KR100761945B1 - Gas fuel processor - Google Patents

Abstract

A gas fuel treating system for converting natural gas or LPG into a hydrogen-containing reforming gas is provided to facilitate heat exchange and reactant distribution in each unit reactor module while allowing downsizing of the system and highly efficient operation of the system. A gas fuel treating system for converting natural gas or LPG into a hydrogen-containing reforming gas comprises: a water steam reforming reactor containing a water steam reforming catalyst(4) filled between a cylindrical combustion chamber(2) having a burner(1) and a cylindrical body(3) having a larger diameter than the combustion chamber; a transition reactor(40,41,42) capable of being coupled to the water steam reforming reactor in such a manner that the water steam reforming reactor is received inside the transition reactor, and comprising a catalyst filled in a flow path(15) corresponding to the space between the transition reactor and the outer wall of the water steam reforming reactor; and a selective reactor having a catalyst layer for reducing the content of CO in the reforming gas supplied from the transition reactor, a diffusion member(24) for contacting the reforming gas uniformly with the catalyst layer, and a cooling section for inhibiting an increase in the temperature of the catalyst layer, wherein the water steam reforming reactor, transition reactor and selective reactor are integrally coupled with one another to accomplish heat exchange.

Description

Gas fuel processor

1 is a cross-sectional view of a gas fuel processor according to a first embodiment of the present invention, wherein the gas fuel processor is integrated with a steam reformer, a water gas transfer reactor, and a selective oxidation reactor.

2A is a perspective view illustrating a donut type selective oxidation reactor capable of being separated from and installed with a main body of a gaseous fuel processor according to Embodiment 1 of the present invention.

FIG. 2B is a plan sectional view of FIG. 2A.

3 is a cross-sectional view showing a cylindrical selective oxidation reactor capable of being separated from and installed with the main body of the gas fuel processor according to the second embodiment of the present invention.

<Description of the symbols for the main parts of the drawings>

1: burner 2: cylindrical combustion chamber

3: cylindrical body 4: reforming catalyst

5: burner guide 6: heat transfer fin

7: Outlet 8: Raw gas inlet

9: source gas buffer 10: source gas preheating unit

11: outer wall of combustion chamber 12: steam reformer outlet

13: first preheater 14: second preheater

15: Euro 16: Casing Flange

17: cylindrical flange 18: gap

19: high temperature transition reaction unit 20: low temperature transition reaction unit

21: Mixing Tube 22: Static Mixer

23: mixing tube output port 24: diffusion part

25: reformed gas outlet 26: heat exchange unit

27: catalyst layer 30: communication hole

31: exhaust gas buffer 32: first inlet hole

33: first inflow hole 34: second inflow hole

35: second outlet hole 36: cooling medium supply pipe

37: cooling medium discharge pipe 39: source gas supply hole

40: casing 41: high temperature transition reaction inlet

42: low temperature transition reactor inlet 220: oxidation reactor casing

221: mixing tube 222: static mixer

225: reformed gas outlet 227: catalyst bed

228: cooling tube 229: cooling jacket

231: coolant supply port 232: coolant discharge port

233: cooling jacket hole

The present invention relates to a cylindrical fuel processor for converting fuel such as natural gas, LPG or general household city gas into hydrogen-rich reformed gas through a fuel treatment process, and more particularly, smoothly supplying reformed gas to a polymer fuel cell. It relates to a gas fuel processor for.

In general, a natural gas fuel treatment system for supplying hydrogen to small-sized distributed polymer fuel cell (PEMFCs) systems for home use consists of a unit process such as desulfurization, steam reforming, high temperature transition, low temperature transition, and selective oxidation.

In the existing large-scale hydrogen manufacturing process, each unit process is operated independently and is not limited in size, but for the home fuel cell system for general home installation, the direction of induction of small size and high efficiency through modularization and integration of each unit process Is being studied.

For example, in the case of the 'cylinder steam reformer' of Korean Patent Publication No. 10-2004-0012890, a plurality of cylindrical tubes are installed, a burner in the center, and a steam reforming catalyst layer, a transition reaction catalyst layer, and a selective oxidation catalyst layer in the gap of each tube. To install the unit reactor.

However, such a reformer is provided with a heat insulation layer between the transition reaction catalyst layer and the outer wall, and the structure of the selective oxidation reactor introduction part is complicated, making it difficult to manufacture and repair work in the event of abnormal catalyst layer.

In addition, in Japanese Patent Application Laid-Open No. 2004-262691, although a cylindrical steam reforming reactor was installed and a transition reactor and an optional oxidation reactor were installed on the outer wall, the structure for cooling and preheating the raw material of the transition and selective oxidation reactor was complicated, Repair for the damage of the transfer reaction catalyst by heat transfer is not easy.

In most cases, the reactor was designed to integrate the unit reaction including the fuel processor. However, a complicated structure is not avoided for the mixing of the reformed gas and air at the inlet of the selective oxidation reactor, which makes the reactor difficult to manufacture. In the event of an abnormality in the catalyst layer, it is difficult to repair and maintain the system, and the improvement of the overall system is inferior.

An object of the present invention devised to solve the above problems is to modularize each unit reaction to facilitate separation and integration, and to induce integration of unit reactions so that each unit reactors can easily perform mutual heat exchange and reactant distribution. In addition, the present invention provides a gas fuel processor that can be operated with high thermal efficiency while being compact, lightweight, and easy to manufacture and maintain.

In order to achieve the above object, the present invention provides a gas fuel processor for converting natural gas or LPG into a reforming gas containing hydrogen, comprising a cylindrical combustion chamber having a burner installed therein, and a cylindrical body having a diameter larger than that of the combustion chamber. A steam reforming reactor filled with a steam reforming catalyst therebetween; A transition reactor capable of fastening with the water vapor reforming reactor in a state in which the steam reforming reactor is accommodated therein, and filling a catalyst for transition reaction in a flow path between the outer wall of the steam reforming reactor; And a selective reactor having a catalyst layer to reduce the content of carbon monoxide in the reformed gas supplied from the transition reactor, a diffusion unit for uniformly contacting the reformed gas to the catalyst layer, and a cooling unit for suppressing the temperature rise of the catalyst layer. And, the steam reforming reactor, the transition reactor, the selective reactor is a gas fuel processor, characterized in that the heat exchange with each other integrally combined.

The reforming reactor and the transition reactor are characterized in that the flange for coupling and separation is formed.

In addition, the heat transfer fins may be provided on the outer wall of the combustion chamber by limiting the stacked height of the reforming catalyst.

In addition, the source gas supplied to the steam reforming reactor through the source gas inlet is mixed in the space between the combustion chamber and the cylinder after being mixed by the collision with the wall of the source gas buffer formed around the upper portion of the cylindrical body It is characterized in that the feed to the raw material gas preheating unit.

In addition, a steam reformer outlet is formed at the bottom of the cylindrical body, and the reformed gas is discharged through the steam reformer outlet to move upward through the flow path.

In addition, by placing a predetermined space between the outer wall of the steam reforming reactor and the inner wall of the transition reactor, the reforming reactor can be easily inserted and separated, and the reforming reactor frees thermal expansion in a predetermined space during normal operation.

In addition, the catalyst of the transition reactor is characterized in that it comprises a platinum-based transition catalyst, iron-chromium catalyst.

In addition, the transition reactor and the selective reactor is characterized in that the static mixer is connected to the built-in mixing tube.

In addition, the catalyst layer of the selective reactor is characterized in that the Pt-based catalyst or Ru-based catalyst is filled, or the Pt-based catalyst is filled in the first half and Ru-based catalyst is filled in the second half.

In addition, the selective reactor has a diffusion layer connected to the mixing tube and the catalyst layer formed in the shape of a tube, the diffusion portion is characterized in that it is formed in a fan shape in order to make contact between the catalyst layer and the reformed gas uniform.

In addition, the selective reactor has a catalyst layer formed surrounding the mixing tube, the oxidation reactor casing is installed to the outside of the catalyst layer, the reformed gas passes through the mixing tube to hit the oxidation reactor casing the catalyst layer It is discharged through the, characterized in that the inlet and the outer wall surface of the catalyst layer is provided with a cooling tube or a cooling jacket for controlling the temperature of the catalyst layer.

Hereinafter, with reference to the accompanying drawings, preferred embodiments of the present invention will be described. In adding reference numerals to components of the following drawings, it is determined that the same components have the same reference numerals as much as possible even if displayed on different drawings, and it is determined that they may unnecessarily obscure the subject matter of the present invention. Detailed descriptions of well-known functions and configurations will be omitted.

The present invention provides a selective steam reactor connected by a cylindrical steam reformer, a transition reactor capable of inserting the cylindrical steam reformer and fastening through a flange, and a tube having a mixing means of reforming gas and air to solve the above problems. It is a gas fuel processor comprising.

1 is a cross-sectional view of a gas fuel processor according to a first embodiment of the present invention.

The steam reformer of the present invention comprises a cylindrical combustion chamber 2 having a space in which the burner 1 can be installed, and a cylindrical body 3 having a diameter larger than the diameter of the combustion chamber 2.

The space formed between the combustion chamber 2 and the cylindrical body 3 is a source gas preheating unit 10, and the reforming catalyst 4 is filled in the source gas preheating unit 10.

The burner guide 5 is installed inside the combustion chamber 2 at a predetermined distance from the outer wall of the combustion chamber 2 to prevent the flame of the burner 1 from directly closing on the surface.

As shown in FIG. 1, the burner 1 has approximately half the length of the combustion chamber 2, and the burner guide 5 is longer than the burner 1 and approximately to the end of the combustion chamber 2. Is extended.

The length of the burner 1, the combustion chamber 2, and the burner guide 5 is determined in consideration of the length of the flame discharged from the burner 1.

A communication hole 30 is formed at an upper end of the combustion chamber 2, and an annular exhaust gas buffer 31 is installed around the communication hole 30.

In addition, an outlet 7 is formed at an upper end of the exhaust gas buffer 31.

Therefore, the combustion flue gas generated by the burner 1 passes through the space between the burner guide 5 and the combustion chamber 2 and is collected in the flue gas buffer 31 through the communication hole 30. The discharge port 7 is discharged.

At this time, the heat of the exhaust gas buffer 31 heats the water flowing through the first preheating unit 13 formed to surround the exhaust gas buffer 31.

The first preheating part 13 is formed with a first inflow hole 32 and a first outflow hole 33 to allow water to enter and exit.

In addition, a heat transfer fin 6 is installed on the outer wall of the combustion chamber to increase the heat transfer area.

The heat transfer fins 6 are installed at the same position as the steam reforming catalyst layer 4 or up to the height of the catalyst layer 4.

The length of the heat transfer fins 6 is limited to be equal to or smaller than the stacked length of the reforming catalyst 4 to be described below, which, when longer, may adversely affect the filling of the catalyst and the mixing of the reactants. Because

At the upper end of the combustion chamber 2, a raw material gas buffer 9 is installed below the exhaust gas buffer 31.

A raw material gas inlet 8 for injecting raw material gas is installed at one end of the raw material gas buffer 9.

The source gas buffer 9 forms a space having a cross-sectional area larger than the cross-sectional area of the source gas inlet 8 so that the source gas can be uniformly supplied around the combustion chamber 2, and around the outer wall of the combustion chamber 2. The raw material gas supply hole 39 is formed.

The raw material gas flows between the combustion chamber 2 and the cylindrical body 3 formed around the outer wall of the combustion chamber 2 to pass through the reforming catalyst 4 and the heat transfer fin 6.

A combustion chamber outer wall 11 is formed at the lower end of the combustion chamber 2, and the cylindrical body 3 extends further downward than the combustion chamber 2, and a steam reformer outlet 12 is formed at the end of the cylindrical body. ) Is formed.

A casing 40 of a transition reactor is formed to surround the cylindrical body 3 and form a flow path 15 in communication with the steam reformer outlet 12.

The cylindrical body 3 and the casing 40 are fastened by a cylindrical flange 17 formed at the upper end of the cylindrical body 3 and a casing flange 16 formed at the upper end of the casing 40.

A second preheating portion 14 is formed outside the central portion of the casing 40 so that the reformed gas passing through the flow passage 15 and the water flowing in the second preheating portion 14 achieve heat transfer.

The second preheating part 14 is provided with a second inflow hole 34 and a second outflow hole 35 to allow water to enter and exit.

The high temperature transition reaction part 19 and the low temperature transition reaction part 20 are sequentially stacked from the substantially middle portion of the flow path 15.

A predetermined gap 18 is formed between the outer wall of the cylindrical body 3 and the high temperature transfer reaction unit 19 and the low temperature transfer reaction unit 20 to prevent deformation due to thermal expansion.

The high temperature transition reaction unit 19 and the low temperature transition reaction unit 20 are installed in an annular housing to maintain its shape, and each has a high temperature transition reaction unit inlet 41 and a low temperature transition reaction unit inlet 42. Communication with the flow path 15 is made.

The reformed gas, which is a result of the reaction, is temporarily collected at an upper side of the low temperature transition reaction part 42, and passes through the mixing tube 21 through a mixing tube input port 43 formed at one side of the space. Is supplied to the diffusion portion 24 through the mixing tube output port (23).

In Example 1, as the selective oxidation reactor, a tubular selective oxidation reactor is used as shown in FIG.

The diffusion part 24 is adjacent to the catalyst layer 27 and serves to diffuse the reformed gas so as not to be biased in a predetermined portion.

The catalyst layer 27 is formed around the buffer 9.

A reformed gas outlet 25 for discharging hydrogen is provided on the opposite side of the diffusion portion 24.

FIG. 2 is a perspective view and a plan cross-sectional view showing clearly the relationship between the catalyst layer 27 and the diffusion part 24 of Example 1. FIG.

The diffusion part 24 is formed in a substantially fan-shaped shape, so that the reformed gas in the diffusion part 24 can be contacted over a wide range of the catalyst layer 27.

3 shows a cylindrical selective oxidation reactor of Example 2. FIG. The cylindrical selective oxidation reactor of Example 2 may be used in place of the tubular selective oxidation reactor of Example 1.

A mixing tube 221 connected to the transition reactor is installed to penetrate through the oxidation reactor casing 220, and an end of the mixing tube 221 is formed to be close to the bottom surface of the oxidation reactor casing 220.

A catalyst layer 227 is wrapped around a portion of the mixing tube 221 to fill a space between the oxidation reactor casing 220 and the mixing tube 221.

A tubular cooling tube 228 is formed on the outer circumferential surface of the casing 220 in which the catalyst layer 227 is formed.

The cooling jacket 229 formed by bending the inside of the oxidation reactor casing 220 integrally with the coolant supply port 231 formed at the bottom of the oxidation reactor casing 220 and the tubular cooling tube 228 are connected. The cooling liquid passing through the cooling jacket 229 passes through the tubular cooling tube 228 and is discharged to the cooling liquid discharge port 232 formed above the tubular cooling tube 228.

At this time, the cooling jacket 229 protrudes to the outside through the cooling jacket hole 233 formed in the bottom portion of the oxidation reactor casing 220 is connected to the tubular cooling pipe 228.

Therefore, the reformed gas and air flow into the mixing tube 221 and flow from the top to the bottom while being mixed by the static mixer 222 installed in the mixing tube 221, and the mixed reformed gas and air flow into the oxidation reactor casing. While hitting the bottom surface of 220, the catalyst layer 227 passes through the reformed gas outlet 225.

Hereinafter, the reforming process according to the present invention will be described.

Fuel and combustion air flow into the burner 1, and combustion exhaust gas is discharged downward, and the combustion exhaust gas flows upward between the combustion chamber 2 and the burner guide 5, and the exhaust gas buffer 31 Discharge through the outlet (7) via).

At this time, the combustion exhaust gas preheats the raw material gas flowing around the combustion chamber 2, and supplies heat to the water in the first preheating unit 13 around the exhaust gas buffer 31.

Water vapor introduced through the raw material gas inlet 8 and the raw material, which is natural gas or LPG, collide with the raw material gas buffer 9 and are primarily mixed while changing the flow from the vertical direction to the horizontal direction, and again flowing in the vertical downward direction. The same is passed in the second pass through the gas preheating unit 10.

The mixture of steam and raw material gas preheated to about 500 ° C. by the combustion exhaust gas in the raw material gas preheating unit 10 is introduced into the reforming catalyst 4 so that hydrocarbons such as ethane, propane and isobutane are converted into methane. Then undergo the following steam reforming reaction.

CH ₄ + H ₂ O → CO + 3H ₂

The reforming catalyst 4 is configured to be in contact with both the combustion chamber outer wall surface 2 and the lower wall surface 11 so as to receive reaction heat through both the outer wall and the lower wall of the combustion chamber 2, and the combustion chamber 2 The reformed gas generated while descending along the outer wall is collected at one of the steam reformer outlets 12 below the cylindrical body 3.

The water supplied for the reaction is first preheated to 75 ° C. or higher in the first preheater 13, and then using the reaction heat in the second preheater 14 installed outside the hot water gas transition unit 19. It is converted into water vapor and supplied to the raw material gas inlet 8.

At this time, the first preheating unit 13 and the second preheating unit 14 are configured in the form of a jacket, in order to prevent boiling phenomenon that occurs instantaneously while water vapor stays in a predetermined space when steam is generated. It is also preferable.

The reformed gas discharged through the steam reformer outlet 12 moves to the transition reactor side while giving rise to the insulating catalyst 4 while insulating the reforming catalyst 4 while rising through the flow path 15.

The transition reactor may be fastened and separated through separation of the casing flange 17 and the cylindrical flange flange 16.

The transition reaction unit is divided into a high temperature transition reaction unit 19 and a low temperature transition reaction unit 20, the high temperature transition reaction unit 19 is 450 to 350 ° C., and the low temperature transition reaction unit 20 is 350 to 200 ° C. Allow to operate at temperature.

At this time, carbon monoxide is converted into hydrogen and carbon dioxide through the following water gas transition reaction.

CO + H ₂ O → CO ₂ + H ₂

The high temperature transfer reaction unit 19 fills the iron-chromium-based transfer catalyst layer and reduces the carbon monoxide concentration of 13 to 15% contained in the reformed gas to 5% or less, and the low temperature transfer reaction unit 20 has excellent heat resistance. It is filled with a platinum-serium series transition catalyst layer known to reduce the carbon monoxide concentration of about 5% to 1% or less.

At this time, it is possible to use a platinum-serium series in the high temperature transition reaction unit 19, but a rapid exotherm due to the methanation reaction of carbon monoxide in the 400 ℃ region is expected, and the high temperature transition to reduce the amount of expensive platinum-based catalyst It is preferable to use an iron-chromium catalyst for the reaction part.

In addition, although the low-temperature transition reaction unit 20 may use a low-cost copper-based catalyst, since the heat resistance is weak, there is a problem in durability and low reactivity, so that a large amount of catalyst is required. Preference is given to using a series catalyst.

In order for the reformed gas discharged from the low temperature transition reaction unit 20 to be supplied to the polymer fuel cell, the carbon monoxide concentration should be reduced to 10 ppm or less.

For this purpose, a method of converting carbon monoxide to carbon dioxide through the following selective oxidation reactor is widely used.

CO + 1 / 2O ₂ → CO ₂

In this case, air is supplied for oxygen to react with carbon monoxide, and an effective carbon monoxide oxidation reaction must be induced through uniform mixing of reforming gas and air.

To this end, in the above-described conventional technique, the method of adjusting the size of the reformed gas passage hole to obtain a predetermined passage speed (Korean Patent Publication No. 10-2004-0012890), or maintaining a proper temperature using a heat transfer particle filling layer ( Japanese Patent Laid-Open No. 2004-262691) is also used.

However, when applying these methods, the flow path structure connecting the transition reactor and the selective oxidation reactor becomes complicated, and maintenance and maintenance may be difficult.

In the present invention, as shown in Figures 2 and 3, between the outlet of the transition reactor and the selective oxidation reactor with a mixing tube (21, 221) and the vortex generating structure, more specifically the static mixer (22, 222) inserted therein reforming gas Induce mixing of air with air.

In the case of the static mixer, since the minimum length is required for uniform mixing of the reactants, a mixing tube capable of inserting the minimum length of the mixer according to the tube inner diameter was used.

Therefore, the water gas shift reactor and the selective oxidation reactor are separated by a certain distance, but the length does not affect the startup time, the differential pressure, the thermal efficiency, etc. of the entire system.

Moreover, when the selective oxidation reactor is tubular as shown in Fig. 2, it is placed on the flanges 16 and 17 joining the reforming reactor and the transition reactor, and is in contact with the top of the reforming reactor. It is possible to freely adjust the direction and length of the oxidation reactor inlet connection.

The reformed gas passing through the mixing tube was widely diffused in the fan-shaped diffusion portion 24 through the inlet 23 and introduced into the catalyst layer 27 to prevent concentration on any part of the catalyst layer.

The reformed gas passing through the catalyst bed in the horizontal direction is collected again and discharged through the outlet 25 in the vertical direction. This allows the reformed gas to pass uniformly throughout the catalyst bed.

In addition, since the selective oxidation reactor generates a rapid exothermic reaction due to the oxidation reaction at the inlet of the catalyst bed, a heat exchange part 26 capable of flowing air or water for cooling is provided, and a heat exchange part is provided to prevent an increase in temperature of the entire catalyst bed. .

The heat exchanger 26 may use a jacket or a cooling tube.

A cooling medium supply pipe 36 and a cooling medium discharge pipe 37 capable of supplying air or water to the heat exchange part 26 are formed.

The inlet temperature is maintained at 130 ° C. or lower through heat exchange in the heat exchanger 26, and the maximum temperature of the oxidation catalyst layer is maintained at 160 ° C. or lower to remove the carbon monoxide concentration to 10 ppm or less using a platinum-based or ruthenium-based catalyst. It is possible.

The type of the selective oxidation reactor is not limited to the donut type, but a cylindrical reactor having a tube into which a static mixer is inserted may be configured according to Example 2 as shown in FIG. 3.

In this case, the reformed gas and the air are uniformly mixed while passing through the static mixer 222 in the mixing tube 221 and introduced into the catalyst layer 227 while inverting and rising from the bottom of the reactor.

At this time, in order to prevent the rapid rise of the temperature of the inlet of the catalyst layer 227, a cooling pipe 228 capable of maintaining the temperature of the reformed gas at the inlet of the catalyst layer at 130 ° C or less is installed.

The water discharged from the cooling tube 228 is supplied to the cooling tube or jacket 29 to prevent the temperature of the catalyst layer from increasing again to maintain the maximum temperature of the catalyst layer at 160 ° C or less.

[Test Example]

Hereinafter, the features of the present invention through the test examples in more detail.

In the present embodiment, Example 1 is applied to a gas fuel processor having a hydrogen production scale of 1.0 Nm ³ / hr for a 1 kW class polymer fuel cell, but the present invention is not limited to this test example, and the hydrogen production is more than 3.0 Nm ³ / hr. Applicable in scale.

Steam reformers, transition reactors, and selective oxidation reactors were charged with each catalyst, and each reactor was connected through a flange and a mixing tube. City gas was used as the reforming feedstock gas, supplied at a flow rate of 4.3NL / min, and pure water was supplied at 11.8 g / min to operate at a water vapor / carbon ratio (S / C ratio) = 3.0.

Air for the selective oxidation reaction was supplied at 1.6 NL / min.

The flow rate of the natural gas supplied to the burner 1 is 2.14 NL / min, and the reformed gas outlet temperature is 730 ° C. or higher to convert most of the hydrocarbons such as methane, ethane, propane and butane into hydrogen and carbon monoxide in the raw natural gas. It was possible.

Table 1 shows the composition, methane conversion and thermal efficiency of the reformed gas discharged from the fuel treatment system at steady state.

 Reforming gas composition (Dry basis) H ₂ 73.0 wt% CO ₂ 19.5 wt% CH ₄ 2.0 wt% CO 10 ppm N ₂ 5.5 wt% Methane conversion 91% Thermal efficiency 78% (HHV)

As described above, it has been described with reference to the preferred embodiment of the present invention, but those skilled in the art various modifications and changes of the present invention without departing from the spirit and scope of the present invention described in the claims below I can understand that you can.

As described above, through the present invention, since the cylindrical steam reforming reactor and the cylindrical transition reactor capable of inserting the same can be fastened through the flange, the whole system can be miniaturized, and the partial catalyst can be replaced without replacing the entire reactor. Repair is now possible.

In addition, the transition reactor and the selective oxidation reactor were connected through a tube into which a static mixer was inserted, enabling uniform mixing of the reforming gas and the oxidizing air, thereby avoiding complicated connection structure.

It can provide miniaturization of the entire reactor, simplification of fabrication, ease of maintenance and maintenance, and increased thermal efficiency.

Claims (11)

In the gas fuel processor for converting natural gas or LPG into reformed gas containing hydrogen, A steam reforming reactor in which a steam reforming catalyst is filled between a cylindrical combustion chamber having a burner installed therein and a cylindrical body having a diameter larger than that of the combustion chamber; A transition reactor capable of fastening with the water vapor reforming reactor in a state in which the steam reforming reactor is accommodated therein, and filling a catalyst for transition reaction in a flow path between the outer wall of the steam reforming reactor; And A selective reactor having a catalyst layer to reduce the content of carbon monoxide in the reformed gas supplied from the transition reactor, a diffusion unit for uniformly contacting the reformed gas to the catalyst layer, and a cooling unit for suppressing a temperature rise of the catalyst layer; , The steam reforming reactor, the transition reactor, the selective reactor is integrally coupled to the gas fuel processor, characterized in that the mutual heat exchange. The gaseous fuel processor of claim 1, wherein the reforming reactor and the transition reactor have flanges for coupling and separating. The gas fuel processor according to claim 1, wherein heat transfer fins are provided on the outer wall surface of the combustion chamber in a manner of limiting the stacked height of the reforming catalyst. The method according to claim 1, wherein the source gas supplied to the steam reforming reactor through the source gas inlet is mixed by collision with the wall of the source gas buffer formed around the upper part of the cylinder, and then between the combustion chamber and the cylinder. Gas fuel processor, characterized in that the feed to the raw material gas preheating unit formed in the space. The gas fuel processor of claim 1, wherein a steam reformer outlet is formed at a bottom of the cylindrical body, and a reformed gas is discharged through the steam reformer outlet to move upward through a flow path. The method according to claim 1, wherein a space is provided between the outer wall of the steam reforming reactor and the inner wall of the transition reactor to facilitate insertion and separation of the reforming reactor, and the reforming reactor frees thermal expansion in a predetermined space during normal operation. Gas fuel processor characterized in that. The gaseous fuel processor of claim 1, wherein the catalyst of the transition reactor comprises a platinum-based transition catalyst and an iron-chromium catalyst. The gas fuel processor of claim 1, wherein the transition reactor and the selective reactor are connected to a mixing tube in which a static mixer is embedded. The gas fuel processor according to claim 1, wherein the catalyst layer of the selective reactor is filled with a Pt-based catalyst or a Ru-based catalyst, or a Pt-based catalyst is filled in the first half and the Ru-based catalyst is filled in the second half. The method of claim 8, wherein the selective reactor has a diffusion portion connected to the mixing tube and the catalyst layer formed in the shape of a tube, the diffusion portion is characterized in that it is formed in a fan shape to uniform contact between the catalyst layer and the reformed gas Gas fuel processor. The method of claim 8, wherein the selective reactor has a catalyst layer formed surrounding the mixing tube, the oxidation reactor casing is installed to the outside of the catalyst layer, the reforming gas passes through the mixing tube and the oxidation reactor casing And a cooling tube or a cooling jacket installed at the inlet and the outer wall of the catalyst layer to be discharged through the catalyst layer to impinge the surface of the catalyst layer.

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