JP2002356303A - Reducing method for carbon monoxide and reducing reactor for carbon monoxide - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a reducing method and a reducing reactor for carbon monoxide capable of surely reducing carbon monoxide contained in a processed gas. SOLUTION: In an inside of a number of honeycomb catalyst layers 25 and a number of cooling layers 26 which are alternately layered, a flow path 31 which a cross section increases gradually is formed from an inlet side 27 of a honeycomb catalyst layers to an outlet side 28 of the honeycomb catalyst layers. The honeycomb catalyst layers 25 are cooled by introducing a coolant into the flow path 31 from the inlet side 27 of the honeycomb catalyst layers. A temperature distribution of the honeycomb catalyst layers 25 from the inlet side 27 of the honeycomb catalyst layers to the outlet side 28 of the honeycomb catalyst layers is reduced.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for reducing carbon monoxide contained in a gas to be treated and a reactor for reducing carbon monoxide.

[0002]

2. Description of the Related Art Conventionally, as a power generator, for example,
Thermal power and nuclear power plants have been used to extract chemical energy generated by combustion as heat and convert it into electrical energy via mechanical energy.However, due to problems such as energy conversion efficiency, chemical energy generated by combustion has been used. The development of a fuel cell device that directly converts gas into electric energy is under way. Among such fuel cells, a solid polymer fuel cell is particularly useful because the electrolyte is not easily decomposed and can be operated at a low temperature.

In a polymer electrolyte fuel cell, it is known that the platinum catalyst carried on the anode electrode is poisoned by carbon monoxide contained in a reformed gas such as hydrogen, which causes a decrease in cell performance. ing.

In order to reduce carbon monoxide to less than about 100 ppm in the reformed gas, a solid polymer fuel cell system for operating a solid polymer fuel cell is provided with a carbon monoxide reduction reaction. Vessels are arranged.

[0005] Such a carbon monoxide reduction reactor has a catalyst layer carrying a catalyst. A gas to be treated containing a reformed gas and an oxidizing agent is introduced into the catalyst layer, and a reaction represented by the following formula (1) is performed. Is caused to reduce carbon monoxide.

Embedded image Here, the reaction of the above formula (1) is an exothermic reaction as can be seen from the following formula (2).

Embedded image Therefore, the temperature of the catalyst layer increases due to the oxidation reaction of carbon monoxide. When the temperature of the catalyst layer rises to some extent, hydrogen in the gas to be treated reacts with carbon dioxide, and the leftward reaction (reverse shift reaction) of the following equation (3) tends to occur.

Embedded image In order to effectively suppress the reverse shift reaction, see
Japanese Patent Application Publication No. 0-245573 discloses a technique in which cooling layers are alternately stacked with catalyst layers, and a cooling medium flows into and out of the cooling layers to cool the catalyst layers.

[0006]

However, in the above technique, the cooling medium flows into and out of the cooling layer to uniformly cool the catalyst layer. That is, the cooling power of the cooling layer is kept constant. Here, since the gas to be treated is introduced from the inlet of the catalyst layer, the reaction speed is higher near the inlet than near the outlet. That is, since the reaction is more likely to occur near the inlet than in the vicinity of the outlet, the temperature is higher. Therefore,
If the catalyst layer is cooled with a uniform cooling power, the temperature near the inlet of the catalyst layer and the temperature near the outlet are different, and a temperature distribution occurs in the catalyst layer.

When such a temperature distribution occurs, even if the temperature near the inlet is set to an optimum temperature for reducing carbon monoxide, the temperature near the outlet becomes too low, and the above equation (1) The reaction hardly occurs. Conversely, even when the temperature near the outlet is set to an optimum temperature, the temperature near the inlet becomes too high, and the reverse shift reaction shown in the above equation (3) is likely to occur near the inlet.

As a result, since the entire catalyst layer cannot be maintained at an optimum temperature, there is a problem that carbon monoxide contained in the gas to be treated cannot be reliably reduced.

The present invention has been made to solve the above-mentioned conventional problems. That is, an object of the present invention is to provide a carbon monoxide reduction method and a carbon monoxide reduction reactor that can surely reduce carbon monoxide contained in a gas to be treated.

[0010]

According to the present invention, there is provided a method for reducing carbon monoxide, wherein a plurality of cooling layers are alternately provided, and a plurality of catalyst supporting layers supporting a catalyst contain carbon monoxide and an oxidizing agent. A carbon monoxide reduction method for introducing a processing gas, oxidizing and reducing carbon monoxide in the gas to be processed, and discharging the processing gas with reduced carbon monoxide, wherein a cooling medium flows out to the cooling layer. And reducing the carbon monoxide while reducing the temperature distribution of the catalyst carrier layer from the side of introduction of the gas to be treated to the side of discharge of the treatment gas. In the carbon monoxide reduction reaction method of the present invention, a cooling medium flows into and out of the cooling layer, and the temperature distribution of the catalyst carrier layer from the introduction side of the gas to be treated to the exhaust side of the treatment gas is reduced. Since the carbon monoxide is reduced, the carbon monoxide contained in the gas to be treated can be surely reduced.

The carbon monoxide reduction reactor of the present invention has a plurality of inlets for introducing a gas to be treated containing carbon monoxide and an oxidizing agent, and a plurality of outlets for discharging the processing gas having reduced carbon monoxide. And, a plurality of catalyst carrier layers having a catalyst carrier carrying a catalyst, and a treatment gas introducing means connected to the catalyst carrier layer and introducing the gas to be treated into each of the catalyst carrier layers, A plurality of cooling mediums, which are arranged alternately with the respective catalyst supporting layers, cool the catalyst supporting layer and reduce the temperature distribution of the catalyst supporting body layer from the inlet to the outlet, and allow a cooling medium to flow in and out. It is characterized by comprising a cooling layer and cooling medium inflow means connected to each of the cooling layers and flowing the cooling medium into each of the cooling layers.
In the carbon monoxide reduction reactor of the present invention, the catalyst support layers are alternately disposed, and the catalyst support layers are cooled to reduce the temperature distribution of the catalyst support layer from the inlet to the outlet. Since the cooling medium is provided with a plurality of cooling layers through which the cooling medium can flow, carbon monoxide contained in the gas to be treated can be reliably reduced.

Another carbon monoxide reduction reactor according to the present invention comprises a plurality of inlets for introducing a gas to be treated containing carbon monoxide and an oxidizing agent, and a plurality of outlets for discharging a treatment gas reduced in carbon monoxide. A plurality of catalyst carrier layers having a plurality of catalyst carrier portions each having an exhaust port and having a catalyst carrier carrying a catalyst, and the gas to be treated connected to the catalyst carrier layer, And a plurality of cooling layers that are alternately arranged with the respective catalyst-supporting layers and through which a cooling medium can flow in and out, and are connected to the respective cooling layers, and the cooling layers are cooled by the respective cooling layers. Cooling medium inflow means for inflowing a medium,
It is characterized by having. In another carbon monoxide reduction reactor of the present invention, a plurality of inlets for introducing a gas to be treated including carbon monoxide and an oxidizing agent and a plurality of outlets for discharging a treatment gas having reduced carbon monoxide are provided. And a plurality of catalyst carrier layers having a plurality of catalyst carrier portions each having a catalyst carrier carrying a catalyst, so that the reaction efficiency on the outlet side can be improved, The temperature distribution of the catalyst carrier layer from the mouth to the outlet can be reduced.

[0013] Another carbon monoxide reduction reactor of the present invention comprises a plurality of inlets for introducing a gas to be treated containing carbon monoxide and an oxidizing agent, and a plurality of outlets for discharging the process gas reduced in carbon monoxide. A plurality of catalyst carrier layers having a plurality of catalyst carrier portions each having an exhaust port and having a catalyst carrier carrying a catalyst, and the gas to be treated connected to the catalyst carrier layer, Means for introducing a gas to be treated, oxidizing agent introducing means for introducing the oxidizing agent between the respective catalyst supporting members, and a plurality of the oxidizing agents which are alternately arranged with the respective catalyst supporting layers and through which a cooling medium can flow. And cooling medium inflow means connected to each of the cooling layers and flowing the cooling medium into each of the cooling layers. In another carbon monoxide reduction reactor of the present invention, since the oxidizing agent introducing means for introducing the oxidizing agent is provided between the respective catalyst carriers, the reaction can be dispersed and a rapid temperature rise can be suppressed. be able to.

[0014]

DESCRIPTION OF THE PREFERRED EMBODIMENTS (First Embodiment) Hereinafter, a fuel cell system according to a first embodiment of the present invention will be described. In this embodiment, a description will be given using a polymer fuel cell system as the fuel cell system. FIG.
FIG. 1 is a diagram schematically showing a configuration of a polymer electrolyte fuel cell system according to the present embodiment. As shown in FIG. 1, the polymer electrolyte fuel cell system 1 includes a polymer electrolyte fuel cell 2 and a fuel gas supply system 3 for supplying a fuel gas of an organic compound such as a hydrocarbon or alcohol. ing. In addition, a reformer 4 for generating a reformed gas containing hydrogen as a main component from a fuel gas, a carbon monoxide converter 5 for reducing carbon monoxide contained in the reformed gas, and a carbon monoxide converter And a carbon monoxide reduction reactor for further reducing the carbon monoxide contained in the reformed gas discharged from the fuel cell 5. Here, the direction in which the fuel gas supply system 3 is disposed will be referred to as the upstream side, and the direction in which the polymer electrolyte fuel cell 2 is disposed will be referred to as the downstream side. The arrangement of each device in the polymer electrolyte fuel cell system 1 will be specifically described. Each device includes a fuel gas supply system 3, a reformer 4, a carbon monoxide converter 5 from an upstream side to a downstream side. , A carbon monoxide reduction reactor 6, and a polymer electrolyte fuel cell 2. Each device is connected in series by piping.

The fuel gas supply system 3 mainly includes a liquid fuel tank 31 containing a liquid fuel mixture of liquid methanol and water, a pump 32 for pumping liquid fuel from the liquid fuel tank 31, and a liquid fuel tank 31 from the liquid fuel tank 31. And a vaporizer 33 for vaporizing the liquid fuel pumped by the pump 32. An appropriate amount of fuel can be pumped by controlling the operation of the pump 32, and the liquid fuel can be changed to fuel gas by vaporizing the liquid fuel by the vaporizer 33. .

The reformer 4 is connected to the vaporizer 33 via the compressor 7, and the fuel gas vaporized by the vaporizer 33 is introduced by the operation of the compressor 7. Further, the reformer 4 has a heating means such as a resistance heating element, and heats a fuel gas introduced into the reformer 4 and steam described below. The reformer 4 is connected to a steam introduction system 8 and an air introduction system 9 for introducing steam and air.
Steam is introduced into the reformer 4 from the steam introduction system 8,
By heating together with the fuel gas, a steam reforming reaction occurs in the reformer 4, and a reformed gas mainly composed of hydrogen is generated from the fuel gas. In addition, by introducing air from the air introduction system 9 to the reformer 4, a partial oxidation reaction occurs in the reformer 4 to generate the above-described reformed gas. In the method for generating the reformed gas using the partial oxidation reaction, heat is generated by oxygen in the air, so that a heating unit is not required, and the space of the reformer 4 can be saved. In the present embodiment, both a steam reforming reaction and a partial oxidation reaction are used as a method for generating the reformed gas.

The reformer 4 is connected to a carbon monoxide converter 5 via a compressor 10 so that the reformed gas generated in the reformer 4 is introduced. In the carbon monoxide converter 5, a rightward reaction (shift reaction) of the above equation (3) is caused to change carbon monoxide contained in the reformed gas into carbon dioxide, thereby reducing carbon monoxide. It has become. By reducing carbon monoxide from the reformed gas in the carbon monoxide converter 5, poisoning of an anode electrode of the polymer electrolyte fuel cell 2 described later can be reduced. However, when the concentration of carbon monoxide contained in the reformed gas is low, the carbon monoxide converter 5 can be omitted.

A carbon monoxide reduction reactor 6 is connected to the carbon monoxide converter 5 via a compressor 11 as a means for introducing a gas to be treated. An oxidant tank 12 containing an oxidant for oxidizing carbon monoxide, such as air, is provided through a compressor 13 in a pipe between the carbon monoxide converter 5 and the carbon monoxide reduction reactor 6. It is connected.

The polymer electrolyte fuel cell 2 is connected to the carbon monoxide reduction reactor 6 via a compressor 14. The polymer electrolyte fuel cell 2 mainly includes an anode electrode, a cathode electrode, and a polymer polymer membrane. An air introduction system 15 for introducing air into the polymer electrolyte fuel cell 2 is connected to the polymer electrolyte fuel cell 2. The polymer electrolyte fuel cell 2 is configured to generate power by introducing a reformed gas into the anode electrode and introducing air into the cathode electrode.

Next, the carbon monoxide reduction reactor 6 according to the present embodiment will be described. FIG. 2 is a perspective view schematically illustrating the carbon monoxide reduction reactor 6 according to the present embodiment, and FIG. 3 is a schematic view illustrating the carbon monoxide reduction reactor 6 according to the present embodiment. FIG. FIG. 4 is a vertical sectional view schematically showing the inside of the carbon monoxide reduction reactor 6 according to the present embodiment, and FIG. 5 is the inside of the carbon monoxide reduction reactor 6 according to the present embodiment. FIG. 2 is a plan view schematically showing As shown in FIGS. 2 to 5, the carbon monoxide reduction reactor 6 according to the present embodiment includes a box-shaped case 21. An upstream surface of the case 21 has a reformed gas discharged from the carbon monoxide converter 5 and an oxidizing agent introduced from the oxidizing agent tank 12 (hereinafter referred to as both reforming gas and oxidizing agent). Is referred to as “gas to be treated”).
A case introduction port 22 is formed for introduction into the case 1. Further, a case outlet 2 for discharging a reformed gas (hereinafter, referred to as “process gas”) in which carbon monoxide oxidized by an oxidizing agent is reduced is provided on a downstream surface of the case 21.
3 are provided. The case outlet 23 is connected to the polymer electrolyte fuel cell 2 via a pipe. In the case 21, a honeycomb catalyst layer 25 as a plurality of catalyst carrier layers having a flow path 24 formed in a honeycomb shape, and a plurality of cooling layers 26 alternately stacked with the honeycomb catalyst layer 25 are accommodated. I have. Here, the term “honeycomb” refers to a shape provided with a plurality of through holes, and the shape of the holes is not limited. That is, various shapes such as a quadrangle and a hexagon can be adopted as the shape of the hole. By making the honeycomb catalyst layer 25 into a honeycomb shape, the contact area with the gas to be treated can be increased. Hereinafter, the upstream end of the flow path 24 of the honeycomb catalyst layer 25 is referred to as a honeycomb catalyst layer inlet, and the downstream end is referred to as a honeycomb catalyst layer outlet. The gas to be processed passes through the flow path 24 from the honeycomb catalyst layer introduction port 27 serving as an inlet to the honeycomb catalyst layer discharge port 28 serving as a discharge port.

The honeycomb catalyst layer 25 is formed of, for example, a box-shaped material made of a material such as cordierite-based ceramics that can withstand heat generated by oxidation of carbon monoxide. In particular, it is preferable to be formed of a metal. The reason that the honeycomb catalyst layer 25 is preferably formed of metal is that the cooling layer 26 is generally formed of metal.
This is because heat transfer characteristics can be improved, and the honeycomb catalyst layer 25 whose temperature has increased due to oxidation of carbon monoxide can be efficiently cooled. Furthermore, among metals,
When the honeycomb catalyst layer 25 is formed of copper, the heat transfer characteristics can be further improved, and when formed of aluminum, the weight can be reduced. In addition, a base as a catalyst carrier that carries a catalyst is formed in each channel 24 of each honeycomb catalyst layer 25. By supporting the catalyst on the base, the same reaction efficiency as when the base is not used can be obtained with a small amount of the catalyst. Also,
The catalyst supported on the base is a catalyst that selectively oxidizes carbon monoxide, such as nickel or chromium. Here, the reason why the catalyst for selectively oxidizing carbon monoxide is used is that the main component of the reformed gas is hydrogen, so that carbon monoxide is preferentially oxidized over hydrogen. In particular, noble metal catalysts such as a platinum catalyst, a ruthenium catalyst, and a palladium catalyst are preferable. The noble metal-based catalyst is preferred because the reaction efficiency of the oxidation reaction can be improved. In this embodiment, a case where a platinum-based catalyst is supported as a catalyst will be described. As a method for supporting the catalyst on the base, impregnation, thermal spraying, electrodeposition, sputtering and the like can be mentioned.

The cooling layer 26 is formed of, for example, a box-shaped metal. An inflow port 29 through which a cooling medium supplied from a cooling medium inflow unit to be described later flows into the cooling layer 26 is formed in an upstream portion of the cooling layer 26. An outlet 30 for allowing the cooling medium to flow out of the cooling layer 26 is formed in a downstream portion of the cooling layer 26. By flowing the cooling medium from the upstream side to the downstream side, it is possible to effectively suppress a rapid temperature rise near the honeycomb catalyst layer inlet 27 of the honeycomb catalyst layer 25 due to the oxidation reaction of carbon monoxide. This is because the cooling medium having the largest cooling power flows into the portion where the temperature rises most. In each cooling layer 26, a flow path 31 through which a cooling medium flows is formed. The cross-sectional area of the flow channel 31 gradually increases (increases) from the inlet 29 to the outlet 30. That is, the flow path 31
Is formed so as to gradually increase from the upstream side to the downstream side. The flow path 31 can be formed of, for example, a plate-like member or a tubular member.
A cooling medium inflow means 32 for flowing a cooling medium into the cooling layer 26 is connected to the 6 inlets 29 via a pipe 33. Specifically, the cooling medium inflow means 32 includes, for example, a cooling medium tank 34 for storing a cooling medium, and a cooling medium pumped from the cooling medium tank 34 to form a cooling layer 26.
And a pump 35 for flowing into the inside. Further, the cooling medium flowing out of the outlet 30 of the cooling layer 26 can be returned to the cooling medium tank 34 and circulated. As a cooling medium that flows from the cooling medium inflow means 32 into the cooling layer 26, a gas or a liquid used, consumed, and generated in the polymer electrolyte fuel cell system 1 can be used. For example, it is possible to use the cooling water used in the polymer electrolyte fuel cell 2, the water generated in the polymer electrolyte fuel cell 2, and the air supplied to the polymer electrolyte fuel cell 2. . By using such a gas or liquid as a cooling medium for the cooling layer 26, running costs can be reduced.

Next, a flow of power generation performed in the polymer electrolyte fuel cell system 1 will be described. FIG. 6 is a flowchart showing the overall flow of the polymer electrolyte fuel cell system 1 according to the present embodiment. First, the pump 32
Is operated to pump out the liquid fuel from the liquid fuel tank 31 and introduce the liquid fuel into the vaporizer 33. When the liquid fuel is introduced into the vaporizer 33, the liquid fuel is vaporized and changed to a fuel gas (step 1).

After the liquid fuel is changed to fuel gas, the compressor 7 is operated, and the fuel gas and steam are introduced into the reformer 4 by the steam introduction system 8 and heated. This heating causes a steam reforming reaction. Fuel gas,
And air is introduced into the reformer 4 by the air introduction system 9 and mixed. This mixing causes a partial oxidation reaction. A reformed gas containing hydrogen as a main component is generated from the fuel gas by a steam reforming reaction and a partial oxidation reaction (step 2).

After generating the reformed gas, the compressor 1
0 is operated to introduce the reformed gas into the carbon monoxide converter 5. In the carbon monoxide converter 5, a shift reaction as shown in the above equation (3) occurs, and carbon monoxide contained in the reformed gas is changed to carbon dioxide to reduce carbon monoxide (step 3). .

After the carbon monoxide has been reduced to some extent, the compressor 13 is operated to introduce the oxidant from the oxidant tank 12 into the piping, and
Is operated to introduce the gas to be treated into the carbon monoxide reduction reactor 6 from the case inlet 22. In addition, the gas to be treated is introduced, and the pump 35 is operated to pump up the cooling medium from the cooling medium tank 34 and to supply the cooling medium to the inlet 29.
From the cooling layer 26. When the gas to be treated passes through the honeycomb catalyst layer introduction port 27 and enters the flow channel 24 of the honeycomb catalyst layer 66, the carbon monoxide in the reformed gas and the carbon dioxide in the oxidant are deposited on the surface of the catalyst supported on the base. Oxygen adheres.
The carbon monoxide and oxygen attached on the catalyst surface are separated from the catalyst surface by the reaction of the above formula (1). That is, carbon monoxide is oxidized to carbon dioxide and separated. Thereafter, the processing gas with reduced carbon monoxide is discharged from the carbon monoxide reduction reactor 6 through the honeycomb catalyst layer discharge port 28 and the case discharge port 23 (Step 4). Here, in the present embodiment, the honeycomb catalyst layer 2 extending from the honeycomb catalyst layer inlet 27 to the honeycomb catalyst layer outlet 28 is used.
Since the temperature distribution of No. 5 can be reduced, carbon monoxide contained in the gas to be treated can be reliably reduced. That is, the gas to be processed is introduced, and the cooling medium is caused to flow into the cooling layer 26 from the inflow port 29. Since the flow path 31 of the cooling layer 26 is formed so as to gradually widen from the inflow port 29 to the outflow port 30, the cooling power of the cooling layer 26 is reduced from the honeycomb catalyst layer introduction port 27 to the honeycomb catalyst layer discharge port. It gradually decreases (gradually decreases) toward the outlet 28. Therefore, the cooling power is increased in the portion where the temperature rise is high, and the cooling power is reduced in the portion where the temperature rise is low, so that the temperature of the honeycomb catalyst layer 25 from the honeycomb catalyst layer inlet 27 to the honeycomb catalyst layer outlet 28 is reduced. The distribution can be reduced. Therefore, the entire honeycomb catalyst layer 25 can be maintained at an optimum temperature for reliably reducing carbon monoxide, and the carbon monoxide contained in the gas to be treated can be reduced to, for example, several ppm or less. .

After the processing gas is discharged from the carbon monoxide reduction reactor 6, the compressor 14 is operated to introduce the reformed gas into the polymer electrolyte fuel cell 2, and the air is introduced to the solid polymer fuel cell 2 by the air introduction system 15. It is introduced into the molecular fuel cell 2 to generate power (step 5).

(Second Embodiment) Hereinafter, a second embodiment of the present invention will be described.
The carbon monoxide reduction reactor according to the embodiment will be described. In the following description, among the embodiments after this embodiment, description of contents which are the same as those of the preceding embodiment will be omitted. In the present embodiment, the cooling layer is divided substantially equally to form a plurality of cooling sections, and each cooling section is cooled so that the flow rate of the cooling medium gradually decreases from the upstream cooling section to the downstream cooling section. The medium was made to flow in. FIG. 7 is a vertical sectional view schematically showing the inside of the carbon monoxide reduction reactor according to the present embodiment, and FIG. 8 is a schematic view showing the inside of the carbon monoxide reduction reactor according to the present embodiment. FIG. As shown in FIGS. 7 and 8, the cooling layer 40 according to the present embodiment is divided into a plurality of substantially equal parts, and a plurality of, for example, box-shaped cooling parts 41 are formed by this division. Each cooling unit 41 has a cooling medium inflow means 42.
Pump 43 is connected. Each of the pumps 43 is electrically connected to a cooling medium inflow controller 44 for controlling the operation of each of the pumps 43 so as to control the flow rate of the cooling medium flowing into each of the cooling units 41. Specifically, the cooling medium inflow control unit 44 controls the operation of the pump 43 so that the flow rate of the cooling medium gradually decreases, for example, from the upstream cooling unit 41 to the downstream cooling unit 41. Has become.

As described above, in the present embodiment, the cooling layer 4
0 is almost equally divided to form a plurality of cooling sections 41, and when reducing the carbon monoxide contained in the gas to be treated,
Since the flow rate of the cooling medium flowing into each cooling section 41 is controlled by the cooling medium inflow control section 44, the carbon monoxide contained in the gas to be processed can be more reliably reduced. That is, when the carbon monoxide contained in the gas to be treated is reduced, the operation of the pump 43 is controlled by the cooling medium inflow control unit 44, so that each cooling unit 41 is provided with the upstream cooling unit 41. A cooling medium having a flow rate that gradually decreases flows into the cooling unit 41 on the downstream side. As a result, the cooling layer 40
Can be gradually reduced from the upstream side to the downstream side. Therefore, the cooling power is increased in a portion where the temperature rise is high, and the cooling power is reduced in a portion where the temperature rise is low, so that the entire honeycomb catalyst layer 25 can be maintained at an optimum temperature. Therefore, carbon monoxide contained in the gas to be treated can be reliably reduced.

(Third Embodiment) Hereinafter, a third embodiment of the present invention will be described.
The carbon monoxide reduction reactor according to the embodiment will be described. In the present embodiment, the cooling layer is divided so as to gradually increase in volume from the upstream side to the downstream side to form a plurality of cooling portions, and the cooling medium flows into each of the cooling portions at a substantially equal flow rate. FIG. 9 is a vertical cross-sectional view schematically illustrating the inside of the carbon monoxide reduction reactor according to the present embodiment, and FIG. 10 is a schematic view illustrating the inside of the carbon monoxide reduction reactor according to the present embodiment. FIG. 9 and 1
As shown in FIG. 0, the cooling layer 50 of the present embodiment is divided into a plurality of portions such that the volume gradually increases from the upstream side to the downstream side, and a plurality of cooling portions 51 are formed by this division. . A pump 53 of a cooling medium inflow means 52 is connected to each cooling unit 51. Each pump 53
Is connected to a cooling medium inflow control unit 54 for controlling the operation of each pump 53, and controls the flow rate of the cooling medium flowing into each cooling unit 51. Specifically, the cooling medium inflow control unit 54 includes, for example, the upstream cooling unit 5.
Each pump 53 is controlled so that the flow rate of the cooling medium is substantially uniform from 1 to the cooling section 51 on the downstream side.

As described above, in the present embodiment, the cooling layer 5
0 is divided so that the volume gradually increases from the upstream side to the downstream side to form a plurality of cooling units 51, and when the carbon monoxide contained in the gas to be treated is reduced, the cooling medium inflow control unit Since the flow rate of the cooling medium flowing into each cooling section 51 is controlled at 54, the carbon monoxide contained in the gas to be treated can be reduced more reliably. That is, when the carbon monoxide contained in the reformed gas is reduced, each cooling unit 51 is controlled by the cooling medium inflow control unit 54 so that the cooling unit 51 includes the upstream cooling unit 51 and the downstream cooling unit 51. A substantially uniform flow rate of the cooling medium flows in. As a result, the cooling layer 50
Can be gradually reduced from the upstream side to the downstream side. Therefore, the cooling power is increased in a portion where the temperature rise is high, and the cooling power is reduced in a portion where the temperature rise is low, so that the entire honeycomb catalyst layer 25 can be maintained at an optimum temperature. Therefore, carbon monoxide contained in the gas to be treated can be reliably reduced.

(Fourth Embodiment) Hereinafter, a fourth embodiment of the present invention will be described.
The carbon monoxide reduction reactor according to the embodiment will be described. In this embodiment, the length from the upstream side to the downstream side of the cooling layer is shorter than the length of the honeycomb catalyst layer in the same direction. FIG. 11 is a vertical sectional view schematically illustrating the inside of the carbon monoxide reduction reactor according to the present embodiment, and FIG. 12 is a schematic view illustrating the inside of the carbon monoxide reduction reactor according to the present embodiment. FIG. FIG.
As shown in FIG. 12 and FIG.
Is formed such that the length from the upstream side to the downstream side is shorter than the length of the honeycomb catalyst layer 25 in the same direction. Specifically, for example, the length of the cooling layer 60 is made equal to the length from the honeycomb catalyst layer inlet 27 to the middle part of the honeycomb catalyst layer 25. The portion where the cooling layer 60 is not provided has a heat insulating structure.

As described above, in the present embodiment, the cooling layer 6
By forming the length from the upstream side to the downstream side of 0 to be shorter than the length of the honeycomb catalyst layer 60 in the same direction, the carbon monoxide contained in the gas to be treated can be more reliably reduced. That is, since the reaction for oxidizing carbon monoxide has a high reaction rate near the honeycomb catalyst layer introduction port 27, the reaction is almost completed from the honeycomb catalyst layer introduction port 27 to the middle part of the honeycomb catalyst layer 25. Therefore, the reaction hardly occurs near the honeycomb catalyst layer outlet 28,
The calorific value is small. Here, cooling the vicinity of the honeycomb catalyst layer outlet 28 may cause an excessive temperature drop. However, in the present embodiment, the length from the upstream side to the downstream side of the cooling layer 60 is formed shorter than the length of the honeycomb catalyst layer 25 in the same direction. Therefore, it is possible to prevent an excessive decrease in temperature near the honeycomb catalyst layer discharge port 28. Therefore, the entire honeycomb catalyst layer 25 can be maintained at an optimum temperature, and carbon monoxide contained in the gas to be treated can be reliably reduced. The cooling layer 60
Of the cooling layer 60
It is possible to save the cooling medium flowing into the apparatus.

(Fifth Embodiment) Hereinafter, a fifth embodiment of the present invention will be described.
The carbon monoxide reduction reactor according to the embodiment will be described. In the present embodiment, the inside of the honeycomb catalyst layer is divided substantially equally to form a plurality of honeycomb catalyst portions. FIG. 13 is a vertical sectional view schematically showing the inside of the carbon monoxide reduction reactor according to the present embodiment.
FIG. 1 is a plan view schematically showing the inside of a carbon monoxide reduction reactor according to the present embodiment. As shown in FIGS. 13 and 14, the inside of the honeycomb catalyst layer 70 according to the present embodiment is divided into a plurality, and a plurality of honeycomb catalyst portions 71 are formed inside the honeycomb catalyst layer 70 by this division. ing. By dividing the inside of the honeycomb catalyst layer 70 substantially equally to form a plurality of honeycomb catalyst portions 71, the contact probability of contact between the catalyst and the gas to be treated is improved. Note that the cooling power of the cooling layer 72 according to the present embodiment is substantially uniform.

Next, the reaction of the gas to be treated in the honeycomb catalyst layer 70 according to the present embodiment will be described. A gas to be treated is introduced from a honeycomb catalyst layer introduction port 73 of a honeycomb catalyst layer 70 having a plurality of honeycomb catalyst portions 71. Here, from the upstream side to the downstream side, a first honeycomb catalyst section, a second honeycomb catalyst section,..., An n-th honeycomb catalyst section are referred to. The introduced gas to be processed reacts in the flow path of the first honeycomb catalyst unit, but the gas to be processed that has passed through the flow path of the first honeycomb catalyst unit without reacting flows through the other flow path. The gas is mixed with the gas to be processed and introduced into the second honeycomb catalyst section. The gas to be processed introduced into the second honeycomb catalyst section reacts in the flow path to become a processing gas. Also,
The to-be-processed gas that has passed without reacting in the flow path of the second honeycomb catalyst unit is mixed with the to-be-processed gas that has passed through another flow path, and is introduced into the third honeycomb catalyst unit. Hereinafter, similarly, the gas to be treated mixed into the fourth honeycomb catalyst section,..., N-th catalyst section is introduced.

As described above, in the present embodiment, by dividing the inside of the honeycomb catalyst layer 70 substantially equally to form a plurality of honeycomb catalyst portions 71, the carbon monoxide contained in the gas to be treated can be reduced. It can be surely reduced. That is, by dividing the inside of the honeycomb catalyst layer 70 substantially equally to form the plurality of honeycomb catalyst portions 71, the gas to be treated is mixed, and the contact probability between the catalyst and the gas to be treated is improved. As a result, the gas to be treated also reacts in the downstream honeycomb catalyst section 71 to generate heat.
Accordingly, the temperature distribution of the honeycomb catalyst layer 70 from the honeycomb catalyst layer inlet 73 to the honeycomb catalyst layer outlet 74 is reduced. Therefore, even when the honeycomb catalyst layer is uniformly cooled by the cooling layer 72, the entire honeycomb catalyst layer 70 can be maintained at an optimum temperature, and the carbon monoxide contained in the gas to be treated can be reliably reduced. Can be reduced.

(Sixth Embodiment) Hereinafter, a sixth embodiment of the present invention will be described.
The carbon monoxide reduction reactor according to the embodiment will be described. In the present embodiment, the honeycomb catalyst portion is formed so that the number of flow passages is gradually increased from the honeycomb catalyst portion on the honeycomb catalyst layer inlet side to the honeycomb catalyst portion on the honeycomb catalyst layer outlet side. . FIG. 15 is a vertical sectional view schematically showing the inside of the carbon monoxide reduction reactor according to the present embodiment, and FIG. 16 is a schematic view showing the inside of the carbon monoxide reduction reactor according to the present embodiment. FIG. As shown in FIGS. 15 and 16, a plurality of honeycomb catalyst portions 81 as described in the fifth embodiment are formed inside a honeycomb catalyst layer 80 according to the present embodiment. Here, each honeycomb catalyst portion 81 is formed such that the number of flow paths 82 gradually increases from the honeycomb catalyst portion 81 on the honeycomb catalyst layer inlet 83 side to the honeycomb catalyst portion 81 on the honeycomb catalyst layer outlet 84 side. Have been. Channel 8
The number 4 is gradually increased from the honeycomb catalyst portion 81 on the side of the honeycomb catalyst layer introduction port 83 to the honeycomb catalyst portion 81 on the side of the honeycomb catalyst layer discharge port 84. The contact probability between the catalyst and the gas to be treated is improved over the catalyst layer discharge port 84 so that the reaction can be reliably performed also on the honeycomb catalyst layer discharge port 84 side.

Next, the reaction of the gas to be treated in the honeycomb catalyst layer 80 according to the present embodiment will be described. A gas to be treated is introduced from a honeycomb catalyst layer introduction port 83 of a honeycomb catalyst layer 80 having a plurality of honeycomb catalyst sections 81. Here, in the present embodiment, the number of channels 82 is formed so as to gradually increase from the honeycomb catalyst portion 81 on the honeycomb catalyst layer inlet 83 side to the honeycomb catalyst portion 81 on the honeycomb catalyst layer outlet 84 side. ing. That is, the reaction speed of the gas to be processed increases from the first honeycomb catalyst portion to the n-th honeycomb catalyst portion. Therefore, the possibility that the gas to be treated introduced into the first honeycomb catalyst portion passes without reacting in the first honeycomb catalyst portion increases. The gas to be processed that has passed through the first honeycomb catalyst section gradually reacts from the second honeycomb catalyst section to the n-th honeycomb catalyst section.

As described above, in the present embodiment, the plurality of honeycomb catalyst portions 81 are connected to the honeycomb catalyst portions 81 on the side of the honeycomb catalyst layer inlet 83 from the honeycomb catalyst portions 81 on the side of the honeycomb catalyst layer outlet 84. Since the gas is formed so as to gradually increase toward the portion 81, the carbon monoxide contained in the gas to be treated can be more reliably reduced. That is,
By forming the number of the flow passages 82 so as to gradually increase from the honeycomb catalyst portion 81 on the honeycomb catalyst layer inlet 83 side to the honeycomb catalyst portion 81 on the honeycomb catalyst layer outlet 84 side, the reaction of the gas to be treated is increased. Honeycomb catalyst layer inlet 8
It gradually occurs from the third side to the honeycomb catalyst layer discharge port 84 side. As a result, the honeycomb catalyst layer inlet 83
The temperature distribution of the honeycomb catalyst layer 80 from the outlet to the honeycomb catalyst layer outlet 84 is reduced. Therefore, even when the honeycomb catalyst layer 80 is uniformly cooled by the cooling layer 72, the entire honeycomb catalyst layer 80 can be maintained at an optimum temperature, and the carbon monoxide contained in the gas to be treated can be further reduced. It can be surely reduced.

(Seventh Embodiment) Hereinafter, a seventh embodiment of the present invention will be described.
The carbon monoxide reduction reactor according to the embodiment will be described. In the present embodiment, the amount of the catalyst supported on the base of the honeycomb catalyst portion is gradually increased from the honeycomb catalyst portion on the honeycomb catalyst layer introduction port side to the honeycomb catalyst portion on the honeycomb catalyst layer discharge port side. FIG. 17 is a vertical sectional view schematically showing the inside of the carbon monoxide reduction reactor according to the present embodiment, and FIG. 18 is a schematic view showing the inside of the carbon monoxide reduction reactor according to the present embodiment. FIG. As shown in FIGS. 17 and 18, a plurality of honeycomb catalyst portions 91 as described in the fifth embodiment are formed inside a honeycomb catalyst layer 90 according to the present embodiment. Here, the amount of the catalyst in each honeycomb catalyst section 91 is determined by the amount of the honeycomb catalyst section 91 on the honeycomb catalyst layer introduction port 92 side.
From the honeycomb catalyst layer outlet 93 side of the honeycomb catalyst portion 91
, Gradually increasing. By gradually increasing the amount of the catalyst from the honeycomb catalyst portion 81 on the honeycomb catalyst layer inlet 92 side to the honeycomb catalyst portion 81 on the honeycomb catalyst layer outlet 93 side, the amount of catalyst is gradually increased from the honeycomb catalyst layer inlet 92 to the honeycomb catalyst layer outlet. Through 93, the contact probability of contact between the catalyst and the gas to be treated is improved, so that the reaction is surely caused also on the honeycomb catalyst layer outlet 93 side.

Next, the reaction of the gas to be treated in the honeycomb catalyst layer 90 according to the present embodiment will be described. A gas to be treated is introduced from a honeycomb catalyst layer inlet 92 of a honeycomb catalyst layer 90 having a plurality of honeycomb catalyst portions 91. Here, in the present embodiment, the amount of the catalyst gradually increases from the honeycomb catalyst section 91 on the honeycomb catalyst layer inlet 92 side to the honeycomb catalyst section 91 on the honeycomb catalyst layer outlet 93 side. That is, as the gas to be processed progresses from the first honeycomb catalyst portion to the n-th honeycomb catalyst portion, the reaction becomes easier. Therefore, the gas to be treated introduced into the first honeycomb catalyst section passes through more than reacts in the first honeycomb catalyst section. The gas to be processed that has passed through the first honeycomb catalyst section gradually reacts from the second honeycomb catalyst section to the n-th honeycomb catalyst section.

As described above, in the present embodiment, the amount of the catalyst supported on the base of the honeycomb catalyst portion 91 is changed from the honeycomb catalyst portion 91 on the honeycomb catalyst layer inlet 92 side to the honeycomb catalyst portion on the honeycomb catalyst layer outlet 93 side. Since the temperature is gradually increased toward 91, carbon monoxide contained in the gas to be treated can be more reliably reduced. That is, the amount of the catalyst is adjusted to the honeycomb catalyst portion 91 on the honeycomb catalyst layer introduction port 92 side.
From the honeycomb catalyst layer outlet 93 side of the honeycomb catalyst portion 91
, The reaction of the gas to be treated gradually occurs from the honeycomb catalyst layer inlet 92 to the honeycomb catalyst layer outlet 93. as a result,
Honeycomb catalyst layer inlet 92 to honeycomb catalyst layer outlet 9
The temperature distribution of the honeycomb catalyst layer 91 toward 3 decreases. Therefore, even when the honeycomb catalyst layer 91 is uniformly cooled by the cooling layer 72, the entire honeycomb catalyst layer 91 is
It is possible to maintain the temperature at an optimum value for surely reducing carbon monoxide, and it is possible to more reliably reduce carbon monoxide contained in the gas to be treated.

(Eighth Embodiment) Hereinafter, an eighth embodiment of the present invention will be described.
The carbon monoxide reduction reactor according to the embodiment will be described. In the present embodiment, the configuration is such that the oxidizing agent is introduced into the space between the honeycomb catalyst portions. FIG. 19 is a vertical cross-sectional view schematically illustrating the inside of the carbon monoxide reduction reactor according to the present embodiment, and FIG. 20 is a schematic view illustrating the inside of the carbon monoxide reduction reactor according to the present embodiment. FIG.
As shown in FIG. 19 and FIG. 20, a plurality of honeycomb catalyst portions 101 as described above are formed inside the honeycomb catalyst layer 100 according to the present embodiment. Here, between the honeycomb catalyst unit 101 and the honeycomb catalyst unit 101,
A pipe 102 as an oxidant introducing means for introducing an oxidant and a compressor 103 are connected. This pipe 10
2 is also connected to the oxidizing agent tank 12, and operates the compressor 103 to introduce the oxidizing agent contained in the oxidizing agent tank 12 into the space between the honeycomb catalyst units 101. It is supposed to. Further, an oxidant introduction control unit 104 that controls the operation of each compressor 103 is electrically connected to each compressor 103 so that the amount of the oxidant introduced into the space between the honeycomb catalyst units 101 is controlled. Has become. Here, the amount of the oxidizing agent introduced between the respective honeycomb catalysts 101 is set in accordance with the concentration of carbon monoxide contained in the gas to be treated, the flow rate of the gas to be treated, or a change in load.

Next, the reaction of the gas to be treated in the honeycomb catalyst layer 100 according to the present embodiment will be described. Honeycomb catalyst layer 100 having a plurality of honeycomb catalyst portions 101
The gas to be treated is introduced from the honeycomb catalyst layer introduction port 105 of the above. Here, in the present embodiment, the oxidizing agent is introduced into the honeycomb catalyst layer introduction port 105 and the compressor 103 is operated between the respective honeycomb catalyst portions to introduce the oxidizing agent. That is, since a new oxidizing agent is introduced into the space between the respective honeycomb catalyst units 101, the reaction is dispersed.

As described above, in the present embodiment, since the oxidizing agent is introduced into the space between the respective honeycomb catalyst units 101, the carbon monoxide contained in the gas to be treated can be reduced more reliably. That is, the reaction is dispersed by introducing the oxidizing agent into the space between the respective honeycomb catalyst units 101. As a result, the temperature distribution of the honeycomb catalyst layer 100 decreases from the honeycomb catalyst layer inlet 105 to the honeycomb catalyst layer outlet 106. Therefore, the honeycomb catalyst layer 1 in the cooling layer 72
00, the entire honeycomb catalyst layer 100 can be maintained at an optimum temperature for surely reducing carbon monoxide, and the amount of carbon monoxide contained in the gas to be treated can be reduced. It can be surely reduced.

The present invention is not limited to the description of the above embodiment, and the structure, material, arrangement of each member, and the like can be appropriately changed without departing from the gist of the present invention. For example, in the second embodiment, the flow rate of the cooling medium is changed to reduce the temperature distribution of the honeycomb catalyst layer 25. Can also be reduced. That is, a cooling medium having a large cooling power is introduced into the honeycomb catalyst layer introduction port 27 side, and a cooling medium having a small cooling power is introduced into the honeycomb catalyst layer discharge port 28 side.

In the fifth embodiment, a plurality of honeycomb catalyst portions 71 are formed to surely reduce carbon monoxide from the gas to be treated. Thus, carbon monoxide can be more reliably reduced from the gas to be treated. Specifically, for example, when two honeycomb catalyst portions 71 are present, a platinum-based catalyst is supported on the honeycomb catalyst portion 71 on the honeycomb catalyst layer inlet 73 side, and the honeycomb catalyst portion 71 on the honeycomb catalyst outlet 74 side. Is loaded with a ruthenium-based catalyst. Here, the platinum catalyst is supported on the honeycomb catalyst layer introduction port 73 side and the ruthenium catalyst is supported on the honeycomb catalyst discharge port 74 side, because the ruthenium catalyst is supported on the honeycomb catalyst layer introduction port 73 side. , Heat generated by the oxidation reaction of carbon monoxide,
This is because a reaction as shown in the following formula (4) proceeds and a large amount of hydrogen is consumed.

Embedded image By supporting a platinum-based catalyst on the honeycomb catalyst portion 71 on the side of the honeycomb catalyst layer introduction port 73 and supporting a ruthenium-based catalyst on the honeycomb catalyst portion 71 on the side of the honeycomb catalyst outlet 74, most of the platinum-based catalyst is used for the monoxide. The carbon can be changed to carbon dioxide, and then a small amount of carbon monoxide can be converted to methane with a ruthenium-based catalyst, and the carbon monoxide can be more reliably reduced from the gas to be treated. Similarly, a palladium-based catalyst may be supported on the honeycomb catalyst layer inlet 73 side, and a ruthenium-based catalyst may be supported on the honeycomb catalyst outlet 74 side. Furthermore, in the above description, the case where two types of catalysts are supported on the two honeycomb catalyst units 71 has been described. However, the number of honeycomb catalyst units 71 and the number of types of catalysts may be different.

Further, in the first to eighth embodiments, the carbon monoxide reduction reactor is provided in the polymer electrolyte fuel cell system 1, but if the purpose is to reduce carbon monoxide, , Can be arranged in another system or device.

[0049]

As described above, according to the carbon monoxide reduction reaction method and the carbon monoxide reduction reactor of the present invention,
Carbon monoxide contained in the gas to be treated can be reliably reduced.

[Brief description of the drawings]

FIG. 1 is a diagram schematically showing a configuration of a polymer electrolyte fuel cell system according to a first embodiment.

FIG. 2 is a perspective view schematically showing a carbon monoxide reduction reactor according to the first embodiment.

FIG. 3 is a vertical sectional view schematically showing a carbon monoxide reduction reactor according to the first embodiment.

FIG. 4 is a vertical sectional view schematically showing the inside of the carbon monoxide reduction reactor according to the first embodiment.

FIG. 5 is a plan view schematically showing the inside of the carbon monoxide reduction reactor according to the first embodiment.

FIG. 6 is a flowchart showing a flow of the whole polymer electrolyte fuel cell system according to the first embodiment.

FIG. 7 is a vertical sectional view schematically showing the inside of a carbon monoxide reduction reactor according to a second embodiment.

FIG. 8 is a plan view schematically showing the inside of a carbon monoxide reduction reactor according to a second embodiment.

FIG. 9 is a vertical sectional view schematically showing the inside of a carbon monoxide reduction reactor according to a third embodiment.

FIG. 10 is a plan view schematically showing the inside of a carbon monoxide reduction reactor according to a third embodiment.

FIG. 11 is a vertical sectional view schematically showing the inside of a carbon monoxide reduction reactor according to a fourth embodiment.

FIG. 12 is a plan view schematically showing the inside of a carbon monoxide reduction reactor according to a fourth embodiment.

FIG. 13 is a vertical sectional view schematically showing the inside of a carbon monoxide reduction reactor according to a fifth embodiment.

FIG. 14 is a plan view schematically showing the inside of a carbon monoxide reduction reactor according to a fifth embodiment.

FIG. 15 is a vertical sectional view schematically showing the inside of a carbon monoxide reduction reactor according to a sixth embodiment.

FIG. 16 is a plan view schematically showing the inside of a carbon monoxide reduction reactor according to a sixth embodiment.

FIG. 17 is a vertical sectional view schematically showing the inside of a carbon monoxide reduction reactor according to a seventh embodiment.

FIG. 18 is a plan view schematically showing the inside of a carbon monoxide reduction reactor according to a seventh embodiment.

FIG. 19 is a vertical sectional view schematically showing the inside of a carbon monoxide reduction reactor according to an eighth embodiment.

FIG. 20 is a plan view schematically showing the inside of a carbon monoxide reduction reactor according to an eighth embodiment.

[Explanation of symbols]

6 Carbon monoxide reduction reactor 11, 103 Compressor 24, 82 Flow path 25, 70, 80, 90, 100 Honeycomb catalyst layer 26, 40, 50, 60, 72 Cooling layer 27, 73, 83 92, 105: honeycomb catalyst layer introduction port 28, 74, 84, 93, 106: honeycomb catalyst layer discharge port 31: flow path 32, 42, 52: cooling medium inflow means 41, 51: cooling unit 44, 54: cooling medium Inflow control unit 71, 81, 91, 101 ... honeycomb catalyst unit

 ──────────────────────────────────────────────────続 き Continuing on the front page (72) Inventor Ryo Harada 2-4-4 Suehirocho, Tsurumi-ku, Yokohama-shi, Kanagawa Prefecture Inside Toshiba Keihin Works (72) Inventor Shinkazu Suzuki 2--4, Suehirocho, Tsurumi-ku, Yokohama-shi, Kanagawa Address F-term in Toshiba Keihin Works (reference) 4G040 EA02 EA03 EA06 EB31 EB46 5H026 AA06 5H027 AA06 BA17 KK31 MM12 MM16

Claims (21)

[Claims] 1. A gas to be treated containing carbon monoxide and an oxidizing agent is introduced into a plurality of catalyst carrier layers, which are arranged alternately with a plurality of cooling layers and carry a catalyst, and the monoxide in the gas to be treated is introduced. A carbon monoxide reduction method for oxidizing and reducing carbon and discharging a processing gas with reduced carbon monoxide, wherein a cooling medium flows into and out of the cooling layer, and the processing gas is introduced from an introduction side of the gas to be processed. Reducing the carbon monoxide while reducing the temperature distribution of the catalyst carrier layer toward the discharge side of the carbon monoxide. 2. The method for reducing carbon monoxide according to claim 1, wherein the cooling medium flows into the cooling layer such that the cooling power of the cooling layer gradually decreases from the introduction side to the discharge side. A method for reducing carbon monoxide, comprising: 3. The method for reducing carbon monoxide according to claim 2, wherein the cooling layer has a flow path through which the cooling medium flows, and the flow path is cut from the introduction side to the discharge side. A method for reducing carbon monoxide, characterized in that the area is formed so as to increase gradually. 4. The method for reducing carbon monoxide according to claim 2, wherein said cooling layer has a plurality of cooling portions formed by dividing said cooling layer substantially equally. A method for reducing carbon monoxide, comprising: introducing a pre-cooling medium such that a flow rate of the cooling medium gradually decreases from the cooling section on the introduction side to the cooling section on the discharge side. 5. The method for reducing carbon monoxide according to claim 2, wherein the cooling layer is formed by dividing the cooling layer so as to increase in volume from the introduction side to the discharge side. A cooling medium having a flow rate substantially equal to each cooling section. 6. The method for reducing carbon monoxide according to claim 1, wherein the catalyst carrier layer has a plurality of catalyst carrier portions formed by dividing the catalyst carrier layer. To reduce carbon monoxide. 7. The method for reducing carbon monoxide according to claim 6, wherein each of the catalyst carriers has a flow path for flowing the gas to be processed and the processing gas, and the number of the flow paths is reduced. Wherein the amount is gradually increased from the catalyst carrier on the introduction side to the catalyst carrier on the discharge side. 8. The method for reducing carbon monoxide according to claim 6, wherein the amount of the catalyst carried on each of the catalyst carriers is changed from the catalyst carrier on the introduction side to the catalyst on the discharge side. A method for reducing carbon monoxide, wherein the amount is gradually increased toward a support portion. 9. It has a plurality of inlets for introducing a gas to be treated containing carbon monoxide and an oxidizing agent, and a plurality of outlets for discharging a treatment gas reduced in carbon monoxide, and carries a catalyst. A plurality of catalyst carrier layers having a catalyst carrier; a treatment gas introducing means connected to the catalyst carrier layer, for introducing the gas to be treated into each of the catalyst carrier layers; A plurality of cooling layers through which a cooling medium can flow, which cools the catalyst support layer and reduces the temperature distribution of the catalyst support layer from the inlet to the outlet, and And a cooling medium inflow means for connecting the cooling medium into each of the cooling layers. 10. The carbon monoxide reduction reactor according to claim 9, wherein the cooling layer is formed such that the cooling power of the cooling layer gradually decreases from the inlet to the outlet. A reactor for gradually reducing carbon monoxide, characterized in that: 11. The carbon monoxide reduction reactor according to claim 10, wherein each of the cooling layers has a flow path for flowing the cooling medium, and the flow path is from the inlet to the outlet. , Wherein the cross-sectional area is formed so as to increase gradually. 12. The reactor for reducing carbon monoxide according to claim 10, wherein said cooling layer has a plurality of cooling sections formed by dividing each of said cooling layers substantially equally. A cooling medium inflow control means for controlling the cooling medium inflow means so as to flow the cooling medium at a reduced flow rate from the cooling section on the introduction port side to the cooling section on the discharge port side. Reactor for reducing carbon monoxide. 13. The carbon monoxide reduction reactor according to claim 10, wherein the cooling layer is formed by dividing the cooling layer so as to increase in volume from the introduction side to the discharge side. Carbon monoxide, further comprising a cooling medium inflow control means for controlling the cooling medium inflow means so as to flow the cooling medium into each of the cooling parts at a substantially equal flow rate. Reduction reactor. 14. The carbon monoxide reduction reactor according to claim 9, wherein the length of each cooling layer from the inlet side to the outlet side is equal to the inlet of each catalyst carrier layer. Characterized in that the reactor is formed to be shorter than the length from the outlet to the outlet. 15. A catalyst having a plurality of inlets for introducing a gas to be treated containing carbon monoxide and an oxidizing agent, and a plurality of outlets for discharging a treatment gas reduced in carbon monoxide, and carrying a catalyst. A plurality of catalyst carrier layers having a plurality of catalyst carrier portions each having a carrier; a treatment gas introducing unit connected to the catalyst carrier layer, for introducing the gas to be treated into each of the catalyst carrier layers; A plurality of cooling layers arranged alternately with the respective catalyst supporting layers and through which a cooling medium can flow in and out, and cooling medium inflow means connected to the respective cooling layers and flowing the cooling medium into the respective cooling layers. A carbon monoxide reduction reactor, comprising: 16. The carbon monoxide reduction reactor according to claim 15, wherein each of the catalyst carriers has a flow path for flowing the gas to be processed and the processing gas, and the number of the flow paths Is gradually increased from the catalyst carrier on the inlet side to the catalyst carrier on the outlet side. 17. The carbon monoxide reduction reactor according to claim 15, wherein the amount of the catalyst supported on each of the catalyst carriers is from the catalyst carrier on the inlet side to the discharge port side. A carbon monoxide reduction reactor characterized by a gradual increase over the catalyst carrier. 18. The reactor for reducing carbon monoxide according to claim 15, wherein the catalyst carriers of the respective catalyst carriers carry different catalysts. Reactor for reducing carbon monoxide. 19. The carbon monoxide reduction reactor according to claim 9, wherein each of the catalyst carrier layers is formed of a metal. Reduction reactor. 20. The reactor for reducing carbon monoxide according to claim 9, wherein the catalyst is a noble metal. 21. A catalyst having a plurality of inlets for introducing a gas to be treated containing carbon monoxide and an oxidizing agent, and a plurality of outlets for discharging a treatment gas reduced in carbon monoxide, and carrying a catalyst. A plurality of catalyst support layers each including a plurality of catalyst support portions having a support, a processing gas introduction unit connected to the catalyst support layer, and introducing the processing gas into each of the catalyst support layers; An oxidizing agent introducing means for introducing the oxidizing agent between the respective catalyst supporting members, and a plurality of cooling layers which are arranged alternately with the respective catalyst supporting layers and through which a cooling medium can flow.
A cooling medium inflow means connected to the cooling layers and flowing the cooling medium into the cooling layers.