WO2024075890A1 - Functional catalytic reactor and fuel gas reforming device - Google Patents

Abstract

This functional catalytic reactor is installed in a fuel gas reforming device comprising: a first reactor that includes an electrode and reforms fuel to generate reformed gas; and a second reactor that re-reforms the reformed gas reformed by the first reactor. The functional catalytic reactor includes: a ventilation unit which has an accommodation space formed therein and through which the reformed gas reformed by the first reactor passes; a functional catalyst which is accommodated in the accommodation space of the ventilation unit and reacts with the reformed gas passing through the ventilation unit; and a hollow ventilation support which guides the reformed gas reformed by the first reactor toward the second reactor and supports the ventilation unit so that the vertical position of the ventilation unit can be adjusted.

Description

Functional catalytic reactor and fuel gas reforming device

The present invention relates to a functional catalytic reactor and fuel gas reforming device.

Due to the influence of rapid industrialization, the use of fossil fuels such as oil and coal is rapidly increasing. Accordingly, as problems such as environmental pollution and depletion of energy resources emerge, the need for research on new and renewable energy is emerging. In particular, hydrogen energy, one of the new renewable energies, is evaluated as a key energy source of the future due to its high energy density and almost no environmental pollution.

Hydrogen is generally produced by reforming hydrogen-containing fuels such as alcohol-based fuels (methanol, ethanol, etc.), hydrocarbon-based fuels (methane, butane, propane, etc.), natural gas-based fuels (liquefied natural gas, etc.), and biogas by a fuel reformer. obtained. These fuel reformers mainly use the steam reforming method. In a steam reforming type fuel reformer, hydrogen-containing fuel is supplied into the reformer along with water, and reacts with a catalyst within the reformer to produce hydrogen through a hydrogen production reaction. At this time, heat suitable for the reaction can be supplied by the burner. However, this steam reforming method involves a strong endothermic reaction, requires a high heat source, and has problems with slow start-up characteristics. In addition, there are various technical limitations such as catalyst poisoning from trace amounts of sulfur compounds, and as the size of the reformer increases, there is a problem of increased operation and maintenance costs.

Meanwhile, in order to compensate for this problem, the development of a fuel reformer that uses plasma to reform hydrogen-containing fuel is in progress. In a plasma reforming type fuel reformer, plasma-inducing gas is discharged by direct current power converted from alternating current power to generate high-temperature plasma, and the fuel is reformed using the generated high-temperature plasma. The conventional plasma reforming type fuel reformer has the problem of incurring additional costs because alternating current power must be converted back to direct current power.

To solve the above problems, the present applicant has proposed a composite fuel reforming system that combines two reforming methods. The composite fuel reforming system produces reformed gas by first reforming fuel through a first reforming reaction unit using plasma, and produces hydrogen by reforming the primary reformed gas again through a second reforming reaction unit using a catalyst. do. However, the plasma reforming reactor, which is the first reforming reaction unit of the composite fuel reforming system, has a problem in that the reforming efficiency of the catalytic reforming reactor, which is the second reforming reaction unit, is reduced due to low methane (CH ₄ ) conversion rate and high carbon dioxide (CO ₂ ) production. .

(Prior art literature)

(Patent Document 1) Korean Patent Publication No. 2390611

Embodiments of the present invention were invented in the above background, and are a functional catalyst reactor capable of improving the production performance of hydrogen and carbon monoxide by reducing carbon dioxide by reacting unreacted gas generated in the first reactor with a functional catalyst. We would like to provide.

The functional catalytic reactor according to one aspect of the present invention includes an electrode, a first reactor for reforming fuel to generate reformed gas, and a second reactor for reforming the reformed gas again by the first reactor. A functional catalytic reactor installed in a fuel gas reforming device, comprising: a ventilation portion through which the reformed gas reformed by the first reactor passes and a receiving space is formed therein; and a functional catalyst accommodated in the accommodation space of the ventilation unit and reacting with the reformed gas passing through the ventilation unit. It guides the reformed gas reformed by the first reactor to the second reactor and includes a hollow vent supporter supporting the vent so that the vertical position of the vent can be adjusted.

Additionally, the ventilation portion support is formed to surround the electrode, and the electrode may communicate with the outside through the ventilation portion.

In addition, the ventilation unit may include: a first ventilation unit installed at an end of the ventilation unit support at the second reactor side and having a plurality of ventilation holes for the reformed gas reformed by the first reactor to pass through; and is installed on the inside of the ventilation portion support so as to be spaced apart from the first ventilation portion to create the receiving space between the first ventilation portion and the reformed gas reformed by the electrode of the first reactor passes through. It may include; a second ventilation portion in which a plurality of ventilation holes are formed to

In addition, the first reactor is configured to generate plasma for use as a reforming means, and the ventilation portion passes through the reformed gas reformed by the first reactor at a temperature of 600°C to 900°C. It can be installed at any point.

In addition, the functional catalyst is Ni/BaZrO ₃ having a perovskite structure. It can be.

A fuel gas reforming device according to another aspect of the present invention includes a first reactor including an electrode and reforming fuel to generate reformed gas; a second reactor that re-reforms the reformed gas reformed by the first reactor; and a functional catalytic reactor that reacts the unreacted gas generated in the first reactor, wherein the functional catalytic reactor passes the reformed gas reformed by the first reactor, and a ventilation portion in which a receiving space is formed. ; and a functional catalyst accommodated in the accommodation space of the ventilation unit and reacting with the reformed gas passing through the ventilation unit. It guides the reformed gas reformed by the first reactor to the second reactor and includes a hollow vent supporter supporting the vent so that the vertical position of the vent can be adjusted.

According to embodiments of the present invention, there is an effect of improving the production performance of hydrogen and carbon monoxide by reducing carbon dioxide by reacting unreacted gas generated in the first reactor with a functional catalyst.

Figure 1 is a schematic diagram showing a fuel gas reforming device in which a functional catalytic reactor is installed according to an embodiment of the present invention.

Figure 2 is a cross-sectional view showing a fuel gas reforming device in which a functional catalytic reactor is installed according to an embodiment of the present invention.

Figure 3 is a diagram showing a functional catalytic reactor according to an embodiment of the present invention.

Hereinafter, specific embodiments for implementing the technical idea of the present invention will be described in detail with reference to the drawings.

In addition, when describing the present invention, if it is determined that a detailed description of a related known configuration or function may obscure the gist of the present invention, the detailed description will be omitted.

In addition, when a component is mentioned as being 'connected', 'supported', 'connected', 'supplied', 'delivered', or 'contacted' with another component, it is directly connected, supported, connected, or connected to that other component. It may be supplied, delivered, or contacted, but it should be understood that other components may exist in the middle.

The terms used in this specification are merely used to describe specific embodiments and are not intended to limit the invention. Singular expressions include plural expressions unless the context clearly dictates otherwise.

In addition, it should be noted in advance that expressions such as upper, lower, and side in this specification are explained based on the drawings, and may be expressed differently if the direction of the object in question changes. For the same reason, in the accompanying drawings, some components are exaggerated, omitted, or schematically shown, and the size of each component does not entirely reflect the actual size.

Additionally, terms including ordinal numbers, such as first, second, etc., may be used to describe various components, but the components are not limited by these terms. These terms are used only to distinguish one component from another.

As used in the specification, the meaning of "comprising" is to specify a specific characteristic, area, integer, step, operation, element and/or component, and to specify another specific property, area, integer, step, operation, element, component and/or group. It does not exclude the existence or addition of .

Hereinafter, the specific configuration of a functional catalytic reactor according to an embodiment of the present invention will be described with reference to FIGS. 1 to 3.

Before explaining the functional catalytic reactor according to an embodiment of the present invention, a fuel gas reforming device in which the functional catalytic reactor is installed will be described.

The fuel gas reforming device 1 may include a reactor 10, a burner unit 20, a first reactor 30, a heat exchange unit 40, and a second reactor 50.

The reactor 10 may provide an internal space in which the burner unit 20, the first reactor 30, the heat exchange unit 40, and the second reactor 50 can be placed. For this purpose, the reactor 10 includes a first reaction body 11 and a first reactor 11 in which at least one of the burner unit 20, the first reactor 30, the heat exchange unit 40, and the second reactor 50 is disposed. It is coupled to the reaction body 11 and may include a second reaction body 12 in which the remainder of the burner unit 20, the first reactor 30, the heat exchange unit 40, and the second reactor 50 are disposed. there is. Hereinafter, for convenience of explanation, the first reactor 30 is disposed in the first reaction body 11, and the burner unit 20, the heat exchanger 40, and the second reactor ( 50) is placed as an example.

The first reaction body 11 has a first reactor 30 disposed therein, a first reaction body side accommodating portion 111 having an open top, and an opening of the first reaction body side accommodating portion 111. It may include a first reaction body-side coupling portion 112 connected to the upper part of the body, and a guide member 113 connected to the inner surface of the first reaction body-side coupling portion 112. At this time, the first reaction body-side accommodating portion 111, the first reaction body-side coupling portion 112, and the guide member 113 may be formed integrally, and the first reaction body-side accommodating portion 111 and the first reaction body-side accommodating portion 111 1 The reaction body side coupling portion 112 and the guide member 113 may be manufactured separately and then coupled to each other. At this time, an inlet 1111 may be connected to the bottom of the first reaction body side receiving portion 111. Fluids to be reformed, such as fuel or plasma-inducing gas, may flow through this inlet 1111, and the introduced fluids may be supplied between electrodes 31 of the first reactor 30, which will be described later. The guide member 113 may guide the reformed gas flowing out of the first reactor 30 to the second reactor 50. The guide member 113 extends from the lower surface of the first reaction body side coupling portion 112 toward the bottom surface of the first reaction body side receiving portion 111, thereby forming a predetermined space therein. At least a portion of the first reactor 30 may be placed in the inner space of the guide member 113 formed in this way and covered by the guide member 113.

The second reaction body 12 has a burner unit 20, a heat exchanger 40, and a second reactor 50 disposed therein, and includes a second reaction body side receiving portion 121 having an open bottom shape, and It may include a second reaction body side coupling portion 122 connected to the open lower portion of the second reaction body side receiving portion 121. At this time, the second reaction main body side accommodating part 121 and the second reaction main body side coupling part 122 may be formed integrally, and the second reaction main body side accommodating part 121 and the second reaction main body side coupling part ( 122) may be manufactured separately and then combined together. At this time, a connection member 1211 may be provided on the inner surface of the second reaction body side receiving portion 121. At least one of the heat exchanger 41, the burner unit 20, and the second reactor 50 may be connected to this connection member 1211.

Meanwhile, the first reaction body side coupling portion 112 of the first reaction body 11 and the second reaction main body side coupling portion 122 of the second reaction body 12 are connected by separate fastening means (not shown). can be mutually concluded. In this case, the first through hole 1121 formed in the first reaction body side coupling portion 112 of the first reaction body 11 and the second reaction body side coupling portion 122 of the second reaction body 12 The second through-holes 1221 previously formed may be in communication with each other. The first through-holes 1121 and the second through-holes 1221 communicated with each other in this way are used to supply the first reformed gas generated in the first reactor 30 to the heat exchanger 41 of the heat exchanger 40. It can be used as a passage. To this end, the end of the heat exchanger 41 of the heat exchanger 40 may be connected to a position corresponding to the first through hole 1121 and the second through hole 1221.

The burner unit 20 transfers heat to the heat exchange unit 40 to preheat the first reformed gas to a first temperature, and transfers heat to the second reactor 50 to preheat the first reformed gas to the first temperature. The gas may be heated to a second temperature that is higher than the first temperature. In other words, when the heat of the burner unit 20 is transferred to the heat exchange unit 40, the first reformed gas supplied to the heat exchange unit 40 is preheated to the first temperature by the heat of the burner unit 20, and the burner unit 20 When the heat from 20 is transferred to the second reactor 50, the preheated first reformed gas supplied to the second reactor 50 may be heated to the second temperature. Here, the first reformed gas refers to a gas produced by reforming fuel by the first reactor 30. Furthermore, the first reformed gas heated to the second temperature may be reformed by the second reactor 50, which will be described later, and converted into the second reformed gas. Here, the first temperature may be about 650°C to about 700°C, and the second temperature may be about 800°C to about 850°C.

The burner unit 20 may be provided inside the reactor 10, for example, inside the second reaction body 12. This burner unit 20 may be inserted into a hole previously formed in the second reaction body 12 and may be supported by a connection member 1211 coupled to the inner surface of the second reaction body 12. For this purpose, support pieces 21 may be formed to protrude along the circumference of the burner unit 20, and these support pieces 21 may be in surface contact with the connection member 1211.

At this time, the burner unit 20 may, for example, be provided as a cylindrical structure with a predetermined space formed therein to correspond to the shape of the inner peripheral surface of the second reaction body 12. At this time, in order to uniformly supply the heat of the burner unit 20 to the heat exchange unit 40 and the second reactor 50, the burner unit 20 has an internal cylindrical off gas to which metal fiber is applied, for example. It may be provided with a burner. Accordingly, the amount of heat required to preheat the first reformed gas in the heat exchanger 40 through the burner unit 20 and the amount of heat required to reform the first reformed gas preheated in the second reactor 50 will be supplied uniformly at the same time. You can.

The first reactor 30 may convert fuel into a first reformed gas. For this purpose, the first reactor 30 may be provided inside the reactor 10, for example, inside the first reaction body 11, and may include a first reforming means capable of reforming fuel supplied from the outside. Can be created optionally. Here, the fuel may be a hydrogen-containing fuel such as alcohol-based fuel, hydrocarbon-based fuel, natural gas-based fuel, or biogas, and the first reforming means may be gliding arc plasma. This first reactor 30 may include an electrode 31, an electrode support 32, and a power supply (not shown).

The electrode support 32 extends upward from the bottom of the first reaction body side accommodating portion 111, and the electrode 31 may be coupled to and supported at the top.

The electrode 31 may be supported by being coupled to an electrode support 32 that is coupled to the first reaction body side receiving portion 111. For example, the electrode 31 may be provided in a fan-shaped shape including a curved line. At this time, a plurality of electrodes 31 can be provided to increase the plasma discharge area. For example, the plurality of electrodes 31 may be arranged to be spaced apart at a predetermined interval so that the gap between the electrodes 31 widens toward the top. The electrode 31 is electrically connected to the power supply device and can receive alternating current power from the power supply device. After fuel and plasma inducing gas for inducing gliding arc plasma are introduced between the electrodes 31 through the inlet 1111 provided in the first reaction body side receiving portion 111, AC power is applied to the electrodes 31. Then, discharge starts at the bottom where the distance between the electrodes 31 is shortest. The arc generated in this way slides and moves upward due to the flow of plasma inducing gas supplied from the bottom and the buoyancy of the high-temperature arc. When the plasma reaches the top of the electrode 31, the plasma that moves upward is extinguished at the last part of the electrode 31. When the arc disappears, at the same time the gap between the electrodes 31 is re-ignited at the closest part, and this phenomenon is maintained repeatedly. The plasma generated in this way can be used as a reforming means to reform fuel.

The heat exchange unit 40 may receive the first reformed gas from the first reactor 30, and transfer heat from the burner unit 20 to the first reformed gas supplied from the first reactor 30 to perform the first reformed gas. The gas may be preheated to a first temperature. To this end, the heat exchange unit 40 may be disposed inside the reactor 10, for example, inside the second reaction body 12. At this time, at least some of the plurality of heat exchangers 41 are arranged to be offset from at least some of the plurality of second reforming reactors 51 of the second reforming reaction unit 50, which will be described later, so that the radiant heat of the burner unit 20 It can be easily transferred to a plurality of heat exchangers 41. This heat exchange unit 40 may include a plurality of heat exchangers 41. The plurality of heat exchangers 41 may be arranged to be spaced apart along an imaginary circle with a certain radius based on the center of the burner unit 20. The heat exchanger 41 may have a passage inside through which the first reformed gas can flow. At this time, one end of the heat exchanger 41 may be coupled to the inner surface of the second reaction body side coupling portion 122 of the second reaction body 12. In this case, one end of the heat exchanger 41 has a first through hole 1121 formed in the first reaction body side coupling portion 112 of the first reaction body 11 and a second through hole 1121 of the second reaction body 12. It may be in communication with the second through hole 1221 already formed in the reaction body side coupling portion 122. As a result, the passage provided inside the heat exchanger 41 communicates with the internal space of the first reaction body 11, so that the first reformed gas of the first reaction body 11 is supplied to the heat exchanger 41. You can. The other end of the heat exchanger 41 may be coupled through a hole already formed in the connection member 1211 coupled to the inner surface of the second reaction body side receiving portion 121. At this time, an extension piece may be formed extending from one surface of the connecting member 1211 corresponding to the outer circumference of the hole. This extension piece can cover a hole already formed in the connecting member 1211. As a connection pipe is connected to the extension piece, the first reformed gas discharged through the other end of the heat exchanger 41 can be supplied to the second reactor 50 through the connection pipe.

The second reactor 50 may convert the first reformed gas that has passed through the heat exchanger 40 into a second reformed gas. To this end, the second reactor 50 may be equipped with a second reforming means that is different from the first reforming means. To this end, the second reactor 50 may be disposed inside the reactor 10, for example, inside the second reaction body 12. At this time, at least a portion of the plurality of second reaction units 51 is arranged to be offset from at least a portion of the plurality of heat exchangers 41, so that the radiant heat of the burner unit 20 is easily transferred to the plurality of second reaction units 51. can be conveyed. This second reactor 50 may include a plurality of second reaction units 51. The plurality of second reaction units 51 may be spaced apart from each other along an imaginary circle with a certain radius based on the center of the burner unit 20. Here, the second reactor 50 is disposed closer to the burner unit 20 than the heat exchange unit 40, so that the plurality of second reaction units 51 form a circle based on the center of the burner unit 20. The size may be smaller than the size of the circle formed by the plurality of heat exchangers 41 based on the center of the burner unit 20. The second reactor 50 may include an exterior 511 and an inner tube 512 disposed inside the exterior 511. At this time, the lower end of the outer tube 511 may be closed, and the lower end of the inner tube 512 may be provided in an open structure. Accordingly, a second reforming means, for example, a reforming catalyst, may be provided between the outer tube 511 and the inner tube 512. In this way, as the second reactor 50 is provided in the form of a double tube including an outer tube 511 and an inner tube 512, the residence time of the first reformed gas can be increased. The outer pipe 511 is provided with a first passage 5112 through which the first reformed gas flows, and the inner pipe 512 is in communication with the first passage 5112, and at least one of the first reformed gas and the second reformed gas is provided. A flowing second passage 5122 may be provided. When the radiant heat of the burner unit 20 is transferred to the exterior 511, heat exchange between the radiant heat of the burner unit 20 and the first reformed gas proceeds, and the radiant heat supplied through the inlet 5111 connected to the top of the exterior 511 is A reforming reaction proceeds as the first reforming gas passes through a second reforming means, for example, a reforming catalyst, provided between the outer tube 511 and the inner tube 512. The temperature of the first reformed gas moved to the bottom of the outer tube 511 is higher than the temperature of the first reformed gas supplied to the top of the outer tube 511, and the raised first reformed gas rises through the inner tube 512, which is a riser tube. After being converted to the second reformed gas, it is discharged through the outlet 5121 connected to the top of the inner tube 512.

In the above-described fuel gas reforming device, fuel is first reformed in the first reactor 30, preheated to a temperature at which a reforming reaction can occur through the heat exchanger 40, and then secondarily reformed in the second reactor 50. Reforming improves reforming efficiency.

However, as shown in Table 1, the primary reformed gas primary reformed by the first reactor 30 has a low conversion rate of methane (CH ₄ ) and a high amount of carbon dioxide (CO ₂ ) generated in the second reactor 50. ) There is a problem that the reforming efficiency of is reduced.

ingredient	H 2	CH 4	C.O.	CO2	C 2 H 4	C 2 H 6	C 2 H 2	C 3 H 8
content (%)	23.75	33.45	14.1	28.02	0.11	0.05	0.52	0.001

To solve this problem, a functional catalytic reactor 60 is formed between the first reactor 30 and the second reactor 50, and unreacted methane and carbon dioxide of the primary reformed gas reformed by the first reactor 30 are formed. The reforming efficiency of the second reactor 50 can be increased by producing more hydrogen by performing a methane reforming reaction (DRM, Dry Reforming of Methane) using the functional catalytic reactor 60. The functional catalytic reactor 60 according to an embodiment of the present invention extends from the bottom of the first reaction body side receiving portion 111 to the upper side, that is, toward the second reactor 50, and is used by the first reactor 30. It is installed at the end of the second reactor 50 side of the ventilation portion support 61 that guides the reformed reformed gas toward the second reactor 50, and allows the reformed gas reformed by the first reactor 30 to pass through and is accommodated therein. It includes a ventilation portion 62 in which a space is formed and a functional catalyst 63 that is accommodated in the internal accommodation space of the ventilation portion 62 and reacts with the reformed gas passing through the ventilation portion 62.

The ventilation portion support 61 has a hollow cylindrical shape, and a space is formed therein, so that the first reactor 30 can be placed in this inner space. The ventilation portion support 61 may extend upward from the bottom of the first reaction body side receiving portion 111 to provide a space in which the fuel to be reformed and the plasma inducing gas for inducing the gliding arc plasma flow. A plasma reforming reaction may be performed in the internal space formed in the ventilation portion support 61. The ventilation portion support 61 may be made of a material that can be electrically insulated from the electrode 31.

The lower part of the ventilation portion support 61 (lower part in FIG. 2) extends upward from the bottom of the first reaction body side receiving portion 111, and the upper part of the ventilation portion support 61 (upper part in FIG. 2) is open. A ventilation portion 62 may be installed on one open side. That is, the ventilation portion support 61 surrounds the first reactor 30 so that the portion excluding the upper open side of the ventilation portion support 61 where the ventilation portion 62 is formed blocks the first reactor 30 from the outside. It can be formed as follows. Because of this, all of the reformed gas reformed through the first reactor 30 passes through the ventilation portion 62.

The ventilation portion support 61 may be disposed radially inside the guide member 113. The horizontal separation distance between the ventilation unit support 61 and the guide member 113 may be smaller than the horizontal separation distance between the ventilation unit support 61 and the side wall of the first reaction body side receiving portion 111. You can. In addition, the separation distance between the upper end of the electrode 31 and the upper end of the ventilation support 61 can be formed to be larger than the separation distance between the lower end of the electrode 31 and the bottom of the first reaction body side accommodating portion 111. there is.

The ventilation unit 62 may be installed on the upper part of the ventilation unit support 61 and may be formed of a mesh member having a plurality of ventilation holes for the reformed gas reformed by the first reactor 30 to pass through, and the ventilation unit ( It may include a first ventilation portion 621 and a second ventilation portion 622 spaced apart at a predetermined interval along the thickness direction of 62). The first vent 621 and the second vent 622 may be installed inside the vent support 61. The first ventilation portion 621 and the second ventilation portion 622 are formed to have an area corresponding to the cross-sectional area of the internal space formed by the ventilation portion support 61 to close one open side of the ventilation portion support 61. Can be installed. At this time, the first ventilation part 621 and the second ventilation part 622 may be spaced apart at a certain interval to create an accommodation space therebetween. One open side of the vent supporter 61 is closed by the first vent 621 and the second vent 622, but the first vent 621 and the second vent 622 have a plurality of vents. Pores are formed so that the reformed gas guided through the ventilation portion supporter 61 passes through the first ventilation portion 621 and the second ventilation portion 622.

The reformed gas generated from the first reactor 30 passes through the ventilation portion 62 and then flows downward along the space formed between the guide member 113 and the ventilation portion support 61, and flows downward toward the first reaction body. After rising through the space formed between the side wall of the receiving part 111 and the guide member 113, it may flow into the heat exchange part 40. According to this flow path, the reformed gas generated in the first reactor 30 may flow into the heat exchange unit 40 without remaining inside the first reaction body 11.

Meanwhile, the functional catalyst 63 is accommodated in the receiving space formed between the first ventilation portion 621 and the second ventilation portion 622 and reacts with the reformed gas passing through the ventilation portion 62. At this time, the reforming gas and the functional catalyst 63 undergo methane reforming reaction (DRM), and reaction heat of 600°C to 900°C is required for the metal reforming reaction to occur. Since the first reactor 30 reforms fuel by plasma, the reformed gas reformed by the first reactor 30 is maintained at a high temperature.

Therefore, the ventilation portion 62 must be installed at a location where the reformed gas maintains a high temperature, that is, a point through which the reformed gas can pass while its temperature is between 600°C and 900°C. Since the ventilation portion 62 is installed at one open end of the ventilation portion support 61, the length of the ventilation portion support 61 is adjusted to adjust the ventilation portion 62 so that the temperature of the reformed gas is 600°C to 900°C. It can be installed at a point where it passes through at °C. In addition, the length of the ventilation portion support 61 is formed to be long, and predetermined fastening means, such as a rack and pinion gear, are provided on the inner surface of the ventilation portion support 61 and the outer surface of the ventilating portion, respectively, to secure the ventilation portion. (62) can be installed inside the ventilation portion support 61 so that the ventilation portion 62 is installed at a point where the reformed gas passes through at a temperature of 600°C to 900°C. In this case, the ventilation portion 62 can be installed at the corresponding location regardless of the total length of the ventilation portion support 61. That is, the ventilation portion support 61 adjusts its overall length or adjusts the vertical position of the ventilation portion 62 disposed inside the ventilation portion 62 so that the temperature of the reformed gas is maintained at 600°C to 900°C. It can be installed at a point where it passes through at °C.

The vertical separation distance between the ventilation portion 62 and the first reaction body side coupling portion 112 is greater than the separation distance between the lower end of the guide member 113 and the bottom of the first reaction body side receiving portion 111. You can.

Meanwhile, the functional catalyst 63 may be Ni/BaZrO ₃ having a perovskite structure. The functional catalyst 63 uses BaZrO ₃ as a support, and is a catalyst coated with nickel on BaZrO ₃ powder prepared by a solid-phase method and a pellet-shaped BaZrO ₃ structure manufactured by extrusion molding. Looking at the method of manufacturing the functional catalyst 63, first, the precursors are barium carbonate (BaCO _{3 ,} 99.9%), zirconium oxide (ZrO ₂ , 99.9%), yttrium oxide (Y ₂ O ₃ , 99.9%), and acetone. Mix and homogenize. The mixed materials as described above are dried and ground at 110°C, then heat-treated in air at 1200°C for 5 hours, and the heat-treated material is ground into uniform powder using an attrition milling. The BaZrO ₃ powder prepared in this way may be a structure having a specific surface area of 10 m ² /g to 20 m ² /g. Next, the metal precursor is coated on BaZrO ₃ powder through temperature-controlled chemical vapor deposition. Here, Ni(Cp) ₂ may be used as the metal precursor, and the metal precursor is injected at 1 wt% to 30 wt% based on the weight of the BaZrO ₃ carrier (BaZrO ₃ powder or BaZrO ₃ gear-type pellets) to form a surface of the BaZrO ₃ carrier. The content of nickel (Ni) coated on can be controlled. For the deposition of nickel, nickel vapor in the form of an organic metal compound sublimated at a temperature of 250 ℃ reacts with oxygen in the air on the surface of the BaZrO ₃ carrier to coat it in the form of NiO, and is coated in the form of NiO at 800 ℃ (reducing atmosphere) for 2 to 4 hours. A functional catalyst (63) made of Ni/BaZrO ₃ is prepared by heat treatment. The functional catalyst (63), Ni/BaZrO ₃ , has high performance in methane reforming reaction (DRM) and a structurally stabilized perovskite structure, enabling steam It has high stability in (steam) atmosphere. Accordingly, the unreacted methane (CH ₄ ), carbon dioxide (CO ₂ ), and CxHx series gases generated in the first reactor 30 are supplied to the functional catalytic reactor 60 and are combined with the plasma heat source of the first reactor 30. The reforming efficiency of fuel can be increased by increasing the production of hydrogen (H ₂ ) and carbon monoxide (CO) through methane reforming reaction (DRM).

Although embodiments of the present invention have been described above as specific embodiments, this is merely an example, and the present invention is not limited thereto, and should be construed as having the widest scope following the technical idea disclosed in this specification. A person skilled in the art may implement a pattern of a shape not specified by combining/substituting the disclosed embodiments, but this also does not depart from the scope of the present invention. In addition, a person skilled in the art can easily change or modify the embodiments disclosed based on the present specification, and it is clear that such changes or modifications also fall within the scope of the present invention.

(National research and development project that supported this invention)

(Unique assignment number) 1545025291

(Assignment number) 421045032SB010

(Ministry Name) Ministry of Agriculture, Food and Rural Affairs

(Project management (professional) organization name) Agriculture, Food and Rural Technology Planning and Evaluation Institute

(Research Project Name) Smart Farm Multi-Ministry Package Innovation Technology Development Project

(Research project title) Development of biogas pretreatment and hydrogen conversion technology

(Contribution rate) 1/1

(Name of project carrying out organization) Advanced Technology Research Institute Research Association

(Research period) 2022.01.01 ~ 2022.12.31

Claims (6)

1. A functional catalytic reactor installed in a fuel gas reforming device including an electrode, a first reactor for reforming fuel to produce reformed gas, and a second reactor for reforming the reformed gas again by the first reactor. ,

   a ventilation portion that passes the reformed gas reformed by the first reactor and has a receiving space therein;

   a functional catalyst accommodated in the accommodation space of the ventilation unit and reacting with the reformed gas passing through the ventilation unit; and

   Guiding the reformed gas reformed by the first reactor to the second reactor and comprising a hollow ventilation portion supporter supporting the ventilation portion so that the vertical position of the ventilation portion can be adjusted,

   Functional catalytic reactor.
2. According to claim 1,

   The ventilation portion support is formed to surround the electrode, and the electrode communicates with the outside through the ventilation portion,

   Functional catalytic reactor.
3. According to claim 1,

   The ventilation part,

   a first ventilation portion installed at an end of the ventilation portion support toward the second reactor and having a plurality of ventilation holes through which the reformed gas reformed by the first reactor passes; and

   It is installed inside the ventilation portion support so as to be spaced apart from the first ventilation portion to create the receiving space between the first ventilation portion and allow the reformed gas reformed by the electrode of the first reactor to pass through. Includes a second ventilation portion in which a plurality of ventilation holes are formed for

   Functional catalytic reactor.
4. According to claim 1,

   The first reactor is configured to generate plasma for use as a reforming means,

   The ventilation unit is installed at a point where the reformed gas reformed by the first reactor passes through at a temperature of 600°C to 900°C.

   Functional catalytic reactor.
5. According to claim 1,

   The functional catalyst is Ni/BaZrO ₃ having a perovskite structure,

   Functional catalytic reactor.
6. A first reactor including an electrode and reforming fuel to generate reformed gas;

   a second reactor that re-reforms the reformed gas reformed by the first reactor; and

   It includes a functional catalytic reactor that reacts the unreacted gas generated in the first reactor,

   The functional catalytic reactor includes a ventilation portion through which the reformed gas reformed by the first reactor passes and a receiving space is formed therein; and

   a functional catalyst accommodated in the accommodation space of the ventilation unit and reacting with the reformed gas passing through the ventilation unit;

   Guiding the reformed gas reformed by the first reactor to the second reactor and comprising a hollow ventilation portion supporter supporting the ventilation portion so that the vertical position of the ventilation portion can be adjusted,

   Fuel gas reforming device.

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