KR20220130435A - Sustainable hydrogen extraction reactor - Google Patents

Abstract

According to one embodiment of the present invention, provided is a hydrogen extraction reacting device which comprises: a reactor in which a reaction of extracting hydrogen from a hydrogen storage compound is performed; a catalytic foam provided in the inside of the reactor; and a heat source providing heat to the catalyst foam, wherein the catalyst foam includes: nickel (Ni); chromium (Cr); aluminum (Al); and pores therein.

Description

SUSTAINABLE HYDROGEN EXTRACTION REACTOR

The present invention relates to a sustainable hydrogen extraction reactor using a renewable heat source.

Hydrogen has recently attracted attention as an eco-friendly and sustainable energy carrier capable of storing large-capacity renewable energy of 0.1 to 10 MWh per pressure tank or 0.1 to 100 GWh per liquid tank. At the same time, hydrogen energy is being actively developed as an efficient energy system to replace the existing energy system powered by fossil fuels that have a negative impact on the environment. Accordingly, the hydrogen fuel cell is positioned as an eco-friendly system with high efficiency and water (H ₂ O) as a by-product.

Conventional methods for producing hydrogen include electrolysis of water, solar electrolysis of water, steam-methane reforming (hereinafter, SMR) method using a metal catalyst such as nickel or rhodium supported on nickel (Ni) or alumina support, carbon There are a direct decomposition of methane using a sieve catalyst and a method of decomposing methanol using a catalyst such as copper, gold, or platinum supported on an alumina or zinc oxide support.

Hydrogen is a useful energy source, but the above-described conventional methods have a problem in that hydrogen production efficiency is low. In particular, since a lot of energy is required to produce hydrogen, there is also a problem that the production and use of hydrogen is difficult to be considered as energy efficient. In order to solve this problem, a technology capable of producing hydrogen energy efficiently is required.

An object of the present invention is to provide a sustainable hydrogen extraction reaction apparatus capable of producing hydrogen energy efficiently.

According to an embodiment of the present invention, a reactor in which a reaction for extracting hydrogen from a hydrogen storage compound is performed; Catalytic foam provided inside the reactor; and a heat source for providing heat to the catalytic foam, wherein the catalytic foam includes nickel (Ni), chromium (Cr) and aluminum (Al) and includes voids therein, a hydrogen extraction reaction device is provided

According to an embodiment of the present invention, the catalytic foam further comprises a catalytic foam substrate comprising nickel (Ni), chromium (Cr) and aluminum (Al) and a subcatalyst provided on the catalytic foam substrate, hydrogen extraction reaction A device is provided.

According to an embodiment of the present invention, the subcatalyst is provided with a hydrogen extraction reaction device comprising ruthenium (Ru).

According to an embodiment of the present invention, the subcatalyst is provided by being coated on the surface of the catalyst foam substrate in a form inserted on the surface of the catalyst foam substrate, or inserted on the coating substrate to form a coating layer, A hydrogen extraction reaction apparatus is provided.

According to an embodiment of the present invention, the heat source is provided in the form of an electrode attached to the catalyst foam, and the electrode supplies current to the catalyst foam to generate Joule heating from the catalyst foam, A hydrogen extraction reaction apparatus is provided.

According to an embodiment of the present invention, the hydrogen storage compound contains ammonia, and a reaction in which hydrogen is extracted from the ammonia is performed in the reactor, a hydrogen extraction reaction apparatus is provided.

According to an embodiment of the present invention, the reactor is provided in the form of a tube extending in one direction, the hydrogen storage compound is provided to one side of the reactor, and hydrogen is discharged to the other side of the reactor, hydrogen extraction A reaction apparatus is provided.

According to an embodiment of the present invention, the catalyst foam is provided to be filled along the extension direction of the reactor inside the reactor in the form of a tube, a hydrogen extraction reaction device is provided.

According to an embodiment of the present invention, a hydrogen extraction reaction device; and a stack for generating electricity by separating electrons from hydrogen gas in the gas generated from the hydrogen extraction reaction apparatus, wherein the hydrogen extraction reaction apparatus comprises: a reactor in which a reaction of extracting hydrogen from a hydrogen storage compound is performed; Catalytic foam provided inside the reactor; and a heat source for providing heat to the catalytic foam, wherein the catalytic foam includes nickel (Ni), chromium (Cr) and aluminum (Al) and includes voids therein, a fuel cell is provided do.

According to an embodiment of the present invention, hydrogen can be produced with high energy efficiency using a renewable heat source.

1 is a perspective view showing a hydrogen extraction reaction apparatus according to an embodiment of the present invention.
2 is an image and a TEM image schematically showing a catalyst foam according to an embodiment of the present invention.
3 is an image and a TEM image schematically showing a catalyst foam according to an embodiment of the present invention.
4 is a perspective view illustrating a fuel cell according to an embodiment of the present invention.
5 is a result of analyzing a catalyst foam according to an embodiment of the present invention.
6 is a graph analyzing the hydrogen extraction reaction efficiency of a hydrogen extraction reaction apparatus including a catalyst foam according to an embodiment of the present invention.
7 is a graph analyzing the thermal energy efficiency of a hydrogen extraction reaction apparatus including a catalyst foam according to an embodiment of the present invention.

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.

In describing each figure, like reference numerals have been used for like elements. In the accompanying drawings, the dimensions of the structures are enlarged than the actual size for clarity of the present invention. Terms such as first, second, etc. may be used to describe various elements, but the elements should not be limited by the terms. The above terms are used only for the purpose of distinguishing one component from another. For example, without departing from the scope of the present invention, a first component may be referred to as a second component, and similarly, a second component may also be referred to as a first component. The singular expression includes the plural expression unless the context clearly dictates otherwise.

In the present application, terms such as “comprise” or “have” are intended to designate that a feature, number, step, operation, component, part, or combination thereof described in the specification exists, but one or more other features It is to be understood that it does not preclude the possibility of the presence or addition of numbers, steps, operations, components, parts, or combinations thereof. Also, when a part of a layer, film, region, plate, etc. is said to be “on” another part, this includes not only cases where it is “directly on” another part, but also cases where another part is in between. In addition, in the present specification, when a portion such as a layer, film, region, or plate is formed on another portion, the formed direction is not limited only to the upper direction, and includes those formed in the side or lower direction. . Conversely, when a part, such as a layer, film, region, plate, etc., is "under" another part, it includes not only cases where it is "directly under" another part, but also a case where another part is in between.

In this specification, 'upper surface' and 'lower surface' are used as relative concepts to easily understand the technical idea of the present invention. Accordingly, the terms 'top' and 'bottom' do not refer to specific directions, positions, or components, and may be interchangeable with each other. For example, 'top' may be interpreted as 'bottom' and 'bottom' may be interpreted as 'top'. Therefore, 'top' may be expressed as 'first' and 'bottom' as 'second', 'bottom' may be expressed as 'first' and 'top' as 'second'. However, in one embodiment, 'top surface' and 'bottom surface' are not used interchangeably.

According to an embodiment of the present invention, a hydrogen extraction reaction can be performed using a reactor including a catalyst foam therein, a hydrogen extraction reaction device that transfers heat to the catalyst foam inside the reactor, and the heat supplied to the inside of the reactor It is used for the hydrogen extraction reaction without this loss, and the reactor efficiency is excellent because heat is transferred and contacted with the reactants in a large area of the catalyst foam.

1 is a perspective view showing a hydrogen extraction reaction apparatus according to an embodiment of the present invention.

Referring to FIG. 1 , the hydrogen extraction reaction apparatus includes a reactor 100 in which a reaction for extracting hydrogen from a hydrogen storage compound is performed; Catalytic Foam (200) provided inside the reactor (100); and a heat source 300 for providing heat to the catalyst foam 200, wherein the catalyst foam 200 includes nickel (Ni), chromium (Cr), and aluminum (Al) and includes voids therein.

In the reactor 100 , a hydrogen storage compound is introduced and a reaction in which hydrogen is extracted from the introduced hydrogen storage compound occurs. The shape of the reactor 100 may be variously implemented, such as a batch reactor, a continuous reactor, and the like. The shape of the reactor 100 may be determined in consideration of the hydrogen storage compound processing capacity and the use of the hydrogen extraction reactor.

The inside of the reactor 100 may include an empty space so that the reaction can occur. In addition, the outer wall of the reactor 100 may be made of a heat insulating material to prevent heat from entering and leaving the reactor 100 . For example, the outer wall of the reactor 100 may include quartz, and thus thermal conductivity may be very low.

The reactor 100 may include an inlet through which a hydrogen storage compound is introduced and an outlet for discharging hydrogen produced after the reaction in order to perform the above-described reaction. In this case, a hydrogen separation device for separating hydrogen from the reaction product may be further provided on the outlet if necessary. There is no particular limitation on the form of the hydrogen separation device.

The reactor 100 may have a tube shape extending in one direction. In this case, one side of the reactor 100 is provided with the above-described inlet so that the hydrogen storage compound flows into the reactor 100, and the other side of the reactor 100 is provided with the above-described outlet so that hydrogen gas among the reaction products is discharged into the reactor ( 100) can be released. The length and inner diameter of the reactor 100 may be determined in consideration of the hydrogen storage compound processing capacity and the use of the hydrogen extraction reactor.

A catalyst foam 200 is provided inside the reactor 100 for accelerating the reaction in which hydrogen is extracted from the hydrogen storage compound.

The catalyst foam 200 includes nickel (Ni), chromium (Cr), and aluminum (Al), and includes pores therein. Since the catalyst foam 200 includes pores therein, the specific surface area is large. Accordingly, the reaction area between the catalyst foam 200 and the hydrogen storage compound is large, and when a Joule heat source is used, heat is dissipated from the large surface area of the catalyst foam 200, so the exothermic efficiency is very excellent. And the generated heat can meet a larger amount of hydrogen storage compound for the same time, so the reactor efficiency is very good.

The porosity of the catalyst foam 200 may be about 70% to about 90%. In addition, the specific surface area of the catalyst foam 200 may be about 3.0 m ² /L to 5 m ² /L. As the catalyst foam 200 has a porosity and a specific surface area in the above-described ranges, advantageous effects in the above-described calorific value and reaction area may be exhibited.

The form of providing the catalyst foam 200 may vary depending on the form of the reactor 100 . For example, when the reactor 100 is a batch reactor and a continuous reactor, the form of providing the catalyst foam 200 may be different. When the reactor 100 is provided in the form of a tube extending in one direction as described above, the catalyst foam 200 may also be provided by being filled in the reactor 100 along the extension direction of the reactor 100 .

When the catalyst foam 200 is provided filled in one direction as described above, the catalyst foam 200 is in the form of a rod extending along the flow direction of the hydrogen storage compound in the reactor 100 when viewed as a whole. can represent Accordingly, the hydrogen storage compound introduced into the reactor 100 may react with the catalyst foam 200 while flowing inside the reactor 100 . In this case, most of the introduced hydrogen storage compound may complete the reaction with the catalyst foam 200 when it reaches the end region of the reactor 100 , that is, the outlet region where the generated hydrogen gas is discharged. In particular, in the case of the present invention, as will be seen below, since the inside of the catalyst foam 200 or the reactor 100 is not locally heated, but heat is dissipated in the entire area of the catalyst foam 200, the catalyst foam ( 200), sufficient thermal energy can be provided for the hydrogen extraction reaction regardless of its location. More details on the technical configuration for supplying heat to the catalyst foam 200 will be described later.

The hydrogen storage compound reacting in the catalyst foam 200 may include at least one selected from the group consisting of ammonia (NH ₃ ), methanol, liquid organic hydrogen carrier (LOHC), formic acid, and formate. For example, the hydrogen storage compound may be ammonia. Ammonia provides a high gravimetric and bulk hydrogen storage density (about 17.8 wt %, 108 g/L at 20 °C and 8.6 bar) and has the advantage of no carbon emissions and no side reaction problems during dehydrogenation. In addition, ammonia is industrially produced in large quantities, and is excellent for use as a hydrogen storage compound in that the infrastructure for production and transport is currently in place. However, in the case of the hydrogen extraction reactor of the present invention, it can be used to extract hydrogen from various hydrogen storage compounds as well as ammonia by designing differently the composition of the catalyst, the amount of the loaded catalyst, the shape of the reactor, and the like.

Extracting hydrogen from the hydrogen storage compound described above in the catalyst foam 200, the so-called dehydrogenation reaction may be an endothermic reaction. Therefore, a continuous heat supply is required to extract hydrogen from the hydrogen storage compound. In addition, as described above, when the reactor 100 is a continuous reactor or when the catalyst foam 200 is extended in one direction and provided for a long time, it is important to evenly transfer heat to various regions of the catalyst foam 200 . . When heat is locally applied, the hydrogen extraction reaction is actively performed in the region to which the heat is provided and the region adjacent thereto, but the hydrogen extraction reaction does not occur or the efficiency is lowered in the region far from the region to which the heat is provided, so the reactor efficiency is low.

A heat source 300 is provided to evenly transfer heat to the catalyst foam 200 as described above.

The heat source 300 is a device for transferring heat to the catalyst foam 200 , and supplies heat to the inside of the reactor 100 . The heat source 300 may be provided in the form of an electrode attached to the catalyst foam 200 , and the electrode may supply current to the catalyst foam 200 to generate Joule heating from the catalyst foam 200 . Therefore, in this case, the heat source 300 supplies electric energy to the entire area of the catalyst foam 200, rather than locally supplying thermal energy to a specific area of the catalyst foam 200 or the reactor 100, and the catalyst foam. In (200), electrical energy may be converted into thermal energy by Joule heating. Accordingly, thermal energy may be uniformly generated in the entire region of the catalyst foam 200 .

As the heat source 300 is provided in the form described above, the entire catalyst foam 200 may be used as a kind of heat generating device. In this case, the catalyst foam 200 may be formed of an alloy of thermally stable nickel (Ni), chromium (Cr), and aluminum (Al). In addition, the catalyst foam 200 of the above composition has the advantage that there is no fear of being deformed at high temperature or corroded by reacting with oxygen or ammonia.

The heat source 300 may further include an electrode unit electrically connected to the catalyst foam 200 and a power supply unit for supplying current to the electrode unit. The electrode part is made of a material with high conductivity, and may be provided outside the reactor 100 to avoid unnecessary reaction with the hydrogen storage compound. Accordingly, the catalyst foam 200 may represent a form in which a portion is derived from the reactor 100 , and the protruding region of the catalyst foam 200 may be electrically connected to the electrode portion of the heat source 300 . The power supply unit is a power supply device for supplying current to the electrode unit, and may supply DC power or AC power.

The shape of the heat source 300 is not limited to that shown in the drawings. For example, the electrode portion of the heat source 300 may be provided to be spaced apart from the catalyst foam 200 . In this case, for example, the electrode part of the heat source 300 may be connected to a power supply for supplying AC power, and the catalyst foam 200 may be heated using induction heating.

In the above, a hydrogen extraction reactor according to an embodiment of the present invention was examined. The hydrogen extraction reactor according to the present invention may exhibit high thermal efficiency and hydrogen extraction efficiency by causing Joule heat to occur in the entire area of the catalyst foam 200 having a large specific surface area. In addition, the hydrogen extraction reactor according to an embodiment of the present invention has the advantages of high pressure drop, toxic emissions, inherent combustion complexity, and no need for additional catalysts for oxidation.

Hereinafter, the modified form of the catalyst foam according to an embodiment of the present invention will be looked at in more detail.

2 and 3 are images and TEM images schematically showing the catalyst foam according to an embodiment of the present invention.

2 and 3 , the catalyst foam may further include a co-catalyst in addition to nickel (Ni), chromium (Cr) and aluminum (Al). The catalyst foam may further include a catalyst foam substrate including nickel (Ni), chromium (Cr) and aluminum (Al) and a cocatalyst provided on the catalyst foam substrate.

The catalyst foam substrate includes an alloy of nickel (Ni), chromium (Cr), and aluminum (Al), and may be a substrate including voids therein. The porosity of the catalyst foam substrate may be about 70% to about 90%, and the specific surface area may be about 3.0 m ² /L to 5 m ² /L. When the catalyst foam substrate has a porosity and a specific surface area in the above-described ranges, advantageous effects in the above-described calorific value and reaction area may be exhibited.

A co-catalyst may be provided on the catalyst foam substrate. The co-catalyst may catalyze a reaction to extract hydrogen from the hydrogen storage compound. The co-catalyst may be, for example, ruthenium (Ru). Ruthenium can promote the reaction of extracting hydrogen from a hydrogen storage compound, but it is difficult to use in large amounts because of its high price. In the case of the prior art, a large amount of ruthenium was used to increase the hydrogen production reaction efficiency, but in the present invention, ruthenium only functions as a co-catalyst, and it is possible to secure a commercially available hydrogen extraction reaction efficiency without ruthenium. However, when it is necessary to raise the efficiency of the hydrogen extraction reaction device higher than the commercial level, a co-catalyst such as ruthenium may be used together on the catalyst foam.

The co-catalyst may be intercalated on the surface of the catalyst foam substrate or provided in the form of a coating layer on the surface of the catalyst foam substrate.

Referring to FIG. 2 , it can be seen that the sub-catalyst is inserted on the surface of the catalyst foam substrate. As can be seen from the drawings, a part of the subcatalyst is inserted on the catalyst foam substrate and a portion of the subcatalyst is provided derived from the surface of the catalyst foam substrate. The subcatalyst may be provided uniformly dispersed on the surface of the catalyst foam substrate. The hydrogen storage material may react in the protruding region of the intercalated subcatalyst.

Referring to FIG. 3 , it can be seen that the subcatalyst is provided in the form of a coating layer on the surface of the catalyst foam substrate. In this case, the coating layer provided on the surface of the catalyst foam may include a coating substrate and a subcatalyst inserted on the coating substrate. The coating substrate may be, for example, aluminum oxide (Al ₂ O ₃ ) as shown in the drawings. However, the type of the coating substrate is not limited to the above-described material, and any material is possible as long as it has excellent thermal conductivity and does not react with a hydrogen storage material and hydrogen gas without affecting the activity of the subcatalyst.

When the sub-catalyst is provided in the form of a coating layer, a plurality of sub-catalysts may be inserted and provided in the coating substrate. For example, as shown in the drawings, a plurality of ruthenium is inserted into the surface of the aluminum oxide substrate, and the aluminum oxide may form a coating on the surface of the catalyst foam substrate.

When a co-catalyst is included, the hydrogen extraction reaction efficiency from the hydrogen storage compound may be further improved. However, when a metal such as ruthenium is used as a co-catalyst, the manufacturing cost of the reactor may increase, and the design of the reactor may become more complicated.

In the above, the hydrogen extraction reaction apparatus according to an embodiment of the present invention can perform hydrogen extraction with high efficiency without heat loss, including a reactor, a catalyst foam, and a heat source. A hydrogen extraction reaction apparatus may be used as part of an apparatus using hydrogen. For example, the hydrogen extraction reaction apparatus may be used as a part of a fuel cell using hydrogen. Hereinafter, a fuel cell including a hydrogen extraction reaction device will be described.

4 is a perspective view illustrating a fuel cell according to an embodiment of the present invention.

Referring to FIG. 4 , a fuel cell according to an embodiment of the present invention includes a hydrogen extraction reaction device 10 ; and a stack 20 for generating electricity by separating electrons from hydrogen gas among the gas generated from the hydrogen extraction reaction device 10, and the hydrogen extraction reaction device 10 includes a reaction for extracting hydrogen from a hydrogen storage compound reactor; Catalytic foam provided inside the reactor; and a heat source for providing heat to the catalyst foam, wherein the catalyst foam includes nickel (Ni), chromium (Cr) and aluminum (Al) and includes pores therein.

In the fuel cell, the details regarding the hydrogen extraction reaction device 10 are the same as those described above, and the description will be omitted below in order to avoid overlapping of the contents.

The stack 20 may be a device for generating electricity by sucking the hydrogen gas supplied from the hydrogen extraction reaction device 10 . The stack 20 may include an anode, an electrolyte, and an anode for this purpose.

Looking more closely at the operating principle of the stack 20 , the hydrogen gas provided from the hydrogen extraction reaction device 10 moves to the cathode to lose electrons and is converted into hydrogen ions (H ⁺ ) in the electrolyte. At this time, the electrons lost by the hydrogen gas move along the wiring connected to the cathode. At the anode separated by the cathode and electrolyte, hydrogen ions, oxygen, and electrons meet to form water. At this time, a potential difference is generated between the cathode and the anode, and a current flows along the wiring connected to the cathode and the anode.

However, the stack 20 included in the fuel cell according to the present invention is not limited to the above-described configuration. The fuel cell may be any type using hydrogen, and the structure of the stack 20 may vary accordingly. For example, the fuel cell may be a molten carbonate fuel cell (MCFC), and in this case, carbonate ions, not hydrogen ions, may move in the electrolyte in the stack 20 . Also, in another example, the fuel cell may be a solid oxide fuel cell, a phosphoric acid type fuel cell, or the like. The fuel cell may be implemented in any type as long as it uses hydrogen.

In the above, a hydrogen extraction reaction device and a fuel cell according to an embodiment of the present invention have been described. Hereinafter, we will look at the advantageous effects of the hydrogen extraction reaction apparatus according to the present invention in more detail based on the examples.

manufacturing example. Catalyst Foam Preparation

Preparation Example 1-1. Catalyst Foam Substrate Preparation

An open cell NiCrAl foam was used as the catalytic foam substrate. The catalytic foam substrate in the form of a sheet was cut into circular rods (diameter: 5 mm, length: 20 mm) through wire cutting.

Preparation 1-2, Preparation 1-3. Cocatalyst Catalyst Preparation

In Preparation Examples 1-2 and Preparation 1-3, in order to compare with the case where only the catalyst foam substrate was used, a subcatalyst was provided on the catalyst foam substrate. A ruthenium catalyst was used as a co-catalyst, and for this purpose, Ruthenium chloride hydrate (RuCl ₃ .xH ₂ O with Ru content 46.98 wt.%, Sigma Aldrich) was used as a Ru catalyst precursor.

Preparation 1-2. Cocatalyst Intercalation Catalyst Foam (iRu/NF)

A catalyst foam into which ruthenium is inserted, represented by iRu/NF, was prepared through wet impregnation using an aqueous RuCl ₃ solution. Specifically, RuCl ₃ .xH ₂ O powder was added to deionized water and mixed until a uniform solution was obtained. The solution was then carefully injected into the foam in such a way that maximum wetting of the foam surface was achieved. Impregnation was performed twice with drying at 100° C. under vacuum between each step.

Preparation Example 1-3. Cocatalyst Coated Catalyst Foam (cRu/NF)

To prepare a coated catalyst foam represented by cRu/NF, a ceramic support was impregnated with Ru, and then the surface of the catalyst foam substrate was coated with a ceramic support impregnated with Ru.

To this end, first, alumina pellets (γ-Al2O3, Alfa Aesar) were ground into particles with an average size of less than 500 μm. The pulverized alumina particles were then impregnated with Ru using an initial wet impregnation method. The impregnated catalyst particles were dried under vacuum at 100° C. for 12 hours.

Next, polyvinyl alcohol (PVA, Sigma Aldrich) was used as a matrix binder of catalyst particles to prepare a slurry. Specifically, 5 g of PVA beads were added to 75 g of deionized water and magnetically stirred at 60° C. for 2 hours. The viscous mixture was then left without stirring to allow it to settle overnight. The prepared Ru/Al ₂ O ₃ powder was added to a binder in a specific ratio to prepare a catalyst wash coat. The coating of the catalyst slurry on the catalyst foam was performed similarly to the impregnation procedure described in the iRu/NF Preparation Example.

Example 1. Catalytic Activity Analysis

5 is a result of analyzing the form and activity of a catalyst foam according to an embodiment of the present invention.

Referring to a of FIG. 5 , the forms of catalyst foam (bare NF), iRu/NF and cRu/NF in which a co-catalyst is not supported can be confirmed. Referring to the drawings, it can be seen that a nodular structure exists on the surface of the catalyst foam. The morphological properties of the powder catalyst used for cRu/NF preparation are also summarized in Fig. 5a'.

The X-ray diffraction diagram shown in FIG. 5 b shows the index peaks detected for the Ni ₃ Al phase on the surface of the catalyst foam, the Ru peak on the iRu/NF surface, and the Al ₂ O ₃ peak on the cRu/NF surface. Referring to the figure, typical peaks corresponding to Ru(111), (200) and (220) lattices were detected at 2θ of 44, 52 and 77, respectively. It means that Ru is electrodeposited on Ni foam.

The results of the in vitro test are shown in Fig. 5c. As can be seen here, it can be seen that the NH ₃ conversion increases with temperature, reaching a maximum ca of 68% at GHSV of 550 °C and 1000 mL/gCat/h for cRu/NF. The analyzed catalytic activity was shown in the order of cRu/N F > iRu/NF > NF.

Example 2. Analysis of hydrogen extraction reaction efficiency

Hydrogen extraction reaction efficiency was analyzed using the catalyst foams according to Preparation Examples 1-1 to 1-3 described above. Catalyst foams according to Preparation Examples 1-1 to 1-3 were provided in a hydrogen extraction reaction device using Joule heat.

An electrical bias was applied using a regulated DC power supply in the hydrogen extraction reactor. Catalyst foam samples were fixed to copper tubes at both ends of the reactor, and the copper tubes were used as conductive electrodes.

The hydrogen extraction reactor temperature was measured using three K-type thermocouples inserted into a quartz outer walled reactor at the feed gas inlet, center point and gas outlet.

The feed gas flow rate was adjusted using a thermal mass flow controller. The hydrogen extraction reactor was reduced for 2 hours before exposure to the hydrogen storage compound, NH ₃ .

6 is a graph analyzing the hydrogen extraction reaction efficiency of a hydrogen extraction reaction apparatus including a catalyst foam according to an embodiment of the present invention.

6 shows trends for NH ₃ conversion and reforming efficiency of iRu/NF (indicated by hollow markers) and cRu/NF (indicated by solid markers) reactors. Bare NF (indicated by a continuous black line in all graphs) shows relatively low conversion and reforming efficiency, but when checking the values shown in Bare NF, it was confirmed that the catalyst foam can be used commercially without a co-catalyst.

In general, it was confirmed that the conversion rate and the NH ₃ supply rate increased as the input power was increased. The highest NH ₃ conversion rate was found to be 99.99% or more in P _in 50W, GHSV 1827mL _NH3 / g _Foam /h (see FIGS. 6 a and b). In addition, as shown in c and d of FIG. 6 , it was confirmed that the reforming efficiency of the reactor increased as the input power increased.

As can be seen in FIG. 6 and Table 1, it was confirmed that, despite the low Ru loading of cRu/NF (less than half that of iRu/NF), the catalytic activity was somewhat similar and much higher at some points. This means that when the catalyst pre-impregnated on the coating substrate is used, the Ru particles can be better dispersed. Accordingly, it was confirmed that a hydrogen extraction reaction apparatus with excellent efficiency can be implemented even with a smaller amount of Ru. 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.

Claims (9)

a reactor in which a reaction for extracting hydrogen from the hydrogen storage compound is performed;
Catalytic foam provided inside the reactor; and
Containing a heat source (Heat Source) for providing heat to the catalyst foam,
The catalyst foam includes nickel (Ni), chromium (Cr) and aluminum (Al) and includes a void therein, a hydrogen extraction reaction device. According to claim 1,
The catalytic foam further comprises a catalytic foam substrate comprising nickel (Ni), chromium (Cr) and aluminum (Al) and a subcatalyst provided on the catalytic foam substrate. 3. The method of claim 2,
The subcatalyst comprises ruthenium (Ru), a hydrogen extraction reaction device. 3. The method of claim 2,
The subcatalyst is inserted on the surface of the catalytic foam substrate, or provided by being coated on the surface of the catalytic foam substrate in a form inserted on the coating substrate for forming a coating layer. According to claim 1,
The heat source is provided in the form of an electrode attached to the catalyst foam,
The electrode supplies an electric current to the catalytic foam so that Joule heating is generated from the catalytic foam. According to claim 1,
the hydrogen storage compound comprises ammonia,
In the reactor, a reaction in which hydrogen is extracted from the ammonia is performed, a hydrogen extraction reaction device. According to claim 1,
The reactor is provided in the form of a tube extending in one direction,
One side of the reactor is provided with the hydrogen storage compound,
Hydrogen is discharged to the other side of the reactor, a hydrogen extraction reaction device. 8. The method of claim 7,
The catalyst foam is provided to be filled along the extension direction of the reactor inside the reactor in the form of a tube, a hydrogen extraction reaction device. hydrogen extraction reactor;
A stack for generating electricity by separating electrons from hydrogen gas among the gas generated from the hydrogen extraction reaction device,
The hydrogen extraction reaction device is
a reactor in which a reaction for extracting hydrogen from the hydrogen storage compound is performed;
Catalytic foam provided inside the reactor; and
Containing a heat source (Heat Source) for providing heat to the catalyst foam,
The catalytic foam includes nickel (Ni), chromium (Cr) and aluminum (Al) and includes pores therein.

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