KR20170135189A - Fuel reforming divice - Google Patents

Abstract

A fuel reforming apparatus according to the present invention comprises: a combustion chamber in which a burner is installed; an exhaust flow path through which exhaust gas generated in the combustion chamber is circulated; a reforming reactor which is surrounded by the exhaust flow path and absorbs heat from exhaust gas flowing through the exhaust flow path to convert natural gas into hydrogen; a conversion reactor which is disposed in a lower side of the reforming reactor, converts carbon monoxide produced together with hydrogen into carbon dioxide, and emits heat; and a heat transfer unit which surrounds the reforming reactor and conversion reactor, in which a working fluid for transferring heat through a phase change is provided, which absorbs heat from the reforming reactor by the working fluid to transfer the absorbed heat to the conversion reactor. Therefore, the fuel reforming apparatus according to the present invention can improve reforming performance and simplify design of the burner by enabling operating temperatures of the reforming reactor and the conversion reactor to be controlled easily and accurately.

Description

[0001] FUEL REFORMING DIVICE [0002]

The present invention relates to a fuel reforming apparatus for reforming a hydrocarbon-based raw material to produce hydrogen.

BACKGROUND ART Generally, a fuel reforming apparatus is a kind of reformer that generates hydrogen by reforming a raw material gas such as city gas, LPG, or natural gas. Steam reforming is widely known.

The steam reforming process includes a reforming reactor (steam reformer) for converting the feed gas into hydrogen, a conversion reactor (a high temperature conversion reactor (HTS), a low temperature conversion reactor (LTS)) for converting the carbon monoxide generated with hydrogen into carbon dioxide to lower the concentration of carbon monoxide, And a burner for supplying heat.

For example, when natural gas whose main component is methane (CH4) is a raw material gas, the natural gas reacts with water vapor in a reforming reactor to produce hydrogen and carbon monoxide. However, when carbon monoxide is introduced into the fuel cell stack, the stack may be contaminated and the performance of the stack may be seriously degraded. Therefore, the carbon monoxide generated through the reforming reactor is converted into carbon dioxide by using a high temperature conversion reactor (HTS) and a low temperature conversion reactor (LTS).

Here, the operating temperature in the reforming reactor varies depending on the kind of catalyst, but when nickel (Ni) is used, it is usually about 700 to 800 ° C. The reaction is an endothermic reaction (endothermic reaction) . The operating temperature in the conversion reactor also varies depending on the type of the catalyst, but in the case of a high-temperature conversion reactor using copper-zinc (Cu-Zn), it is usually about 300 to 420 ° C. and iron- In the case of a low-temperature conversion reactor, it is usually about 235 to 300 ° C, and this conversion reaction is exothermic in the reaction due to exothermic reaction.

Meanwhile, the conventional fuel treatment apparatus can be divided into a horizontal (or radial) and a vertical (or vertical) type depending on the arrangement of the reforming reactor and the switching reactor.

In the horizontal type, a reforming reactor is located inside, a conversion reactor is located outside, and a combustion chamber in which a burner is provided is located inside the reforming reactor, that is, at the innermost side of the fuel processor. In the horizontal type, the combustion gas generated in the combustion process passes through the channel between the reforming reactor and the combustion chamber of the fuel processor and flows out from below while supplying heat to the reforming reactor. At this time, the raw material gas passes through the reforming reactor, moves from the top to the bottom of the fuel processor, and then passes through the reforming reactor and is transported to the bottom of the fuel processor.

In the horizontal type, a heat transfer tube (or a cooling tube) is provided outside the conversion reactor so that the conversion reactor can be heated or cooled to maintain an appropriate temperature.

In the conventional horizontal type fuel processing apparatus, the reforming reactor and the switching reactor are radially arranged, so that the internal structure and the flow path of the fuel processing apparatus are complicated and the volume of the entire reactor is increased.

On the other hand, in the bell shape, the reforming reactor is located on the upper side, the reforming reactor is located on the lower side of the reforming reactor, and the combustion chamber in which the burner is provided is located inside the reforming reactor and the conversion reactor. In such a bell-shaped mold, combustion gas passes through the flow path between the inner circumferential surface of the reactor and the combustion chamber, the flow path between the outer circumferential surface of the reactor and the outer wall surface, In this process, the combustion gas supplies heat to the reforming reactor and the conversion reactor.

The conventional bell-type fuel processing apparatus as described above can be further downsized and simplified in internal structure and flow path as compared with the horizontal type fuel processing apparatus. However, unlike the horizontal type fuel processing apparatus, depending on the burner, It is difficult to design the burner. Therefore, the bell-type fuel processing apparatus has a considerable difficulty in realizing actual commercialization.

It is an object of the present invention to provide a fuel reforming apparatus capable of easily and accurately controlling each operating temperature of a reforming reactor and a reforming reactor having different temperature gradients to thereby improve the reforming performance.

Another object of the present invention is to provide a fuel reforming device which can be arranged in the longitudinal direction and capable of making the heat source supplying heat to the reforming reactor different from that of the reforming reactor having different temperature gradient.

Another object of the present invention is to provide a fuel reforming apparatus which can simplify the design of the burner.

Another object of the present invention is to provide a fuel reforming apparatus capable of supplying heat generated in a burner to a reforming reactor and allowing a conversion reactor to utilize heat generated in a reforming reactor.

In order to achieve the object of the present invention, a fuel reforming apparatus having a heat transfer member to absorb heat in a reactor having a relatively high operating temperature and to transfer the heat to a reactor having a relatively low operating temperature may be provided.

Here, the reactor having a high operating temperature may be located above the reactor having a low operating temperature.

A reactor having a high operating temperature can receive heat by using a burner.

The catalyst layer having a relatively low operating temperature has a plurality of catalyst layers, and the plurality of catalyst layers are arranged separately in the longitudinal direction. Among the plurality of catalyst layers, the catalyst layer having a relatively high operating temperature is located above the catalyst layer having a low operating temperature Can be located.

The heat transfer member is in contact with a catalyst layer having a relatively low operating temperature among a plurality of catalyst layers, and the catalyst layer having a relatively high operating temperature can be cooled by a separate cooling unit while being supplied with heat using a burner.

In order to achieve the object of the present invention, a reactor having a relatively high operating temperature may receive heat by convection, and a reactor having a relatively low operating temperature may be provided with a fuel reforming apparatus that receives heat by conduction .

Here, a plurality of catalyst layers having different operating temperatures are arranged in the longitudinal direction of the reactor having a relatively low operating temperature, and a catalyst layer having a low operating temperature among the plurality of catalyst layers is connected to the reactor through the heat transfer material To receive heat.

In order to achieve the object of the present invention, there is provided a burner comprising: a combustion chamber in which a burner is installed; An exhaust passage through which the combustion gas generated in the combustion chamber circulates; A reforming reactor surrounded by the exhaust passage and absorbing heat from a combustion gas flowing through the exhaust passage to convert natural gas into hydrogen; A reforming reactor disposed below the reforming reactor for converting carbon monoxide generated with hydrogen into carbon dioxide and dissipating heat; And a heat transfer unit surrounding the reforming reactor and the reforming reactor and having a working fluid for transferring heat through a phase change therein to absorb heat in the reforming reactor by the working fluid and transfer the heat to the reforming reactor, The fuel reforming device can be provided.

Here, the inlet of the exhaust passage may communicate with the upper end of the combustion chamber, and the outlet of the exhaust passage may be formed at a position higher than the lower end of the conversion reactor.

The conversion reactor may be formed of a single catalyst layer, and the outlet of the exhaust passage may be formed at a height where the reforming reactor and the conversion reactor are in contact with each other.

The high-temperature conversion reactor is connected to the reforming reactor and the high-temperature conversion reactor and the low-temperature conversion reactor are arranged in the longitudinal direction. The high-temperature conversion reactor and the low- The outlet of the flow path may be formed at a position where the high temperature conversion reactor and the low temperature conversion reactor are in contact with each other.

The heat transfer part may be provided such that one end of the heat transfer part exchanges heat with the low temperature conversion reactor.

The high temperature conversion reactor may be configured to be surrounded by a cooling unit for cooling the high temperature conversion reactor.

The heat transfer unit may include one reforming reactor and the reforming reactor.

The exhaust passage includes a first passage formed inside the reforming reactor; And a second flow path formed on the outer side of the heat transfer part.

The plurality of heat transfer parts may be disposed at regular intervals along the outer circumferential surface of the reforming reactor and the reforming reactor.

The exhaust passage includes a first passage formed inside the reforming reactor; And a second flow path formed between the heat transfer parts.

Further, a heat transfer material may be further provided between the heat transfer part and a reactor in contact with the heat transfer part.

In order to achieve the object of the present invention, there is provided a burner for generating convection heat; A first catalyst layer surrounding the burner and converting natural gas into hydrogen; A second catalyst layer arranged in the longitudinal direction with respect to the first catalyst layer and converting carbon monoxide generated in the process of converting into fuel hydrogen into carbon dioxide; An exhaust passage for transferring the convection heat generated in the burner to the first catalyst layer; And a heat transfer member contacting the heat absorbing portion with the first catalyst layer and contacting the heating portion with the second catalyst layer to transfer part of the heat transferred to the first catalyst layer to the second catalyst layer by conduction. A fuel reforming device may be provided.

Here, the second catalyst layer may have a plurality of catalyst layers having different catalysts arranged in the longitudinal direction, and the heating portion of the heat transfer member may be in contact with the catalyst layer located away from the first catalyst layer among the second catalyst layers.

The catalyst layer in the second catalyst layer, which is not in contact with the heat transfer member, may be positioned within the range of the exhaust passage to receive heat by convection of the combustion gas generated in the burner.

The second catalyst layer may comprise a single catalyst layer, and the second catalyst layer may be located outside the range of the exhaust flow path.

In order to accomplish the object of the present invention, there is provided a reforming reactor for reforming a hydrocarbon-based fuel in a gaseous state; A conversion reactor for converting the carbon monoxide generated with hydrogen into carbon dioxide while passing through the reforming reactor to lower the content of carbon monoxide; And a heat pipe which is provided throughout the reforming reactor and the reforming reactor and absorbs heat in the reforming reactor and transfers the heat to the reforming reactor.

Here, the heat pipe may be formed by a capillary method, and one end thereof may be in contact with the outer circumferential surface of the reforming reactor while the other end thereof may be in contact with the outer circumferential surface of the conversion reactor.

In the fuel reforming apparatus according to the present invention, the reforming reactor is heated by a combustion gas using a burner, while the reforming reactor having a temperature gradient different from that of the reforming reactor is configured to receive heat from the reforming reactor using a heat transfer member such as a heat pipe The operating temperature of the reforming reactor and the conversion reactor can be easily and precisely controlled to improve the reforming performance.

In addition, the burner can be designed considering only the reforming reactor, thereby simplifying the design of the burner.

1 is a longitudinal sectional view showing an embodiment of a fuel reforming apparatus according to the present invention,
FIG. 2 is a longitudinal sectional view showing a heat transfer part installed in a reforming reactor in a reforming reactor according to FIG. 1,
Figs. 3 and 4 are cross-sectional views taken along line IV-IV shown in Fig. 1 for explaining aspects of the heat transfer portion,
FIG. 5 is an enlarged view showing a state in which a heat transfer material is interposed between the reforming reactor and the heat transfer portion in the fuel reforming apparatus of FIG.
6 is a longitudinal sectional view showing an example in which the conversion reactor is a single catalyst layer in the fuel reforming apparatus according to the present invention.

Hereinafter, the fuel reforming apparatus according to the present invention will be described in detail on the basis of an example shown in the accompanying drawings.

FIG. 1 is a longitudinal sectional view showing an embodiment of a fuel reforming apparatus according to the present invention, FIG. 2 is a longitudinal sectional view showing a heat transfer portion installed in a reforming reactor in a reforming reactor according to FIG. 1, FIG. 4 is a cross-sectional view taken along line IV-IV of FIG. 1 for explaining the shapes of the heat transfer portion, FIG. 5 is an enlarged view showing a state where a heat transfer material is interposed between the reforming reactor and the heat transfer portion in the fuel reforming apparatus of FIG. .

As shown in the figure, the present embodiment shows an example in which a reforming reactor and a high / low temperature conversion reactor for converting a reactant into a hydrogen and converting it into hydrogen are connected in series along the longitudinal direction. However, although not shown in the drawing, a chamber space may be formed in the upper part of the fuel reforming apparatus to circulate the reactants to recover and preheat the heat discharged to the outside.

In the drawings, the reactant circulation line is wound around the outer circumferential surface of the high temperature conversion reactor. The reactant circulation line is for cooling the high temperature conversion reactor by preheating the reactants by heat exchange with the combustion gas as described below. In some cases, however, the reactant circulation line may not be installed or may be installed on the inner circumferential surface of the high temperature conversion reactor have. Thus, the appearance of the heat transfer part (i.e., heat pipe) according to the present embodiment can be formed more concisely without stepping.

In the drawings, the selective oxidation reactor is shown enlarged. This selective oxidation reactor is for removing carbon monoxide contained in the reactant and is arranged in series in the longitudinal direction at a lower portion of the fuel reformer. However, since the present invention is directed to a fuel reforming apparatus, a detailed description of the selective oxidation reactor will be omitted.

Referring to FIG. 1, the fuel reforming apparatus according to the present embodiment includes a sealed casing 10 having a heat insulating wall on its inner wall surface and a long length in the longitudinal direction. Inside the casing 10, A combustion chamber 110 is formed along the longitudinal direction of the combustion chamber 110 and a burner 111 for generating gas by burning gas may be provided in the combustion chamber 110. A combustion gas inlet 11 may be provided at the lower end of the casing 10 to inject gas to be burned by the burner 111 into the combustion chamber 110. A reaction material inlet 13 for injecting a reactant into the reforming reactor 131 is formed at an upper end of the casing 10 and a plurality of reactors 131, And a reactant outlet 14 through which the reactant is discharged.

The burner 111 may be installed above the combustion chamber 110. That is, in the present invention, the reforming reactor 131 of the reforming reactor 131 and the reforming reactor 132, which will be described later, heats the exhaust gas using heat of the exhaust gas generated from the burner 111, Heat is received from the heat exchanger 131 and heated. Therefore, only the reforming reactor 131 in which the exhaust gas generated by the burner 111 is located is located at a relatively high position in the reforming reactor 131 that is located below the reforming reactor 131 The position of the burner 111 may be higher than the lower end of the reforming reactor 131 or at least equal to or higher than the upper end of the switching reactor 132 so that heat can be transferred only to the high- . However, when the wall of the combustion chamber 110 accommodating the burner 111 is made of a heat insulating wall, the burner 111 may be installed in the longitudinal range H1 of the switching reactor 132. [

The burner 111 may be a conventional Bunsen burner for burning natural gas for combustion to obtain a high temperature, or a metal fiber for combustion natural gas and atmospheric air as fuel. Here, the metal fiber has a shorter flame than the Bunsen burner and can generate a high heat quantity, so that it is efficient, the load is easy to control, and the flame range is wide.

The combustion chamber 110 is located at the center of the casing 10 and an exhaust flow path 120 to be described later is formed outside the combustion chamber 110. Outside the exhaust flow path 120, The reactors 132 may be arranged in series in the longitudinal direction along the longitudinal direction of the casing 1. [

It is preferable that the combustion chamber 110 is installed on the upper side of the casing 10 in consideration of the position of the burner 111. Accordingly, the exhaust gas generated in the combustion chamber 110 can be supplied to the reforming reactor 131 while moving from the top to the bottom of the casing 10.

An exhaust inlet 120a is formed at an upper end of the exhaust passage 120 to communicate with an upper end of the combustion chamber 110 to allow exhaust gas generated in the combustion chamber 110 to flow into the exhaust passage 120, An exhaust outlet 120b for exhausting the exhaust gas to the outside may be formed at an intermediate position (or a position lower than the exhaust inlet). The exhaust passage 120 may be formed in the longitudinal direction along the outer wall surface of the combustion chamber 120 from the middle height of the combustion chamber 110, that is, from the upper end of the reforming reactor 131 to the lower end thereof.

The exhaust passage 120 may be formed as a single passage including the outer wall surface of the combustion chamber 110. The exhaust passage 120 may include a first passage 121 as an inner passage and a second passage 122 as an outer passage, .

The exhaust inlet 120a and the exhaust outlet 120b are formed in parallel to each other so that the exhaust gas flows through both of the exhaust passages 121 and 122 through the exhaust inlet 120a, And then discharged together through the exhaust outlet 120b.

However, in some cases, the exhaust gas is formed in a serial form in which the plurality of exhaust passages 121 and 122 are successively communicated, and exhaust gas is introduced into one of the inner passage 121 and the outer passage 122 You may want to go first and then to another channel.

Here, the exhaust gas passage 120 may be formed so as to transfer the heat of the exhaust gas from the upper end to the lower end of the casing 10, that is, the entire reforming reactor 131 and the conversion reactor 132, which will be described later. However, when the heat pipe 150 to be described later is installed across the reforming reactor 131 and the switching reactor 132 as in the present embodiment, the heat transfer end 120c, which limits the range of the exhaust flow path 120, The first flow path 121 of the exhaust flow path 120 may be formed so as to exist only up to the range H2 of the reforming reactor 131. [ Thus, the exhaust gas outlet 12 may be located at a middle height of the casing, that is, at a height between the lower end of the reforming reactor 131 and the upper end of the switching reactor 132. Accordingly, the reforming reactor 131 receives the heat of the exhaust gas by convection while the exhaust gas generated in the combustion chamber 110 moves along the exhaust flow path 120. However, since the conversion reactor 132 is located outside the range of the exhaust passage 120, the conversion reactor 132 is not in direct contact with the exhaust gas flowing through the exhaust passage 120, and the heat of the exhaust gas is not received by the convection.

Alternatively, the conversion reactor 132 may receive heat by conduction differently from the reforming reactor 131. For example, as shown in FIGS. 1 and 2, both ends of the reforming reactor 131 and the reforming reactor 132 are connected to the two reactors 131 and 132 to form a heat pipe (a heat pipe) 150 may be installed. Accordingly, the conversion reactor 132 can receive heat from the reforming reactor 131 through the heat pipe 150. [

The heat pipe 150 may be of various types such as a capillary type, a gravity type, a rotary type, an electromagnetic type, and the like. Hereinafter, a case in which a capillary type heat pipe using a wick is applied will be described.

2, the heat pipe 150 has a gas passage 152 formed at the center of the inside of the housing 151, a liquid passage 153 formed outside the gas passage 152, a gas passage 152, And a wick (154) may be provided between the liquid passage (153) and the liquid passage (153).

The heat absorbing portion 151a of the heat pipe 150 contacts the outer circumferential surface of the reforming reactor 131 (precisely the wall surrounding the reforming reactor) to absorb heat from the reforming reactor 131, The working fluid in the steam state passes through the wick 154 and moves to the gas passage 152. When the working fluid in this steam state is increased, the heat of the heat pipe 150 And the portion 151b moves to the contacted conversion reactor 132.

Then, the working fluid in the vapor state exchanges heat with the conversion reactor 132 to lose heat, and is then converted into a liquid state and moves toward the reforming reactor 131 through the wick capillary force, (132). ≪ / RTI >

This allows the temperature of the conversion reactor 132 to be controlled by the heat of conduction so that the temperature of the conversion reactor 132 can be easily controlled and the burner 111 can be designed in consideration of the temperature of the reforming reactor 131 So that the burner 111 can be easily designed.

The heat pipe 150 may be formed in various shapes. For example, as shown in FIG. 3, the heat pipe 150 may be formed into a circular cylinder or a circular arc shape so as to surround the reforming reactor 131 and the switching reactor 132, May be formed in a plurality of arc shapes so as to surround the switching reactor (131) and the switching reactor (132) at regular intervals along the circumferential direction.

In the case of the former, the heat transfer area can be doubled by enlarging the heat transfer area compared to the latter. However, if the second flow path 122 is provided on the outer wall surface of the heat pipe 150, the inner diameter D1 of the casing 10 may be large have.

In contrast, in the latter case, the heat transfer area can be reduced compared to the former case, but the second flow path 122 can be formed between the heat pipes 150, so that the outer wall surface of the heat pipe 150 So that the inner diameter D2 of the casing 10 can be reduced correspondingly.

However, it is preferable that each heat pipe 150 has a relatively larger inner peripheral surface area than the outer peripheral surface, so that the heat transfer area with respect to each of the reactors 131 and 132 can be widened. To this end, the heat pipe 150 may be formed in a trapezoidal shape so that the side surface extends in the direction of the inner peripheral surface.

As shown in FIG. 5, a heat transfer pad (heat transfer pipe) 151 is disposed between the heat absorbing portion 151a of the heat pipe 150 and the reforming reactor 131, or between the heating portion 151b of the heat pipe 150 and the switching reactor 132 155 may be preferable in terms of heat exchange between the heat pipe 150 and the reactors 131, 132.

It is preferable that the wall surrounding the catalytic layer constituting the reforming reactor 131 and the reforming reactor 132 is formed of a heat-transferable material as well as the heat pipe 150 in view of heat transfer with the heat pipe 150.

On the other hand, the conversion reactor 132 may be formed as a double heat reactor by arranging a plurality of catalyst layers in a vertical direction in a double direction.

For example, when the conversion reactor 132 is formed as a reheat reactor, the heating unit 151b, which is the second end of the heat pipe 150, is connected to only one of the reheat reactors, It may be desirable to maintain the gradient.

1 and 2, when the conversion reactor 132 is composed of the high temperature conversion reactor 135 and the low temperature conversion reactor 136, the second stage 151b of the heat pipe 150 is operated at a low temperature May be contacted with the conversion reactor 136.

For example, the conversion reactor 132 may be a high-temperature conversion reactor 135 made of a copper-zinc (Cu-Zn) catalyst and having an operating temperature of about 300-400 ° C, an iron- And a low-temperature conversion reactor 136 having an operating temperature of approximately 235 to 300 ° C.

The upper end of the high temperature conversion reactor 135 is connected to the lower end of the reforming reactor 131 and the upper end of the low temperature conversion reactor 136 is connected to the lower end of the high temperature conversion reactor 135. The heat absorbing portion 151a constituting the first end of the heat pipe 150 is in contact with the outer circumferential surface of the reforming reactor 131 while the heating portion 151b constituting the second end is in contact with the outer circumferential surface of the reforming reactor 131, And may be in contact with the outer circumferential surface.

In this case, the exhaust passage 120 is extended from the upper end of the reforming reactor 131 to the lower end of the high-temperature conversion reactor 135 such that the high-temperature conversion reactor 135 can be heated by the heat of the exhaust gas generated in the combustion chamber 110 .

However, since the high temperature conversion reactor 135 has a lower operating temperature than the reforming reactor 131 having an operating temperature of 700 to 800 ° C, a separate cooling unit 160 may be provided to maintain an appropriate operating temperature. have.

For example, the cooling unit 160 may cool the high temperature conversion reactor 135 using natural gas to be used as a reactant, and may preheat the reactant natural gas to a predetermined temperature.

To this end, the reaction product circulation line 161 is installed to surround the outer circumferential surface of the high temperature conversion reaction vessel 132, and one end of the reaction product circulation line 161 is connected to the reaction product inlet 13 through a reaction product injection pipe .

The other end of the reactant circulation line 161 may be connected to a reactant injection flow path 162 formed between the outer circumferential surface of the inner exhaust flow path 120 and the inner circumferential surface of each reactor.

The reactant flowing into the reactant circulation line 161 is heat-exchanged with the exhaust gas passing through the external exhaust flow path 122 while being moved along the reactant circulation line 161, and is heat-exchanged with the high temperature conversion reactor 135 The high temperature conversion reactor 135 is cooled to an appropriate temperature. The reactant may also be preheated to a predetermined temperature by exchanging heat with the inner exhaust passage 162 while passing through the reactant injection passage 162.

On the other hand, the concentration of carbon monoxide is controlled to about 1% through the high temperature conversion reactor 135 and the low temperature conversion reactor 136, but the reformed gas, in which carbon monoxide is removed to less than 10 ppm, should be injected into the fuel cell stack.

Therefore, the selective oxidation reactor 133 may be further provided at the lower end of the low temperature conversion reactor 136. The selective oxidation reactor 133 is installed to reduce the content of carbon monoxide contained in the reactant to about 10 ppm or less contained in the reactant so that the reactant is suitable for the fuel cell stack. The selective oxidation reactor 133 is connected to the lower portion of the fuel reformer And may be arranged in series along the longitudinal direction.

The selective oxidation reactor 133 can utilize atmospheric air for the required oxygen. To this end, an air inlet 15 may be provided in the middle of the lower half of the casing 10, that is, between the lower end of the low temperature conversion reactor and the upper end of the selective oxidation reactor, to suck air into the selective oxidation reactor. And a cooling inlet 16 and a cooling outlet 17 for cooling the selective oxidation reactor 133 may be respectively provided below the inlet. As a result, the reformed gas passed through the low temperature conversion reactor 136 is combined with oxygen, and then reacted with the selective oxidation reactor 133 to remove carbon monoxide to less than 10 ppm.

Meanwhile, in the above-described embodiments, the switching reactor has been described as a multi-layer structure having a plurality of catalyst layers. However, in some cases, the switching reactor may be formed as a single reactor having a single catalyst layer.

For example, when the conversion reactor 132 is formed as a single reactor as shown in FIG. 6, when the heating unit 151b, which is the second end of the heat pipe 150, contacts the conversion reactor 132, And transfer it to the conversion reactor (132).

In this case, since the exhaust outlet 12 is formed at a height between the reforming reactor 131 and the switching reactor 132, the reforming reactor 131 receives heat of the exhaust gas by convection and the conversion reactor 132 Heat is transferred from the reforming reactor 131 by conduction using the heat transfer part such as the heat pipe 150 described above.

The basic configuration and operation effects of the present invention are similar to those of the above-described embodiments, and therefore, a detailed description thereof will be omitted.

Claims (14)

A combustion chamber in which a burner is installed;
An exhaust passage through which the exhaust gas generated in the combustion chamber circulates;
A reforming reactor surrounded by the exhaust passage and absorbing heat from the exhaust gas flowing through the exhaust passage to convert natural gas into hydrogen;
A reforming reactor disposed below the reforming reactor for converting carbon monoxide generated with hydrogen into carbon dioxide and dissipating heat; And
And a heat transfer unit surrounding the reforming reactor and the reforming reactor and having a working fluid for transferring heat through phase change therein to absorb heat in the reforming reactor by the working fluid and transfer the heat to the reforming reactor Characterized in that the fuel reforming device. The method according to claim 1,
Wherein an inlet of the exhaust passage is communicated at an upper end of the combustion chamber and an outlet of the exhaust passage is formed at a position higher than a lower end of the switching reactor. 3. The method of claim 2,
Wherein the conversion reactor comprises a single catalyst bed,
And the outlet of the exhaust channel is formed at a height where the reforming reactor and the conversion reactor are in contact with each other. 3. The method of claim 2,
Wherein the conversion reactor comprises a high temperature conversion reactor having different catalyst layers and a low temperature conversion reactor, the high temperature conversion reactor is connected to the reforming reactor, the high temperature conversion reactor and the low temperature conversion reactor are arranged in the longitudinal direction,
Wherein the outlet of the exhaust passage is formed at a position where the high temperature conversion reactor and the low temperature conversion reactor are in contact with each other. 5. The method of claim 4,
Wherein the heat transfer part is provided so that one end of the heat transfer part exchanges heat with the low temperature conversion reactor. 5. The method of claim 4,
Wherein the high temperature conversion reactor is surrounded by a cooling section for cooling the high temperature conversion reactor. 7. The method according to any one of claims 1 to 6,
Wherein the heat transfer unit comprises a single reforming reactor and a reforming reactor. The method according to claim 1,
The exhaust passage
A first flow path formed inside the reforming reactor; And
And a second flow path formed outside the heat transfer portion. 7. The method according to any one of claims 1 to 6,
Wherein the plurality of heat transfer parts are disposed at regular intervals along the outer circumferential surface of the reforming reactor and the reforming reactor. 10. The method of claim 9,
The exhaust passage
A first flow path formed inside the reforming reactor; And
And a second flow path formed between the heat transfer parts. The method according to claim 1,
Wherein a heat transfer material is further provided between the heat transfer part and a reactor in contact with the heat transfer part. A burner for generating convection heat;
A first catalyst layer surrounding the burner and converting natural gas into hydrogen;
A second catalyst layer arranged in the longitudinal direction with respect to the first catalyst layer and converting carbon monoxide generated in the process of converting into fuel hydrogen into carbon dioxide;
An exhaust passage for transferring the convection heat generated in the burner to the first catalyst layer; And
And a heat transfer member contacting the heat absorbing portion with the first catalyst layer and contacting the heating portion with the second catalyst layer to transfer part of the heat transferred to the first catalyst layer to the second catalyst layer by conduction. Reforming device. A reforming reactor for reforming a fuel in a gaseous state which is hydrocarbon-based;
A conversion reactor for converting the carbon monoxide generated with hydrogen into carbon dioxide while passing through the reforming reactor to lower the content of carbon monoxide; And
And a heat pipe provided over the reforming reactor and the reforming reactor to absorb heat from the reforming reactor and transfer the heat to the reforming reactor. 14. The method of claim 13,
Wherein the heat pipe is formed in a capillary manner so that one end thereof is in contact with the outer circumferential surface of the reforming reactor and the other end is in contact with the outer circumferential surface of the reforming reactor.

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