone disposed in the shell 12 below the first straight pipe 11 and above the second straight pipe 14; the air inlet is communicated with the first straight pipe 11, and the air outlet 2 is communicated with the second straight pipe 14; the top and the bottom of the catalytic reaction zone are respectively sealed by a top sealing plate 5 and a bottom sealing plate 8, the catalytic reaction zone comprises a plurality of cylindrical catalytic reaction modules 13 which are coaxially overlapped, the catalytic reaction modules 13 comprise a central pipe 6, catalytic reaction units and annular gaps 7 which are arranged from inside to outside, and the catalytic reaction units and the annular gaps 7 of two adjacent catalytic reaction modules 13 are separated by a sealing partition plate; the central pipe 6 comprises a first central pipe and a second central pipe which are separated by an intermediate sealing plate 15, and the second central pipe of the previous catalytic reaction module 13 is communicated with the first central pipe of the next catalytic reaction module 13; the catalytic reaction unit comprises a first catalytic reaction unit 13a and a second catalytic reaction unit 13b separated by an intermediate sealing plate 15; the side wall of the central pipe and the side wall of the catalytic reaction unit are respectively provided with an opening; a gas collecting cavity 9 is formed between the bottom sealing plate 8 and the inner wall of the lower part of the shell 12; the top end of the central pipe of the uppermost catalytic reaction module 13 passes through the top sealing plate 5 to be communicated with the first straight pipe 11, and the bottom end of the central pipe of the lowermost catalytic reaction module 13 passes through the bottom sealing plate 8 to be communicated with the gas collection cavity 9; the first catalytic reaction unit 13a and the second catalytic reaction unit 13b are respectively provided with a micro-catalytic reaction plate 10, and the plate surface of the micro-catalytic reaction plate 10 is loaded with a reforming hydrogen production catalyst.

Wherein, the "upper one" and the "lower one" refer to that in two adjacent catalytic reaction modules in the plurality of catalytic reaction modules which are sequentially stacked along the axial direction, one of the two adjacent catalytic reaction modules which is close to the top of the reactor is the "upper one", and the other one of the two adjacent catalytic reaction modules which is close to the bottom of the reactor is the "lower one"; similarly, "uppermost" and "lowermost" refer to the reaction modules of the plurality of catalytic reaction modules that are closest to the top and bottom of the reactor, respectively.

The reforming hydrogen production reactor disclosed by the invention adopts the multistage catalytic reaction module containing the micro-catalytic reaction plate, and the reforming hydrogen production catalyst required by hydrogen production reaction is loaded on the reaction plate, so that the using amount of catalytic active metal is reduced, the catalyst is not easy to deposit carbon and deactivate, the distance from reaction gas to a catalytic activity center is shortened, the mass transfer resistance and the pressure drop of the reactor are reduced, and the conversion rate of the hydrogen production reaction is improved; the reaction gas flows through the multistage catalytic reaction modules in sequence, can be fully contacted with the catalyst on the catalytic reaction plate, and can effectively improve the reaction conversion rate; the reforming hydrogen production reactor has wide application range, and can be suitable for different types of reforming furnaces as a furnace tube of a hydrogen production reforming furnace.

The reforming hydrogen production reactor referred to in the present disclosure is also generally referred to as hydrogen production reformer tube or reformer tube in industrial production, and the above three designations represent the same device unless otherwise specified. According to the present disclosure, the micro-catalytic reaction plate may have a reforming hydrogen production catalyst supported on an optional plate surface, or may have reforming hydrogen production catalysts supported on both plate surfaces of the micro-catalytic reaction plate, preferably, the micro-catalytic reaction plate has catalysts supported on both plate surfaces, so as to further improve the conversion rate of the hydrogen production reaction performed by the reactor. The reforming hydrogen production catalyst may employ a catalytically active component well known to those skilled in the art, for example, the supported active component may be a metal such as nickel, ruthenium, platinum, palladium, iridium, and rhodium, which has a reforming hydrogen production reaction activity; the loading means that the catalyst containing the active component can be loaded on the micro-catalytic reaction plate by a method of dipping, ion sputtering, coating or filling, and the like, or the active component can be directly loaded on the micro-catalytic reaction plate. Among them, the active metal component coating and supporting process may employ a coating method including two stages of pretreatment of a metal substrate and catalyst deposition, which are well known to those skilled in the art.

According to the present disclosure, one or more micro catalytic reaction plates 10 may be included in the catalytic reaction module 13, and a plurality of micro catalytic reaction plates 10 may be arranged in the catalytic reaction module 13 in a conventional manner in the art, as long as it is ensured that the reaction feed gas respectively moves radially from the center to the periphery in the catalytic reaction module 13. The micro-catalytic reaction plates 10 can be axially arranged or radially arranged along the reactor, or the extending direction of the micro-catalytic reaction plates 10 and the horizontal direction form an included angle theta, the theta can be in the range of 0-90 degrees, preferably the theta is 30-90 degrees, the included angles of a plurality of micro-catalytic reaction plates 10 can be the same or different, preferably the same, and the inclined directions of two adjacent micro-catalytic reaction plates 10 can be the same or different.

In order to further reduce the pressure drop of the reactor and adapt to the increase of the volume of the hydrogen production reaction, in an embodiment of the present disclosure, as shown in fig. 2 and 3, the micro-catalytic reaction plates 10 of the first catalytic reaction unit 13a may be radially distributed around the first central tube, the top end of the micro-catalytic reaction plate 10 of the first catalytic reaction unit 13a may be hermetically connected to the top sealing plate 5 or the sealing partition plate, and the bottom end of the micro-catalytic reaction plate 10 of the first catalytic reaction unit 13a may be hermetically connected to the middle sealing plate 15; the micro-catalytic reaction plates 10 of the second catalytic reaction unit 13b may be radially distributed around the second central tube, the top end of the micro-catalytic reaction plate 10 of the second catalytic reaction unit 13b may be hermetically connected to the middle sealing plate 15, and the bottom end of the micro-catalytic reaction plate 10 of the second catalytic reaction unit 13b may be hermetically connected to the bottom sealing plate 8 or to the sealing partition plate; at this time, the included angle θ between the micro catalytic reaction plates 10 in the first catalytic reaction unit 13a and the second catalytic reaction unit 13b and the horizontal direction may be 0 ° to 90 °, and when the included angle between the micro catalytic reaction plates 10 and the horizontal direction is not 0 ° or 90 °, the inclination direction of the micro catalytic reaction plates 10 is not limited, the included angle θ is preferably 30 ° to 90 °, and the included angles of the plurality of micro catalytic reaction plates 10 may be the same or different, preferably the same; the inclination directions of two adjacent micro-catalytic reaction plates 10 may be the same or different, and preferably, the inclination directions of two adjacent micro-catalytic reaction plates 10 are different, that is, the top ends and the bottom ends of two adjacent micro-catalytic reaction plates 10 are respectively sealed in an overlapping manner.

In another embodiment of the present disclosure, the micro-catalytic reaction plate 10 may extend axially and spirally distributed around the first central tube or the second central tube, the top end of the micro-catalytic reaction plate 10 of the first catalytic reaction unit 13a may be connected with the top sealing plate 5 in a sealing manner or connected with the sealing partition plate in a sealing manner, and the bottom end of the micro-catalytic reaction plate 10 of the first catalytic reaction unit 13a may be connected with the middle sealing plate 15 in a sealing manner; the top end of the micro catalytic reaction plate 10 of the second catalytic reaction unit 13b may be hermetically connected to the middle sealing plate 15, and the bottom end of the micro catalytic reaction plate 10 of the second catalytic reaction unit 13b may be hermetically connected to the bottom sealing plate 8 or the sealing partition plate.

In the third embodiment of the present disclosure, the micro-catalytic reaction plate 10 may be one or a plurality of annular plates arranged at intervals along the axial direction, the inner edge of the micro-catalytic reaction plate 10 may be fixedly connected with the outer side of the pipe wall of the central pipe 6 in a sealing manner, and the outer edge of the micro-catalytic reaction plate 10 may be fixedly connected with the inner side of the side wall of the catalytic reaction unit in a sealing manner. The included angle theta between the annular micro-catalytic reaction plate 10 and the horizontal direction is preferably 0-60 deg., and in this case, the annular micro-catalytic reaction plate 10 preferably extends in the radial direction, i.e. the included angle theta is 0 deg..

According to the present disclosure, the use of a micro-catalytic reaction plate loaded with a reforming hydrogen production catalyst in a reforming hydrogen production reactor can reduce the amount of catalytic active metals, reduce the size of the reactor, and reduce the pressure drop of the reactor, wherein the micro-catalytic reaction plate can be of a conventional type in the art. In order to further increase the number of catalytically active centers in the reactor, preferably, the micro catalytic reaction plate may be at least one selected from the group consisting of a flat plate, a toothed plate, a corrugated plate and a corrugated plate, as shown in fig. 3, 8, 9 and 10, and more preferably, at least one selected from the group consisting of a toothed plate (fig. 8), a corrugated plate (fig. 9) and a corrugated plate (fig. 10). The structures and the sizes of the toothed plate, the corrugated plate and the corrugated plate are not limited, and the requirements of loading active components and hydrogen production process conditions are met. In order to increase the number of micro catalytic reaction plates filled in the catalytic reaction module, the same type of micro catalytic reaction plates are preferred in the reactor. Furthermore, in order to facilitate production and installation of the micro-catalytic reaction plates and uniformly distribute the feed gas, the size, type, density degree and the like of the tooth-shaped waveform of each micro-catalytic reaction plate are completely consistent, and the invention does not specifically limit the size, type and density degree of the tooth-shaped waveform, and only needs to meet the process conditions of the hydrogen production reaction.

According to the present disclosure, in order to prolong the service life of the micro reaction plate, the central tube 6 and the micro catalytic reaction plate 10 may be made of metal or ceramic, preferably metal that does not react with the gas in the reaction system.

According to the present disclosure, the reforming hydrogen production reactor may include one or more catalytic reaction modules 13, and under the same reaction conditions and reactor diameter, increasing the number of catalytic reaction modules 13 may increase the contact time of the reaction gas and the catalyst, improve the conversion rate, and adjust the number of catalytic reaction modules 13 according to the actual reaction conditions. The number of the catalytic reaction modules 13 in the present disclosure may be 2 to 3000, preferably 5 to 1000. Further, the catalytic reaction modules 13 may be arranged in series and/or in parallel in the axial direction of the reactor and/or in the radial direction of the reactor, depending on the specific actual process requirements. In order to uniformly distribute the raw material mixture in the catalytic reaction zone, the catalytic reaction module 13 and the housing 12 may be arranged coaxially.

According to the present disclosure, the central tube 6 may have an open pore structure, the open pore form may be a circular pore type as shown in fig. 14 or a groove type as shown in fig. 13, and the shape of the open pore, the size of the open pore, and the number of open pores (open pore ratio) are not limited in the present invention as long as the reforming hydrogen production process conditions are satisfied.

According to the present disclosure, the material adopted by the shell, the upper end enclosure and the lower end enclosure of the reforming hydrogen production reactor can be the same as the material selected by the conventional reforming hydrogen production furnace tube, for example: HP-40Nb, reforming reactor shell materials are well known to those skilled in the art and the present invention is not described in detail herein. The specific dimensions of the reforming hydrogen production reactor may also vary over a wide range. Further, in order to adapt to the scale of a newly-built hydrogen production converter device or the transformation and upgrade of the existing hydrogen production converter device, the inner diameter of the reforming hydrogen production reactor can be 30-1000 mm, and preferably 50-300 mm; the length of the catalytic reaction unit in the reactor can be 1000 mm-30000 mm, preferably 2000 mm-15000 mm.

As shown in fig. 1-3, the flow regime of the reaction feed gas in the reforming hydrogen production reactor of the present disclosure may include: the reaction raw gas enters a first catalytic reaction module 13 from the gas inlet 1 of the reactor to the top through a first straight pipe 11, flows into a first catalytic reaction unit 13a from the outside in the radial direction through a pipe wall opening of a first central pipe of the module and flows from the outside in the radial direction, the reaction raw gas reacts at the active center of the catalyst loaded on the surface of the micro-catalytic reaction plate 10 while flowing from the outside, the reactant flow flows from the outside to the side wall of the first catalytic reaction unit 13a to enter the annular gap 7, flows downwards in the annular gap 7 and enters a second catalytic reaction unit 13b through a side wall opening and flows from the inside in the radial direction, the raw gas reacts on the catalyst loaded on the surface of the micro-catalytic reaction plate 10 at the same time, the raw gas flows into a second central pipe from the inside through the opening, flows downwards into a first central pipe of the next catalytic reaction module after being buffered, the flowing mode in the second catalytic reaction module and the subsequent catalytic reaction module is the same as that in the, the reactant flow flowing out of the second central tube of the last catalytic reaction module positioned at the lowest part enters the gas collection cavity 9 and leaves the reforming hydrogen production reactor through the second straight tube 14 and the gas outlet 2.

As shown in fig. 11 and 12, a second aspect of the present disclosure provides a reforming hydrogen production reformer, which includes an air inlet pipe 24, an air outlet pipe 25, a burner 23, and a combustion chamber 22, and the reformer further includes a reforming hydrogen production reactor 21 of the first aspect of the present disclosure, the reforming hydrogen production reactor 21 is located in the combustion chamber 22, an air inlet 1 of the reforming hydrogen production reactor 21 is communicated with the air inlet pipe 24, and an air outlet 2 of the reforming hydrogen production reactor is communicated with the air outlet pipe 25.

The reforming hydrogen production reformer according to the present disclosure may be of a type conventional in the art, and for example, may be at least one of a top-fired furnace, a side-fired furnace, a bottom-fired furnace, and a trapezoidal furnace, preferably a top-fired furnace as shown in fig. 11 and/or a side-fired furnace as shown in fig. 12. The types of the burner and the fuel in the reformer are not particularly limited as long as the energy required by hydrogen production by reforming can be satisfied. In addition, the number, arrangement mode and the like of the reactors arranged between the gas inlet pipe and the gas outlet pipe of the reforming furnace are not particularly limited, and the reforming hydrogen production process can meet the requirements of the reforming hydrogen production process.

The reforming hydrogen production reformer disclosed by the invention has the advantages that the pressure of the furnace tube of the reforming hydrogen production reformer is reduced, the space-time yield of the catalyst in unit volume in the furnace tube is high, the overall size of the reformer is small, and the equipment investment and energy consumption are reduced.

A third aspect of the present disclosure provides a method for performing a reforming hydrogen production reaction using the reforming hydrogen production converter of the second aspect of the present disclosure, the method comprising the steps of: (1) fuel gas and air are sprayed into the combustion chamber through the burner for combustion; (2) the raw material gas and the steam enter a reforming hydrogen production reactor through an air inlet pipe of a reformer, and the reforming hydrogen production reaction is carried out in a catalytic reaction zone to obtain reformed gas rich in hydrogen.

The reforming hydrogen production reaction method disclosed by the invention has the advantages that the internal pressure of the reforming furnace tube is reduced, the conversion rate of the raw material gas is high, and the hydrogen production reaction requirement can be met.

In the reforming hydrogen production reaction method disclosed by the disclosure, the conditions of the reforming hydrogen production reaction can be changed within a large range, and preferably, the reaction temperature in the reforming hydrogen production reactor can be 700-1100 ℃, and preferably 800-950 ℃; the reaction pressure may be 1.8-5.5 MPaG, preferably 1.8-3.5 MPaG, water vapor H₂The ratio of O to carbon in the feed gas may be conventional in the art, e.g. H in steam₂The molar ratio of O to carbon atoms in the feed gas can be (2.5-5): 1, preferably (2.5-4): 1. the reforming hydrogen production reaction of the present disclosure has a higher conversion rate under the above preferred reaction conditions.

Further, in order to improve the conversion rate of the raw material gas, the space velocity of the raw material gas can be 1000-100000 h^-1More preferably 3000 to 90000h^-1Most preferably 8000-70000 h^-1。

In order to improve the conversion rate of the raw material gas, the average flow velocity of the raw material gas in the catalytic reaction zone can be 0.5-85 m/s, preferably 0.8-55 m/s, more preferably 1.0-45 m/s, and further, the average flow velocity of the raw material gas passing through two adjacent micro-catalytic reaction plates can be 0.5-85 m/s, preferably 0.8-55 m/s, more preferably 1.0-45 m/s.

In the reforming hydrogen production reaction method according to the present disclosure, the reaction raw material gas may be at least one of natural gas, liquefied petroleum gas, refinery gas, a resolved gas of reforming hydrogen concentration PSA, and naphtha. Furthermore, the natural gas mainly becomes methane, contains a small amount of micromolecular hydrocarbons such as ethane and the like, carbon dioxide, nitrogen and the like, has low sulfur content, mainly comprises hydrogen sulfide, mercaptan, hydroxyl sulfur and the like, and can be easily removed through simple hydrotreatment; refinery gas mainly refers to non-condensable gas, catalytic dry gas, coking dry gas, hydrogenation dry gas, reforming dry gas and the like of a crude oil distillation unit; the main components of the liquefied petroleum gas are propane, propylene, butane and butylene, can be a mixture of one or more of the above hydrocarbons, and contains a small amount of pentane, pentene and trace sulfide impurities, wherein carbonyl sulfide is removed by an alcohol amine absorption tower, and sulfides are removed by an alkali washing method; the desorption gas of the reformed hydrogen-enriched PSA contains about a large amount of hydrogen and some small-molecule hydrocarbons; the preferred order of naphtha is: straight-run light naphtha (reforming topped oil) with a dry point of 70 ℃, refinery narrow-cut reforming raffinate oil, full-cut straight-run gasoline with a dry point of 146 ℃ and single-pass hydrocracked naphtha.

In the reforming hydrogen production reaction method according to the present disclosure, the steam may refer to medium-pressure steam, the temperature of the medium-pressure steam may be about 420 ℃, the pressure of the medium-pressure steam may be about 3.5Mpa, and the temperature and the pressure of the medium-pressure steam may fluctuate in the actual gas distribution process.

In the reforming hydrogen production reaction method according to the present disclosure, the reforming hydrogen production reaction catalyst may be of a type conventional in the art, for example, the reforming hydrogen production reaction catalyst may include a reforming hydrogen production active component, and the reforming hydrogen production active component may include at least one of nickel, ruthenium, platinum, palladium, iridium, and rhodium.

The invention will be further illustrated by way of example with reference to the accompanying drawings, without the disclosure being limited thereto in any way.

Example 1

As shown in fig. 1, fig. 2, and fig. 3, the reforming hydrogen production reactor adopted in this embodiment includes a pressure-bearing housing 12 having a first straight pipe 11 at an upper end and a second straight pipe 14 at a lower end, fifty catalytic reaction modules 13 (not all shown in the figures) including a central pipe 6 are disposed in the housing, a sealing partition plate extending in a radial direction is disposed between two adjacent catalytic reaction modules 13, an edge of the sealing partition plate is connected with an inner wall of the housing in a sealing manner, an air inlet 1 is disposed on an upper portion of the first straight pipe 11, and an air outlet 2 is disposed on a lower portion of the second straight pipe. The catalytic reaction module 13 comprises a catalytic reaction unit, the catalytic reaction unit is composed of a first catalytic reaction unit 13a and a second catalytic reaction unit 13b, an intermediate sealing plate 15 is arranged between the first catalytic reaction unit 13a and the second catalytic reaction unit 13b, the edge of the intermediate sealing plate 15 is hermetically connected with the side wall of the catalytic reaction unit, a planar catalytic reaction plate is arranged in the catalytic reaction unit, the planar plates are radially distributed around a central pipe, the included angle between the planar plate and the horizontal direction is 80 degrees, the inclination directions of two adjacent planar micro catalytic reaction plates are opposite so that the top end and the bottom end of the two adjacent planar micro catalytic reaction plates are respectively overlapped in a sealing manner, and the central pipe 6 and the shell 12 are coaxially arranged; the upper edge of the micro-catalytic reaction plate 10 of the first catalytic reaction unit 13a is hermetically connected with the top sealing plate 5 or the sealing partition plate, and the lower edge of the micro-catalytic reaction plate 10 of the first catalytic reaction unit 13a is hermetically connected with the middle sealing plate 15; the upper edge of the micro-catalytic reaction plate 10 of the second catalytic reaction unit 13b is hermetically connected with the middle sealing plate 15, and the lower edge of the micro-catalytic reaction plate 10 of the second catalytic reaction unit 13b is hermetically connected with the bottom sealing plate 8 or the sealing partition plate; the two sides of the micro-catalytic reaction plate 10 are loaded with a catalytic active component NiO required by the reforming hydrogen production reaction.

The inner diameter of the reforming hydrogen production reactor is 110mm, the tangent length is 12000mm, the inner diameter of the central tube is 30mm, the height of the catalytic reaction module 13 is 200mm, the total height of the catalytic reaction zone is 10000mm, the central tube adopts a circular opening, and the aperture is 110mm

The holes are uniformly opened, the opening rate is 17.5 percent, the average distance between two adjacent micro-catalytic reaction plates is 3mm, the annular space distance is 3mm, and the average flow speed between the micro-catalytic reaction plates is 9.46 m/s.

The material of the reactor shell adopts HP40-Nb (containing elements such as Cr, Ni, Nb, W, Mo and Ti), and the micro-catalytic reaction plate 10 adopts Fe-Cr-Al/Al₂O₃The material is a catalytic loading substrate and is a plane substrate, and the loading active metal on the two sides of the substrate is NiO, and the content is 13.5%.

As shown in fig. 11, the reforming hydrogen production converter of this embodiment includes the reforming hydrogen production reactor 21, an air inlet pipe 24, an air outlet pipe 25, a burner 23, and a combustion chamber 22, where the reforming hydrogen production reactor 21 is located in the combustion chamber 22, an air inlet 1 of the reforming hydrogen production reactor 21 is communicated with the air inlet pipe 24, and an air outlet 2 of the reforming hydrogen production reactor is communicated with the air outlet pipe 25.

The reforming hydrogen production reactor and the reformer of the embodiment are applied to the natural gas steam reforming hydrogen production reaction, and the main steps comprise:

1) fuel gas and air are sprayed into a combustion chamber 22 through a burner 23 of the reformer, the fuel is combusted in the combustion chamber of the reformer to provide heat required by hydrogen production reaction, and the temperature of the reactor is 950 ℃;

2) by mixing water vapor with CH₄The mixed gas with the molar ratio of 2.8 (the temperature is 500 ℃, the pressure is 3.2MPaG), the flow rate is 20kmol/h, and the space velocity is 28160h^-1The fully mixed gas enters the air inlet pipe of the converter, enters the micro catalytic reaction plate through the first straight pipe 11 and the central pipe 6 of the reactor to carry out reforming hydrogen production reaction, and the reacted converted gas leaves the reactor through the central pipe 6, the gas collection cavity 9 and the second straight pipe 14 of the bottom catalytic reaction unit, enters the air outlet pipe 25 of the converter and is discharged to the outside of the converter. The detection proves that the outlet methane content (without water vapor) is 0.065%.

A comparison of the reforming hydrogen production reactor of this example with a prior art hydrogen production reactor of the same reactor size and the same catalytic reaction unit size is given in table 1. Pressure drop from reactor bed, CH₄As can be seen from the three indexes of conversion rate and space velocity, the reactor of the embodiment shows excellent performance, and particularly has the advantages of reducing the pressure drop of the reactor and improving the space velocity of the reactor.

Table 1 the reforming reactor of this example is compared to a conventional hydrogen production reactor

Reactor type	Pressure drop, MPa	CH₄Conversion/(%))	Space velocity, h^-1
				Conventional reactor	0.33	95	3400
Reactor of this example	0.1	≥96	28160

Example 2

As shown in fig. 2, fig. 4 and fig. 9, the reforming hydrogen production reactor and the reformer of this example have the same size, the distance between two adjacent catalytic reaction plates, the annular space distance, the matrix material of the micro-reaction plate and the loading parameters of the active component NiO per unit area as those of example 1. The difference from example 1 is that the micro-catalytic reaction plate in this example is a corrugated micro-reaction plate.

The reactor and the reformer of the embodiment are applied to the hydrogen production reaction by natural gas steam reforming in the same way. The hydrogen production process conditions were the same as in example 1, and it was determined that the outlet methane content (containing no water vapor) was 0.06%.

A comparison of the reforming hydrogen production reactor of this example with a prior art hydrogen production reactor of the same reactor size and the same catalytic reaction unit size is given in table 2. Pressure drop from reactor bed, CH₄As can be seen from the three indexes of conversion rate and space velocity, the reactor of the embodiment shows excellent performance, and particularly has the advantages of reducing the pressure drop of the reactor and improving the space velocity of the reactor.

Table 2 the reforming reactor of this example is compared to a conventional hydrogen production reactor

Reactor type	Pressure drop, MPa	CH₄Conversion/(%)	Space velocity, h^-1
				Conventional reactor	0.33	95	3400
Reactor of this example	0.095	≥96.5	28160

Example 3

As shown in fig. 5, 6 and 8, the reactor of this example has the same size, the same distance between two adjacent catalytic reaction plates, the same annular space distance, the same matrix material of the micro reaction plate and the same loading parameters of the active component NiO per unit area as those of example 1. The difference from the embodiment 1 is that the micro-catalytic reaction plate in this embodiment is a toothed micro-reaction plate, the toothed plate extends along the axial direction and is uniformly distributed in a radial shape around the central tube, and the wave-shaped direction is along the axial direction of the reactor. For the castellated plate, the distance between the wave crest and the wave trough is 4mm, and the distance between two adjacent wave crests or adjacent wave troughs of the same micro-plate is 6.5 mm.

The reactor and the reformer of the embodiment are applied to the hydrogen production reaction by natural gas steam reforming in the same way. The hydrogen production process conditions were the same as in example 1, and it was determined that the outlet methane content (containing no water vapor) was 0.05%.

A comparison of the reforming hydrogen production reactor of this example with a prior art hydrogen production reactor of the same reactor size and the same catalytic reaction unit size is given in table 3. Pressure drop from reactor bed, CH₄As can be seen from the three indexes of conversion rate and space velocity, the reactor of the embodiment shows excellent performance, and particularly has the advantages of reducing the pressure drop of the reactor and improving the space velocity of the reactor.

Table 3 comparison of reforming reactor of this example with conventional hydrogen production reactor

Reactor type	Pressure drop, MPa	CH₄Conversion/(%)	Space velocity, h^-1
				Conventional reactor	0.33	95	3400
Reactor of this example	0.09	≥99	28160

Example 4

As shown in fig. 7 and 9, the reactor, hydrogen production process conditions, and the like of this example were the same as those of example 3. The difference from example 3 is that the micro catalytic reaction plate in this example is a corrugated plate.

A comparison of the reforming hydrogen production reactor of this example with a prior art hydrogen production reactor of the same reactor size and the same catalytic reaction unit size is given in table 4. Pressure drop from reactor bed, CH₄As can be seen from the three indexes of conversion rate and space velocity, the reactor of the embodiment shows excellent performance, and particularly has the advantages of reducing the pressure drop of the reactor and improving the space velocity of the reactor.

Table 4 the reforming reactor of this example is compared to a conventional hydrogen production reactor

Reactor type	Pressure drop, MPa	CH₄Conversion/(%)	Space velocity, h^-1
				Conventional reactor	0.33	95	3400
Reactor of this example	0.09	≥99.2	28160

Example 5

As shown in fig. 1 and 2, the reforming hydrogen production reactor and the reformer of the present example are the same as those of example 1. The difference from example 1 is that this example uses a reformed hydrogen-enriched PSA stripping gas as a reaction raw material, and the stripping gas composition is shown in table 5. The fuel is combusted in the combustion chamber of the reformer to provide the heat required for the hydrogen production reaction, with a reactor temperature of 930 ℃. Steam and CH₄The mixed gas (temperature 500 ℃, pressure 3MPaG) with the molar ratio of 2.85 has the flow rate of 25kmol/h and the space velocity of 35200h^-1The fully mixed gas enters the air inlet pipe of the converter, enters the catalytic reaction zone through the first straight pipe 11 of the reactor and the central pipe 6 of the top micro-catalytic reaction unit to carry out reforming hydrogen production reaction, and the reacted converted gas leaves the reactor through the central pipe 6 of the lowest catalytic reaction module, the gas collection cavity 9 and the second straight pipe 14, enters the air outlet pipe of the converter and is discharged to the outside of the converter. The detection proves that the outlet methane content (without water vapor) is 0.3 percent.

Using the reactor provided in example 1, the reaction raw materials and process conditions were different from those of the example, and the reaction results obtained were compared with those obtained in a conventional reactor under the same reaction raw materials and process conditions, as shown in Table 6. Pressure drop from reactor bed, CH₄As can be seen from the three indexes of conversion rate and space velocity, the reactor of the embodiment shows excellent performance, and particularly has the advantages of reducing the pressure drop of the reactor and improving the space velocity of the reactor.

TABLE 5 reformate hydrogen enrichment PSA desorption gas composition

Table 6 comparison of reforming reactor of this example with conventional hydrogen production reactor

Reactor type	Pressure drop, MPa	CH₄Conversion/(%)	Space velocity, h^-1
				Conventional reactor	0.38	97	4400
Reactor of this example	0.12	≥98	35200

The reforming hydrogen production reactor and the reformer provided by the disclosure have compact structures and low active metal consumption; when the reactor is used for reforming hydrogen production reaction, the pressure drop of a bed layer is small, the production intensity of a catalyst in unit volume is high, the diffusion path of reactants is short, the conversion rate of raw materials is high, and the reactor has no phenomena of gas bias flow and short circuit, and can meet the requirement of the existing production process of reforming hydrogen production by water vapor.

As can be seen from the data of examples 1-5, the pressure drop across the reactor bed, CH₄Three indexes of conversion rate and space velocity can be seen, the reforming hydrogen production reactor and the reformer of the present disclosure exhibit excellent performance, and especially have outstanding advantages in reducing the pressure drop of the reactor and increasing the space velocity of the reactor.

The preferred embodiments of the present disclosure are described in detail with reference to the accompanying drawings, however, the present disclosure is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present disclosure within the technical idea of the present disclosure, and these simple modifications all belong to the protection scope of the present disclosure.

It should be noted that the various features described in the above embodiments may be combined in any suitable manner without departing from the scope of the invention. In order to avoid unnecessary repetition, various possible combinations will not be separately described in this disclosure.

In addition, any combination of various embodiments of the present disclosure may be made, and the same should be considered as the disclosure of the present disclosure, as long as it does not depart from the spirit of the present disclosure.

Claims

1. A reforming hydrogen production reactor is characterized by comprising a cylindrical sealed pressure-bearing shell (12), an air inlet (1), an air outlet (2), a first straight pipe (11) extending into the shell from the top of the shell (12), a second straight pipe (14) extending into the shell from the bottom of the shell (12) and a catalytic reaction zone arranged in the shell (12) below the first straight pipe (11) and above the second straight pipe (14); the air inlet is communicated with the first straight pipe (11), and the air outlet (2) is communicated with the second straight pipe (14);

the top and the bottom of the catalytic reaction zone are respectively sealed by a top sealing plate (5) and a bottom sealing plate (8), the catalytic reaction zone comprises a plurality of cylindrical catalytic reaction modules (13) which are coaxially overlapped, each catalytic reaction module (13) comprises a central pipe (6), a catalytic reaction unit and an annular gap (7) which are arranged from inside to outside, and the catalytic reaction units and the annular gaps (7) of two adjacent catalytic reaction modules (13) are separated by sealing clapboards; the central pipe (6) comprises a first central pipe and a second central pipe which are separated by an intermediate sealing plate (15), and the second central pipe of the previous catalytic reaction module (13) is communicated with the first central pipe of the next catalytic reaction module (13); the catalytic reaction unit comprises a first catalytic reaction unit (13 a) and a second catalytic reaction unit (13 b) separated by the intermediate sealing plate (15); the side wall of the central pipe and the side wall of the catalytic reaction unit are respectively provided with an opening; a gas collection cavity (9) is formed between the bottom sealing plate (8) and the inner wall of the lower part of the shell (12); the top end of the central pipe of the uppermost catalytic reaction module (13) passes through the top sealing plate (5) to communicate with the first straight pipe (11), and the bottom end of the central pipe of the lowermost catalytic reaction module (13) passes through the bottom sealing plate (8) to communicate with the gas collection chamber (9);

the first catalytic reaction unit (13 a) and the second catalytic reaction unit (13 b) are respectively provided with a micro-catalytic reaction plate (10), and the plate surface of the micro-catalytic reaction plate (10) is loaded with a reforming hydrogen production catalyst.

2. A reforming hydrogen production reactor according to claim 1, characterized in that the micro-catalytic reaction plates (10) of the first catalytic reaction unit (13 a) are radially distributed around the first central tube, the top end of the micro-catalytic reaction plate (10) of the first catalytic reaction unit (13 a) is hermetically connected with the top sealing plate (5) or with the sealing partition plate, and the bottom end of the micro-catalytic reaction plate (10) of the first catalytic reaction unit (13 a) is hermetically connected with the middle sealing plate (15); the micro-catalytic reaction plate (10) of the second catalytic reaction unit (13 b) surrounds the second central pipe and is radially distributed, the top end of the micro-catalytic reaction plate (10) of the second catalytic reaction unit (13 b) is hermetically connected with the middle sealing plate (15), and the bottom end of the micro-catalytic reaction plate (10) of the second catalytic reaction unit (13 b) is hermetically connected with the bottom sealing plate (8) or the sealing partition plate.

3. A reforming hydrogen production reactor according to claim 1, characterized in that the micro-catalytic reaction plate (10) extends along the axial direction and is spirally distributed around the first central tube or the second central tube, the top end of the micro-catalytic reaction plate (10) of the first catalytic reaction unit (13 a) is connected with the top sealing plate (5) in a sealing way or connected with the sealing baffle plate in a sealing way, and the bottom end of the micro-catalytic reaction plate (10) of the first catalytic reaction unit (13 a) is connected with the middle sealing plate (15) in a sealing way; the top end of the micro-catalytic reaction plate (10) of the second catalytic reaction unit (13 b) is hermetically connected with the middle sealing plate (15), and the bottom end of the micro-catalytic reaction plate (10) of the second catalytic reaction unit (13 b) is hermetically connected with the bottom sealing plate (8) or the sealing partition plate.

4. The reforming hydrogen production reactor according to claim 1, wherein the micro-catalytic reaction plate (10) is one annular plate or a plurality of annular plates arranged at intervals along the axial direction, the inner edge of the micro-catalytic reaction plate (10) is fixedly connected with the outer side of the tube wall of the central tube (6) in a sealing manner, and the outer edge of the micro-catalytic reaction plate (10) is fixedly connected with the inner side of the side wall of the catalytic reaction unit in a sealing manner.

5. A reforming hydrogen production reactor according to claim 1, characterized in that the micro-catalytic reaction plate (10) is at least one selected from the group consisting of a flat plate, a toothed plate and a corrugated plate.

6. A reforming hydrogen production reactor according to claim 4, characterized in that the micro-catalytic reaction plate (10) is a corrugated plate.

7. A reforming hydrogen production reformer comprises an air inlet pipe (24), an air outlet pipe (25), a burner (23) and a combustion chamber (22), and is characterized in that the reformer further comprises the reforming hydrogen production reactor (21) as claimed in any one of claims 1 to 6, the reforming hydrogen production reactor (21) is located in the combustion chamber (22), the air inlet (1) of the reforming hydrogen production reactor (21) is communicated with the air inlet pipe (24), and the air outlet (2) of the reforming hydrogen production reactor is communicated with the air outlet pipe (25).

8. The method for reforming hydrogen production reaction by using the reforming hydrogen production reformer of claim 7, characterized by comprising the steps of:

(1) fuel gas and air are sprayed into the combustion chamber (22) through the burner (23) to be combusted;

(2) and enabling feed gas and steam to enter the reforming hydrogen production reactor (21) through an air inlet pipe (24) of the reforming furnace, and carrying out reforming hydrogen production reaction in the catalytic reaction zone to obtain reformed gas rich in hydrogen.

9. The method of claim 8, wherein the reforming hydrogen production reaction conditions comprise: the reaction temperature is 700-1100 ℃, the reaction pressure is 1.8-5.5 MPaG, and H in the steam₂The molar ratio of O to carbon atoms in the raw material gas is (2.5-5): 1, the airspeed is 1000-100000 h^-1。

10. The method of claim 8, wherein the average flow velocity of the feed gas in the catalytic reaction zone is 0.5 to 85 m/s.

11. The method of claim 8, wherein the feed gas is at least one of natural gas, liquefied petroleum gas, refinery gas, a resolved gas of reformed hydrogen-enriched PSA, and naphtha; the reforming hydrogen production reaction catalyst comprises a reforming hydrogen production active component, and the reforming hydrogen production active component comprises at least one of nickel, ruthenium, platinum, palladium, iridium and rhodium.