KR102423625B1 - Hydrogen Production Reactor without Carbon Emission - Google Patents

Abstract

According to an embodiment of the present invention, the housing; at least one reaction tube provided inside the housing and through which a reactant containing ammonia is introduced into the inlet; a heating unit for providing heat to the reaction tube; and a catalyst layer extending in one direction, wherein the catalyst layer includes a ceramic catalyst layer and a metal structure catalyst layer, wherein the ceramic catalyst layer is disposed adjacent to the inlet of the reaction tube, a hydrogen production reactor is provided.

Description

Hydrogen Production Reactor without Carbon Emission

The present invention is a reactor including one or more reaction tubes inside a housing including a heat insulating layer, wherein the reaction tube has a double tube structure consisting of an inner tube and an outer tube, and includes an ammonia heating unit and a catalyst layer between the inner tube and the outer tube. , The catalyst layer is located at the bottom of the heating unit and is made of a metal catalyst supported on a catalyst support, it relates to a tubular reactor for decomposing ammonia to produce hydrogen.

To address the demand for clean and sustainable technologies for the development of portable, automotive and/or stationary fuel cells, interest in hydrogen storage materials research is on the rise. In particular, liquid or solid materials such as formic acid, ammonia, and the like, are attracting attention as chemical hydrogen storage materials applicable to fuel cells.

H2 generated from NH3, a gas that can be liquefied under mild conditions (20°C and 0.8 MPa), does not generate CO or CO2, and can supply the product to polymer electrolyte membrane fuel cells (PEMFCs). It can be applied to various fuel cell systems such as fuel cells for power generation, linked operation, and energy storage systems. This is evaluated as a potential strength because the system configuration is simple compared to the reforming system that requires additional processes such as water gas shift reaction or selective CO corrosion reaction to remove CO and CO2 generated during the process.

Ammonia decomposition reaction [2NH ₃ -> N ₂ + 3H ₂ , ΔH=46.2 kJ/mol] is an endothermic reaction and is completely converted to hydrogen and nitrogen under high temperature and atmospheric pressure conditions. In the case of an endothermic reaction in which heat transfer from the outside to the inside of the reactor is major, metal-based carriers (monolith, foam, mesh, felt) are very effective in heat transfer than conventional pellet catalysts. In order to solve this problem, when a metal-based carrier is used, in particular, in the case of FeCr alloy, there is a problem of corrosion by ammonia, so there is a problem in long-term operation of the reactor.

Therefore, the present inventors have completed a hydrogen production reactor capable of long-term operation of ammonia decomposition reaction without carbon emission by applying a ceramic support with high ammonia corrosion resistance to the reactor to generate hydrogen used as fuel cell fuel.

As a result of intensive research on the development of an economical hydrogen production reactor capable of producing clean hydrogen without carbon emission, miniaturization, and long-term operation with excellent ammonia corrosion resistance, the present inventors made the reaction tube into a double tube structure consisting of an inner tube and an outer tube. The tubular reactor was completed to produce hydrogen by decomposing ammonia to include an ammonia heating unit and a multi-layered catalyst layer in between, and it was confirmed that economical hydrogen production is possible while improving ammonia corrosion resistance.

According to an embodiment of the present invention, the housing; at least one reaction tube provided inside the housing and through which a reactant containing ammonia is introduced into the inlet; a heating unit for providing heat to the reaction tube; and a catalyst layer extending in one direction, wherein the catalyst layer includes a ceramic catalyst layer and a metal structure catalyst layer, wherein the ceramic catalyst layer is disposed adjacent to the inlet of the reaction tube, a hydrogen production reactor is provided.

According to an embodiment of the present invention, the reaction tube includes a double tube structure consisting of an inner tube of the reaction unit and an outer tube of the reaction unit surrounding the inner tube of the reaction unit, and the catalyst layer is provided in the exterior of the reaction unit, the hydrogen production reactor is provided

According to an embodiment of the present invention, the ceramic catalyst layer and the metal structure catalyst layer are provided in the order of the ceramic catalyst layer-the metal structure catalyst layer along the inflow direction of the reactant, and the reactant passes through the ceramic catalyst layer and the metal structure A hydrogen production reactor is provided, which is introduced into the catalyst bed.

According to an embodiment of the present invention, the ceramic catalyst layer is provided outside the reaction tube, the metal structure catalyst layer is provided inside the reaction tube spaced apart from the ceramic catalyst layer, a hydrogen production reactor is provided.

According to an embodiment of the present invention, the ceramic catalyst layer includes at least one material selected from the group consisting of Al ₂ O ₃ , SiC, Cordierite, and MgO as a support, and includes an active metal provided on the support. Hydrogen A production reactor is provided.

According to an embodiment of the present invention, the active metal includes at least one selected from the group consisting of Ru, Ni, Fe, Co, and Rh, a hydrogen production reactor is provided.

According to an embodiment of the present invention, the metal structure catalyst layer includes a metal structure and catalyst particles, and the metal structure includes at least one material selected from the group consisting of Fe, Cr, Ni, Al, Mn, Cu, and , wherein the catalyst particles comprise a carrier and an active metal provided on the carrier.

According to an embodiment of the present invention, the reaction tube further includes a preheating portion, the preheating portion comprising silicon carbide (SiC) and a metal filler, there is provided a hydrogen production reactor.

According to an embodiment of the present invention, the metal filler is any one or more selected from the group consisting of tungsten, nickel, iron, cobalt, chromium, molybdenum, manganese, aluminum, copper, a hydrogen production reactor is provided.

According to an embodiment of the present invention, the ceramic catalyst layer included in the catalyst layer is included in a ratio of 5% to 15% with respect to the total volume of the catalyst layer, a hydrogen production reactor is provided.

By applying a ceramic support with high ammonia corrosion resistance to a multi-layered catalyst layer in a tubular reactor, the efficiency of the ammonia decomposition reaction was improved and a hydrogen production reactor capable of long-term operation was completed. Through the present invention, it is possible to obtain a clean fuel without carbon emission, and by confirming that hydrogen production is possible economically, high utility is expected in a fuel cell using hydrogen as a fuel.

1 is a cross-sectional view of a hydrogen production reactor according to an embodiment of the present invention.
2 is a cross-sectional view of a reaction tube included in a hydrogen production reactor according to an embodiment of the present invention.
3 is a cross-sectional view of a reaction tube included in a hydrogen production reactor according to another embodiment of the present invention.
4 is an image showing the corrosion pattern according to the amount of the ceramic catalyst layer included in the catalyst layer.
5 is a graph showing the change in ammonia conversion rate according to the amount of the ceramic catalyst layer included in the catalyst layer.

Since the present invention can have various changes and can have various forms, specific embodiments are illustrated in the drawings and described in detail in the text. However, this is not intended to limit the present invention to the specific disclosed form, it should be understood to include all modifications, equivalents and substitutes included in the spirit and scope of the present invention.

Since the hydrogen production reactor according to the present invention includes a ceramic catalyst layer and a metal structure catalyst layer, it is possible to produce hydrogen with high efficiency without a problem of corrosion of the catalyst layer due to the reactant containing ammonia.

1 is a cross-sectional view of a hydrogen production reactor according to an embodiment of the present invention.

Referring to FIG. 1 , the hydrogen production reactor is provided inside the housing 100 and the housing 100 and heats at least one reaction tube 200 through which a reactant containing ammonia is introduced into the inlet, and the reaction tube 200 . It includes a heating unit 300 for providing and a catalyst layer extending in one direction, the catalyst layer includes a ceramic catalyst layer and a metal structure catalyst layer, and the ceramic catalyst layer is disposed adjacent to the inlet of the reaction tube.

The housing 100 may include an empty space therein to accommodate the reaction tube 200 . In some cases, the housing 100 may have a hole in its upper surface so that at least a part of the reaction tube 200 is inserted into the housing 100 .

The housing 100 may have various shapes, such as a cylinder, a cube, and a cuboid. The size of the inner space of the housing 100 may be greater than the volume of the reaction tube 200 . Specifically, the size of the inner space of the housing 100 may be sufficient to accommodate at least one or more reaction tubes 200 spaced apart from each other.

The housing 100 may further include a heat insulating material on the wall surface. Accordingly, when the heating unit 300 is provided inside the housing 100 , the heat generated by the heating unit 300 may be prevented from escaping out of the housing 100 . Since the reaction in which hydrogen is extracted from ammonia is an endothermic reaction, it is possible to produce hydrogen more efficiently by preventing heat loss by using the insulating material included in the housing 100 .

At least one reaction tube 200 is provided within the housing.

In the reaction tube 200 , the conversion reaction of the reactants is performed. In this case, the reactant may include ammonia, and the conversion reaction may be a reaction in which hydrogen is extracted from ammonia. Accordingly, an endothermic reaction in which hydrogen is extracted from ammonia while passing through the reaction tube 200 after a reactant containing ammonia is introduced into the reaction tube 200 may be performed. The produced hydrogen may be discharged to the outside along the reaction tube 200 in a gaseous form. Although not shown in the drawings, the hydrogen production reactor may further include a separator for separating hydrogen gas from the product.

A plurality of reaction tubes 200 may be provided adjacent to the heating unit 300 providing reaction heat. By providing a plurality of reaction tubes 200, the amount of ammonia decomposition per unit time is increased, and thus hydrogen production can be improved.

The reaction tube 200 may be provided in the form of a tubular reactor. A tubular reactor has the advantage of easy catalyst charging compared to a channel reactor. In the channel reactor, it is difficult to uniformly coat the catalyst directly inside the long channel, and it is also not easy to insert the catalyst into the channel. In addition, the channel reactor has a problem in that when the balance between exothermic and endothermic reactions occurring on both sides of the channel is not balanced, the reaction does not occur, so that the catalyst is deactivated and the reactor efficiency is lowered.

A preheating unit 211 may be further provided in the reaction tube 200 . The preheating unit 211 includes a material having high thermal conductivity so that heat supplied from the outside of the reaction tube 200 can be quickly transferred to the inside of the reaction tube 200 . The preheating unit 211 may include silicon carbide (SiC) and a metal filler. The thermal conductivity of the preheating unit 211 may be improved by including the above-described material. In particular, silicon carbide has been confirmed to be an excellent thermally conductive material, and may be included in the preheating unit 211 . The metal filler may be any one or more from the group consisting of stainless steel (SUS), but is not limited thereto. The stainless steel may refer to a material made of Fe and Cr. Non-limiting examples of the metal filler include tungsten, nickel, iron, cobalt, chromium, molybdenum, manganese, aluminum, copper, and the like. In some cases, the preheating unit 211 may include Fe fibers.

The hydrogen production reactor according to an embodiment of the present invention can perform a hydrogen production reaction with high efficiency by including at least one or more reaction tubes 200 .

As described above, the heating unit 300 is provided to provide heat to the inside of the reaction tube 200 .

The heating unit 300 provides heat to the reaction tube 200 . The heating unit 300 may be a heat transfer device or a burner that generates an exothermic reaction such as a combustion reaction. There is no particular limitation on the form of providing the heating unit 300 . However, as shown in the drawings, in the case of an embodiment of the present invention, the heating unit 300 may be provided in the form of a burner.

The heating unit 300 is provided inside the housing 100 and radiates heat into the housing 100 . There is no limitation on the location of the heating unit 300 . For example, the heating unit 300 may be provided at the center of the housing 100 , and a plurality of reaction tubes 200 may be provided in a form surrounding the heating unit 300 . Alternatively, the heating unit 300 may be provided along the wall surface of the housing 100 , and the reaction tube 200 may be provided inside the heating unit 300 .

Heat provided from the heating unit 300 is transferred to the reaction tube 200 and/or the catalyst layer 250 .

The catalyst layer 250 receives heat provided from the heating unit 300 to promote a reaction in which hydrogen is generated from ammonia. The catalyst layer 250 includes a ceramic catalyst layer 251 and a metal structure catalyst layer 252 . At least a portion of the catalyst layer 250 may be provided in the reaction tube 200 . For example, the entire catalyst layer 250 may be provided in the reaction tube 200 as shown in the drawings. According to another example, a portion of the catalyst layer 250 may be provided outside the reaction tube 200 .

Further details regarding the catalyst layer 250 will be described later.

In the above, a hydrogen production reactor according to an embodiment of the present invention was examined. Hereinafter, we will look at the reaction tube included in the hydrogen production reactor in more detail.

2 is a cross-sectional view of a reaction tube included in a hydrogen production reactor according to an embodiment of the present invention.

Referring to FIG. 2 , the reaction tube 200 is provided with a catalyst layer 250 therein. The catalyst layer 250 may have a shape extending in one direction within the reaction tube 200 . For example, the catalyst layer 250 may be provided in the form of filling the inside of the reaction tube 200 in the form of a tube or coated on the inner wall of the reaction tube 200 . As the catalyst layer 250 is provided in a form extending in one direction, the reactant may continue to contact the catalyst layer 250 while flowing along the reaction tube 200 . Accordingly, the effect of promoting the conversion reaction of the reactants by the catalyst layer 250 may be further improved.

The catalyst layer 250 includes a ceramic catalyst layer 251 and a metal structure catalyst layer 252 . In this case, the ceramic catalyst layer 251 is disposed adjacent to the inlet of the reaction tube 200 . Accordingly, the reactant may first meet the ceramic catalyst layer 251 .

The ceramic catalyst layer 251 may include catalyst particles supported on a ceramic support. Since the ceramic support has strong corrosion resistance, it is not corroded by ammonia contained in the reactant. In the ceramic catalyst layer 251 , the catalyst particles may be coated on a ceramic support or may be provided in powder form. Since the ceramic catalyst layer 251 has corrosion resistance to ammonia, the catalyst layer 250 is not deteriorated even after repeated use and the catalytic effect can be maintained. The catalyst particles may include a ceramic carrier and an active metal. Specifically, the catalyst particles may be provided in a form in which an active metal is supported on a ceramic carrier. The ceramic carrier may be at least one selected from the group consisting of Al ₂ O ₃ , SiC, Cordierite, and MgO, but is not limited thereto. In addition, the ceramic is not limited to a specific structure or shape, and for example, monoliths and foams other than pellets may be used. The active metal may be at least one selected from the group consisting of Ru, Ni, Fe, Co, and Rh, but is not limited thereto.

The metal structure catalyst layer 252 includes a metal structure and catalyst particles supported thereon. The metal structure has excellent heat transfer properties. Therefore, since the metal structure is included in the metal structure catalyst layer 252, heat inside the reactor can be rapidly transferred to the catalyst particles supported on the metal structure. Accordingly, the rate of the endothermic reaction promoted by the catalyst particles is increased. The metal structure may be at least one selected from the group consisting of Fe, Cr, Ni, Al, Mn, and Cu, but is not limited thereto. The metal structure may be in the form of a metal foam, monolith, or the like. The catalyst particles may be supported on the metal structure. The catalyst particles may include a ceramic carrier and an active metal. The catalyst particles may be a composite of a ceramic carrier and an active metal. The ceramic carrier may be at least one selected from the group consisting of Al ₂ O ₃ , SiC, Cordierite, and MgO, but is not limited thereto. In addition, the ceramic is not limited to a specific structure or shape, and for example, monoliths and foams other than pellets may be used. The active metal may be at least one selected from the group consisting of Ru, Ni, Fe, Co, and Rh, but is not limited thereto.

The metal structure catalyst layer 252 may be composed of a plurality of stages. The metal structures of the plurality of stages may be independently replaced with each other. In addition, the metal structure catalyst layer 252 may be independently added or removed in the reaction tube 200 according to the throughput of the reactor.

The metal structure catalyst layer 252 is provided after the ceramic catalyst layer 251 along the inflow direction of the reactants. Accordingly, the reactant first passes through the ceramic catalyst layer 251 and then flows into the metal structure catalyst layer 252 . Accordingly, when the reactant contains a high concentration of ammonia gas, a conversion reaction of ammonia is first performed in the ceramic catalyst layer 251 to decrease the concentration of ammonia gas in the reactant. Next, since the metal structure catalyst layer 252 and the reactant meet in a state in which the concentration of ammonia gas is reduced, it is possible to prevent the metal structure catalyst layer 252 from being corroded by ammonia.

According to the prior art, there is a problem that long-term operation is impossible when a metal structure having a corrosive effect on ammonia is used. It was confirmed that the surface of the metal structure was corroded after the ammonia decomposition reaction at an actual high temperature. According to the present invention, since the ceramic catalyst layer 251 and the metal structure catalyst layer 252 are provided in the above-described form, there is no risk of corrosion of the catalyst layer during the process. In addition, since the concentration of ammonia gas included in the reactant may be increased, process efficiency may be improved.

The ceramic catalyst layer 251 included in the catalyst layer 250 may be included in a ratio of 5% to 15% with respect to the total volume of the catalyst layer 250 . When the ceramic catalyst layer 251 is included in less than 5% by volume, the reaction between the ceramic catalyst layer 251 and ammonia may not be sufficiently performed. In this case, a high concentration of ammonia gas may be introduced into the metal structure catalyst layer 252 to cause corrosion of the metal structure catalyst layer 252 . In addition, when the ceramic catalyst layer 251 is included in an amount exceeding 15% by volume, the amount of the metal structure catalyst layer 252 is reduced, so that heat transfer efficiency through the metal structure may be reduced. Accordingly, the hydrogen gas production efficiency from ammonia gas may be reduced.

Looking in more detail with respect to the reaction tube 200 including the catalyst layer 250 described above, the reaction tube 200 includes the reaction unit inner tube 220 and the reaction unit outer tube 210 surrounding the reaction unit inner tube 220 . It may have a double tube structure. By forming the reaction tube 200 in a double tube structure, the reaction tube 200 can be increased in length while preventing the outflow of heat so that the reactant and the catalyst layer 250 react in a wider area. In addition, it is possible to provide a more compact hydrogen production reactor.

3 is a cross-sectional view of a reaction tube included in a hydrogen production reactor according to another embodiment of the present invention.

Referring to FIG. 3 , the ceramic catalyst layer 251 is provided to be spaced apart from the metal structure catalyst layer 252 . Specifically, the ceramic catalyst layer 251 is provided outside the reaction tube 200 , and the metal structure catalyst layer 252 is spaced apart from the ceramic catalyst layer 251 and provided inside the reaction tube 200 .

As described above, the ceramic catalyst layer 251 and the metal structure catalyst layer 252 may be provided to be spaced apart from each other. In this case, by designing the ceramic catalyst layer 251 to first meet the reactants and then to meet the metal structure catalyst layer 252 , the corrosion prevention effect as described above can be obtained.

When the ceramic catalyst layer 251 and the metal structure catalyst layer 252 are provided separately, the degree of freedom in reactor design may be improved. In addition, since the ceramic catalyst layer 251 is provided outside the reaction tube 200 , the ceramic catalyst layer 251 can be easily replaced. The reactant material supplied to the ceramic catalyst layer 251 may be provided after being preheated, so that even if the ceramic catalyst layer 251 is outside the reaction tube 200 , a reaction in which hydrogen is produced from ammonia may be performed without any problem. In addition, a reaction material having a reduced ammonia concentration due to a reaction occurring in the ceramic catalyst layer 251 provided outside the reactor is provided to the metal structure catalyst layer 252, thereby preventing corrosion of the metal structure catalyst layer 252 by ammonia.

The present invention also provides a hydrogen system comprising the hydrogen production reactor described above. The hydrogen system may further include a member that uses the produced hydrogen. For example, hydrogen produced by using the hydrogen production reactor of the present invention in a hydrogen system can be used as a fuel for a fuel cell or as a fuel for a hydrogen vehicle, and thus can be applied to a hydrogen filling station. Thus, a hydrogen system comprising a hydrogen production reactor according to the present invention can be used to produce electric power.

In the above, the shape of the hydrogen production reactor according to an embodiment of the present invention was examined. Hereinafter, we will look at the advantageous effect of the hydrogen production reactor according to an embodiment of the present invention through comparative experimental data.

Experimental Example 1. Catalyst layer corrosion test

In order to check whether the catalyst layer is corroded in the hydrogen production reaction using ammonia, the hydrogen production reaction using ammonia was performed on the catalyst layer in which the amount of the ceramic catalyst layer was 0%, 5%, 10%, and 15% by volume. The experiment was performed under the conditions of a reaction temperature of about 700° C., atmospheric pressure, and GHSV of 5,000 h ⁻¹ , and ruthenium (Ru) was used as the catalyst particles included in the catalyst layer.

4 is an image showing the corrosion pattern according to the amount of the ceramic catalyst layer included in the catalyst layer.

4(a) is a view of the catalyst layer before the reaction, and FIGS. 4(b), (c), (d), and (e) show that the amount of the ceramic catalyst layer is 0%, 5%, 10%, and This is the image after the reaction at 15%.

First, referring to FIG. 4 (a), it can be seen that the catalyst layer has a porous shape before the reaction. Next, referring to FIG. 4B , when the ceramic catalyst layer is not provided, it can be confirmed that the shape of the catalyst layer is deformed due to corrosion after the reaction or the catalyst layer is lost from above. In contrast, in the case of (c), (d), and (e) containing 5% to 15% of the ceramic catalyst layer, it can be seen that the form of the catalyst layer is maintained relatively intact after the reaction. In particular, in the case of FIG. 4(e), it can be confirmed that the deformation of the catalyst layer is not observed with the naked eye before and after the reaction.

Accordingly, it can be seen from the comparison result of FIG. 4 that corrosion can be prevented by providing the ceramic catalyst layer.

Experimental Example 2. Ammonia conversion rate evaluation

In order to evaluate the ammonia conversion rate according to the amount of the ceramic catalyst layer, a hydrogen production reaction using ammonia was performed on the catalyst layer having the amount of the ceramic catalyst layer of 0%, 5%, 10%, and 15% by volume. The experiment was performed under the conditions of a reaction temperature of about 700° C., atmospheric pressure, and GHSV of 5,000 h ⁻¹ , and ruthenium (Ru) was used as the catalyst particles included in the catalyst layer.

5 is a graph showing the change in ammonia conversion rate according to the amount of the ceramic catalyst layer included in the catalyst layer.

Referring to FIG. 5 , when the ceramic catalyst layer is not included in the catalyst layer (displayed as 0%), it can be seen that the ammonia conversion rate is rapidly decreased as the reaction time increases. Specifically, when the reaction time is about 300 hours, it can be confirmed that the ammonia conversion rate is reduced by about 4%.

In contrast, when the catalyst layer contains 5%, 10%, and 15% of the ceramic catalyst layer, respectively, it can be seen that the reduction in ammonia conversion rate according to the reaction time is small. In particular, when about 15% of the ceramic catalyst layer is included in the catalyst layer, it can be confirmed that there is no decrease in the ammonia conversion rate even after the reaction time has elapsed for 300 hours.

Although the above has been described with reference to the preferred embodiment of the present invention, those skilled in the art or those having ordinary knowledge in the technical field will not depart from the spirit and technical scope of the present invention described in the claims to be described later. It will be understood that various modifications and variations of the present invention can be made without departing from the scope of the present invention.

Accordingly, the technical scope of the present invention should not be limited to the contents described in the detailed description of the specification, but should be defined by the claims.

100: housing 200: reaction tube
300: heating unit 210: reaction unit appearance
220: inner tube of reaction unit 250: catalyst layer
251: ceramic catalyst layer 252: metal structure catalyst layer

Claims (10)

housing;
at least one reaction tube provided inside the housing and through which a reactant containing ammonia is introduced into the inlet;
a heating unit for providing heat to the reaction tube; and
It includes a catalyst layer extending in one direction,
The catalyst layer includes a ceramic catalyst layer and a metal structure catalyst layer,
wherein the ceramic catalyst bed is disposed adjacent the inlet of the reaction tube. According to claim 1,
The reaction tube includes a double tube structure consisting of an inner tube of the reaction unit and an outer tube of the reaction unit surrounding the inner tube of the reaction unit,
The catalyst layer is provided in the exterior of the reaction unit, hydrogen production reactor. According to claim 1,
The ceramic catalyst layer and the metal structure catalyst layer are provided in the order of the ceramic catalyst layer-the metal structure catalyst layer along the inflow direction of the reactant,
The reactant is introduced into the metal structure catalyst layer through the ceramic catalyst layer, hydrogen production reactor. According to claim 1,
The ceramic catalyst layer is provided outside the reaction tube,
The metal structure catalyst layer is provided inside the reaction tube spaced apart from the ceramic catalyst layer, hydrogen production reactor. According to claim 1,
The ceramic catalyst layer includes at least one material selected from the group consisting of Al ₂ O ₃ , SiC, Cordierite, and MgO as a carrier,
A hydrogen production reactor comprising an active metal provided on the carrier. 6. The method of claim 5,
The active metal comprises at least one selected from the group consisting of Ru, Ni, Fe, Co, Rh, hydrogen production reactor. According to claim 1,
The metal structure catalyst layer includes a metal structure and catalyst particles,
The metal structure includes at least one material selected from the group consisting of Fe, Cr, Ni, Al, Mn, and Cu,
wherein the catalyst particles comprise a carrier and an active metal provided on the carrier. According to claim 1,
The reaction tube further comprises a preheating unit,
The preheating unit will include silicon carbide (SiC) and a metal filler, hydrogen production reactor. 9. The method of claim 8,
The metal filling is at least one selected from the group consisting of tungsten, nickel, iron, cobalt, chromium, molybdenum, manganese, aluminum, and copper, hydrogen production reactor. The hydrogen production reactor of claim 1, wherein the ceramic catalyst layer included in the catalyst layer is included in a ratio of 5% to 15% with respect to the total volume of the catalyst layer.

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