Fuel reforming apparatus for polymer electrolyte membrane fuel cell

[0001] [Technical field to which the invention belongs] The present invention relates to a fuel reformer for a polymer electrolyte fuel cell. [0002] [Conventional technology] As an example, the fuel reformer of a conventional polymer electrolyte fuel cell is composed of a reformer A, a carbon monoxide metamorphizer B, and a carbon monoxide selective oxidation reactor C, as shown in FIG. .. [0003] The reformer A is supplied with steam 6 obtained as follows. That is, the water 5 in the gas-liquid separator 26 is introduced into the evaporator (steam generator) 13, and the water / steam mixture 4 obtained by partially evaporating the water is introduced into the gas-liquid separator 26. , Here it separates into water 7 and steam 6. [0004] The reformer A mixes the steam 6 obtained as described above with the reforming fuel 8 made of, for example, natural gas, and introduces the reformer A into the reforming catalyst layer 14. While the fuel 8 passes through the reforming catalyst layer 14, the fuel 8 reacts with water vapor to generate hydrogen (H).₂) And carbon monoxide (CO), carbon dioxide (CO)₂) Is generated, so-called reforming reaction occurs. Since this reforming reaction is an endothermic reaction, hydrogen remaining in the combustion fuel (exhaust gas) of the fuel cell body (not shown) is burned in the combustor 10 attached to the reformer to generate heat in the combustion space container 9. Is generated, and this heat is transferred to the reforming catalyst layer 14 in the reformer to cause a reforming reaction. [0005] In the combustion space container 9, a center plug 11 for forming a radiant heat transfer unit 91 by high-temperature combustion gas and a convective heat transfer unit 92 by high- and medium-temperature combustion gas is installed. [0006] Further, in the fuel reformer of a polymer electrolyte fuel cell, carbon monoxide generated by the reforming reaction significantly deteriorates the performance of the fuel cell body even in a very small amount, and therefore needs to be removed. Therefore, in the fuel reformer of the conventional polymer electrolyte fuel cell, the carbon monoxide metamorphic catalyst layer 27 and, for example, the carbon monoxide metamorphic catalyst layer embedded cooler 28 composed of a spirally wound heat transfer tube are used. A carbon monoxide metabolizer B consisting of the above is installed downstream of the reformer A. In the carbon monoxide metamorphic catalyst layer 27, carbon monoxide reacts with water vapor to produce hydrogen and carbon dioxide. Since this reaction is an exothermic reaction, a cooler 28 for removing the heat is introduced in a form of being embedded in the catalyst layer 27. [0007] Further, since the fuel gas after leaving the reforming catalyst layer 14 has a high temperature, it is not suitable for the carbon monoxide transformation reaction as it is. Therefore, the carbon monoxide metamorphizer is placed before the carbon monoxide transformation catalyst layer 27. An inlet cooler (carbon monoxide reforming catalyst layer pre-cooler) 16 is installed. Carbon monoxide selection consisting of a carbon monoxide selective oxidation catalyst layer 29 and a carbon monoxide selective oxidation catalyst layer embedded cooler 30 in order to further remove the carbon monoxide remaining after the reaction in the carbon monoxide transformation catalyst layer 27. Oxidation reactor C is installed downstream of carbon monoxide metamorphizer B. [0008] Before entering the carbon monoxide selective oxidation catalyst layer 29, air 2 is mixed with the reformed fuel, and oxygen in the air and carbon monoxide selectively react in the carbon monoxide selective oxidation catalyst layer 29 to form carbon dioxide. It becomes carbon, and carbon monoxide is reduced to a concentration of 10 ppm or less. At this time, hydrogen also reacts with oxygen to produce water vapor, but if the amount of air and the temperature of the catalyst layer are adjusted to appropriate values, the reaction of hydrogen can be suppressed by the action of the catalyst. [0009] The carbon monoxide selective oxidation reaction is an exothermic reaction, and a cooler 30 is embedded in the catalyst layer 29 in order to remove the generated heat and keep the temperature at an appropriate value. Further, if the gas that has passed through the carbon monoxide metamorphic catalyst layer 27 is directly flowed to the carbon monoxide selective oxidation catalyst layer 29, it is not suitable for the carbon monoxide selective oxidation reaction. After the cooler 20 is attached and the temperature is lowered, it is supplied to the carbon monoxide selective oxidation catalyst layer 29. [0010] As a method for integrating such a system as a single device, for example, the first known example (Japanese Patent Laid-Open No. 7-126001), the second publicly known example (Japanese Square Root 7-133101), etc. A laminated structure is described. In these methods, for example, when methanol is used as a raw material, the reformer and carbon monoxide reactor are 200 to 300 ° C, the carbon monoxide selective reactor is 150 ° C, and the evaporator is 100 to 100 ° C. Only when the operating temperature of all equipment is low at 150 ° C and the temperature difference between each element is small, the equipment is sequentially laminated with a combustor, reformer / carbon monoxide metamorphic device, and carbon monoxide selective oxidation reactor. The heat recovery in the evaporator, the heat absorption reaction in the reformer, and the exothermic reaction between the carbon monoxide metamorphizer and the carbon monoxide selective oxidation reactor can be effectively utilized. It has been possible to provide a reforming apparatus having a function of steam reforming such as. [0011] [Problems to be Solved by the Invention] The main body part that produces electricity from the reaction of hydrogen and oxygen using a catalyst at low temperature, such as a polymer electrolyte fuel cell, can be made more compact than the main body part of other fuel cells, for example, phosphoric acid fuel cells. Since the operating temperature is low, it is expected to be applied to household power generators and vending machines. [0012] However, in the conventional polymer electrolyte fuel cell fuel reformer, as described above, the temperature level required for each reactor is different. The equipment was large because the carbon oxide metaphor, the carbon monoxide selective oxidation reactor inlet cooler, and the carbon monoxide selective oxidation reactor were installed separately and connected by pipes. [0013] In addition, the carbon monoxide selective oxidation reactor is a reactor peculiar to the fuel reformer of a fuel cell that operates at a low temperature, which is not necessary for the fuel reformer of other fuel cells, and is a carbon monoxide selective oxidation reaction. It was difficult to make the fuel reformer of the polymer electrolyte fuel cell smaller because of the need for the reactor and its cooling device. [0014] Therefore, making the fuel reformer smaller is one of the important issues that must be solved in order to put the polymer electrolyte fuel cell into practical use. In addition, the compactness should not reduce the system efficiency of the polymer electrolyte fuel cell system and require a large amount of fuel for the same amount of power generation. [0015] It is assumed that a liquid fuel such as methanol is used as a raw material in the composite integrated fuel cell reformer having a laminated structure described in the first known example and the second known example described above. Therefore, the reformer and carbon monoxide reactor are 200 to 300 ° C, the carbon monoxide selective reactor is 150 ° C, and the evaporator is 100 to 150 ° C, and the operating temperature is low and the temperature difference between each element is low. There are few. Therefore, it is possible to fulfill the function as a reformer even if the laminated structure is made compact. [0016] On the other hand, when steam reforming raw materials such as methane and propane, the operating temperature of the reactor is 700 to 750 ° C for the reformer, 200 to 300 ° C for the carbon monoxide modifier, and selective oxidation of carbon monoxide. The reactor is at 150 ° C, and not only is the operating temperature of the reformer high, but the temperature difference between each element is large. Therefore, in the laminated structure described in the first known example, the second known example, etc., when methane or propane is applied, the reformer is changed to the carbon monoxide metamorphic device or the carbon monoxide selective oxidation reactor. There was a risk that it would be difficult to keep the carbon monoxide reformer and the carbon monoxide selective oxidation reactor at an appropriate temperature due to the large amount of heat transfer. [0017] In the laminated structure, in order to suppress this heat transfer, it is necessary to provide a heat insulating layer between the reformer and the carbon monoxide metaphor or the carbon monoxide selective oxidation reactor, or to provide a means for cooling. is there. In this case, the former hinders compactification, the latter also hinders compactification, and depending on the method, system efficiency is impaired. [0018] Further, in the reformer according to the above-mentioned known example, since the side surface of each reactor comes into contact with the outside air, a heat insulating layer is required to suppress heat dissipation. However, in order to suppress the heat radiation from the reforming reactor whose operating temperature is 700 to 750 ° C to the same level as other reactors, it requires several times more heat insulating layer than other reactors, and it is compact. Inhibits. Moreover, since these heat dissipation is not recovered by heat, it is difficult to improve the thermal efficiency. Since heat dissipation increases as the temperature of the reactor increases, the decrease in thermal efficiency may become more remarkable, especially when the reforming reaction is heated to a high temperature by applying methane or propane. Therefore, the reformer with the highest operating temperature burns hydrogen and methane contained in the fuel cell exhaust gas with a burner to supply heat, and the residual heat of the burner exhaust gas evaporates the water, while the gas on the reformer process side is modified. A cooler is installed in this order to lower the operating temperature of the pawnbroker, carbon monoxide metamorphic device, and carbon monoxide selective oxidation reactor, and the cooler effectively recovers heat and also collects heat from the reactor. Therefore, a technology that can improve the efficiency of the system and make it compact is required. [0019] The present invention has been made to solve such a problem, and an object of the present invention is to provide a fuel reformer for a compact polymer electrolyte fuel cell, regardless of the raw material and fuel, without increasing the required fuel. And. [0020] [Means for solving problems] In order to achieve the above object, the invention according to claim 1 uses carbon monoxide obtained by a reforming reaction obtained by passing a mixed fuel in which a reforming fuel and steam are mixed through a reforming catalyst layer. A reformer in which the reforming gas contained can be taken out and at least a part of the outer peripheral surface is formed on an arc surface. A carbon monoxide metamorphizer is provided which is arranged concentricly on the outer peripheral surface of the reformer having an arc surface, takes in carbon monoxide from the reformer, and lowers the concentration of carbon monoxide by a water gas shift reaction. And The carbon monoxide modifier includes a carbon monoxide transformation catalyst layer inlet cooler, a first stage carbon monoxide transformation catalyst layer, a carbon monoxide transformation catalyst layer intermediate cooler, and a second stage carbon monoxide transformation. It consists of a catalyst layer, all of which are formed in a concentric cylindrical shape, and the reforming gas is released from the reformer.<u style="single">The carbon monoxide metamorphic catalyst layer inlet cooler and</u>The first stage carbon monoxide metamorphic catalyst layer, the carbon monoxide metamorphic catalyst layer intermediate cooler, and the second stage carbon monoxide metamorphic catalyst layer are arranged so as to flow in this order. It is a fuel reformer for polymer electrolyte fuel cells. [0021] [0021] According to the invention corresponding to claim 1, the temperature gradient between each device is leveled by gradually arranging the devices having a low temperature level around the device having a high temperature level, and each device. Less heat transfer between. For this reason, even if each device is installed independently and kept warm by a heat insulating material and these devices are not connected by piping, the devices can be integrated and made compact, and the operating temperature of each reactor can be increased. Can be kept properly. Moreover, the heat transferred from the inner high-temperature reactor to the outside is used to maintain the temperature of the outer reactor, so that the thermal efficiency can be improved. [0022] Further, according to the invention according to claim 1, the temperature gradient between the devices is leveled, and the heat transfer between the devices is reduced. Therefore, even if each device is installed independently and the heat insulating material is used to keep the device warm and the devices are not connected by piping, the devices can be integrated and made compact. [0023] In order to achieve the above object, the invention according to claim 2 is arranged concentrically on the outer peripheral surface of the carbon monoxide metamorphic device, and the carbon monoxide metamorphic device reduces the concentration of carbon monoxide to a low concentration. A carbon monoxide selective oxidation reactor that lowers the concentration of carbon monoxide by taking in the reformed gas, mixing air, oxygen, or combustion gas into the reformed gas and causing an oxidation reaction. A claim characterized in that<u style="single">1</u>The fuel reformer for the polymer electrolyte fuel cell described. [0024] According to the invention according to claim 2, the reformer at a high temperature level and the other reactor at a relatively low temperature can be thermally separated. Further, by making the reformer cylindrical, the heat generated by the combustor in the reformer is effectively transferred to the reforming catalyst layer. Furthermore, since the carbon monoxide modifier, carbon monoxide selective oxidation reactor, carbon monoxide modifier inlet cooler, and carbon monoxide selective oxidation reactor inlet cooler can be combined in a rectangular shape, the polymer electrolyte fuel can be integrated. The fuel reformer of the battery can be made compact. [0025] In order to achieve the above object, in the invention corresponding to claim 3, the carbon monoxide selective oxidation reactor includes a carbon monoxide selective oxidation catalyst layer inlet cooler, a carbon monoxide selective oxidation catalyst layer, and carbon monoxide. It consists of a selective oxidation catalyst layer outlet cooler, all of which are formed in a concentric cylindrical shape, and the reforming gas from the carbon monoxide metamorphic device is the carbon monoxide selective oxidation catalyst layer inlet cooler and the above-mentioned one. The claim is characterized in that the carbon monoxide selective oxidation catalyst layer and the carbon monoxide selective oxidation catalyst layer outlet cooler are arranged so as to flow in this order.<u style="single">2</u>The fuel reformer for the polymer electrolyte fuel cell described. [0026] According to the invention according to claim 3, since the steam generator is also integrated, the fuel reformer can be further made compact. [0027] In order to achieve the above object, in the invention corresponding to claim 4, the carbon monoxide selective oxidation catalyst includes a carbon monoxide selective oxidation catalyst layer inlet cooler and a first stage carbon monoxide selective oxidation catalyst layer. , Carbon monoxide selective oxidation catalyst layer intermediate cooler, second stage carbon monoxide selective oxidation reaction catalyst layer, and carbon monoxide selective oxidation catalyst layer outlet cooler, all of which are formed in a cylindrical shape. The reforming gas from the carbon monoxide modifier is intermediate between the carbon monoxide selective oxidation catalyst layer inlet cooler, the first stage carbon monoxide selective oxidation catalyst layer, and the carbon monoxide selective oxidation catalyst layer. The claim is characterized in that the cooler, the second-stage carbon monoxide selective oxidation catalyst layer, and the carbon monoxide selective oxidation catalyst layer outlet cooler are arranged so as to flow in this order.<u style="single">2</u>The fuel reformer for the polymer electrolyte fuel cell described. [0028] According to the invention according to claim 4, the steam generator and each reactor can be integrated without interfering with the heat transfer between the combustion gas and the catalyst layer in the reformer, so that the fuel consumption amount. The fuel reformer can be made compact without causing an increase in the amount of fuel. [0029] In order to achieve the above object, the invention according to claim 5 is an intermediate surface between the outer peripheral surface of the carbon monoxide transformation catalyst layer inlet cooler, the carbon monoxide transformation catalyst layer of the first stage, and the carbon monoxide transformation catalyst layer. Between the cooler and the inner peripheral surface of the second stage carbon monoxide metamorphic catalyst layer, or between the outer peripheral surface of the carbon monoxide metamorphic catalyst layer inlet cooler and the first stage carbon monoxide metamorphic catalyst layer and the above. The claim is characterized in that a heat insulating layer is formed between the carbon monoxide metamorphic catalyst layer intermediate cooler and the inner peripheral surface of the second stage carbon monoxide metamorphic catalyst layer.<u style="single">1~4</u>The fuel reformer for the polymer electrolyte fuel cell according to any one of. [0030] According to the invention according to claim 5, the temperature distribution in the carbon monoxide selective oxidation catalyst layer can be made uniform, and the fuel reformer can be made compact. [0031] BEST MODE FOR CARRYING OUT THE INVENTION Hereinafter, embodiments of the present invention will be described. [0032] FIG. 1 is for explaining a first embodiment of a fuel reformer for a polymer electrolyte fuel cell, and illustrates a vertical cross section of the cylindrical device. The fuel reformer of the polymer electrolyte fuel cell shown in FIG. 1 is a general reformer A, a carbon monoxide modifier B, a carbon monoxide selective oxidation reactor C, a carbon monoxide modifier inlet cooler 16, 1 It is composed of 20 carbon monoxide selective oxidation reactor inlet coolers. [0033] In the reformer A, the openings at both ends of the cylindrical body 9a are closed by the lid member 9b and the bottom surface member 9c, and the combustion space container 9 for forming the radiation heat transfer portion 91 and the convection heat transfer portion 92 inside, and the cylinder. A cylindrical partition wall 37 arranged and fixed between the outer peripheral surface of the body 9a and the lid member 9b and the bottom member 9c, and the bottom member 9c on the outer peripheral side of the partition wall 37 with a predetermined distance from the partition wall 37. A cylindrical partition wall 38 arranged and fixed to the partition wall 38, a cylindrical modification catalyst layer 14 arranged between the inner peripheral surface of the partition wall 38 and the outer peripheral surface of the partition wall 37, and the lower position of the modification catalyst layer 14 and the lower position of the modification catalyst layer 14. The partition walls 39 and 40, which are arranged at the upper part and are arranged and fixed at predetermined positions of the partition wall 38 and the partition wall 37, respectively, and a part of the lower end side of the reforming catalyst layer 14 are formed, for example, for reforming made of natural gas. A gas inlet 41 that guides the fuel 8 and the reforming steam 6 into the reforming catalyst layer 14, above the partition wall 40, the outer periphery of the reforming catalyst layer 14 and the partition wall 38, and above the reforming catalyst layer 14 (gas introduction). It is the side opposite to the part where the mouth 41 is formed), is fixed to the lid member 9b, is cylindrical for forming the regeneration flow path (regeneration chamber) 15, and extends inward to the opening on the one end side. It is composed of a cylindrical flow path forming member 32 having a flange. [0034] It is arranged so as to form a gap (heat insulating layer) 25 on the outer peripheral side of the flow path forming member 32, has a flange extending to the outer peripheral side at one end opening of the cylindrical body, and is joined to the lower end of the flow path forming member 32. The partition wall 33 is arranged below the inner peripheral surface of the partition wall 33, and the carbon monoxide metamorphic inlet cooler 16 composed of, for example, a spirally wound heat transfer tube, and the partition wall 33 The bottom member is arranged on the outer peripheral surfaces of the first-stage carbon monoxide-modified catalyst layer 17 arranged on the upper side of the inner peripheral surface, the carbon monoxide-modified catalyst layer 17, and the carbon monoxide-modified inlet cooler 16. It is composed of a cylindrical partition wall 34 having one end fixed to a bottom member 42 joined to 9c, and a heat transfer tube arranged above the outer peripheral surface of the partition wall 34 and wound in a spiral shape, for example. Carbon oxide metamorphic catalyst layer Intermediate cooler 18 and the cylindrical second stage carbon monoxide metamorphic catalyst layer 19 arranged below the outer peripheral surface of the partition wall 34, the cooler 18 and the carbon monoxide metamorphic catalyst layer. A cylindrical partition wall 35 arranged on the outer peripheral surface of 19 and having one end fixed to the flange of the partition wall 33, and a cylindrical carbon monoxide selective oxidation catalyst layer on the outer peripheral surface of the partition wall 35 from the lower side to the upper side. Inlet cooler (carbon monoxide selective oxidation catalyst layer pre-cooler) 20, cylindrical first stage carbon monoxide selective oxidation catalyst layer 21 and cylindrical carbon monoxide selective oxidation catalyst layer intermediate cooler 22 A cylindrical second-stage carbon monoxide selective oxidation catalyst layer 23, a cylindrical carbon monoxide selective oxidation catalyst layer outlet cooler (carbon monoxide selective oxidation catalyst layer post-cooler) 24, and a cooler. 20 and carbon monoxide selective oxidation catalyst layer 21 and carbon monoxide selective oxidation catalyst layer Intermediate cooler 22 and carbon monoxide selective oxidation catalyst layer 23 and cooler 24 are arranged on the outer peripheral surface, and both ends are flanges of partition 33. It is composed of a cylindrical partition wall 36 fixed to the bottom member 42 and the bottom member 42, respectively. Air headers 621 and 622 are arranged on the outer peripheral surface of the partition wall 36 as described below. [0035] The coolers 20, 22, and 24 are all composed of, for example, a spirally wound heat transfer tube. [0036] In this case, the carbon monoxide transformer B is composed of a carbon monoxide transformation catalyst layer 17, a carbon monoxide transformation catalyst layer 19, and partition walls 33, 34, 35. Further, the carbon monoxide selective oxidation reactor C is composed of carbon monoxide selective oxidation catalyst layers 21, 23 and an air header 621, 622, as will be described later. [0037] A center plug 11 having a U-shaped cross section is arranged in the combustion space container 9, and a cylindrical partition wall 12 and an evaporator (steam generator) 13 are arranged in the lower space of the center plug 11. A combustor 10 is arranged on the lid member 9b at the upper part of the combustion space container 9, and the combustor 10 supplies air 2 to the combustion fuel 1 of the fuel cell body to emit the combustion gas obtained by burning the combustion fuel 1. It is designed to be supplied to the radiant heat transfer unit 91. [0038] Further, the reforming steam 6 separated by the gas-liquid separator 26 is supplied to the inlet 41 of the reforming refrigerant layer 14 together with the reforming fuel 8, and the gas-liquid separator 26 is supplied from the evaporator 13. Water 4 is to be supplied. [0039] Hereinafter, the operation of the first embodiment configured in this way will be described. Combustion fuel 1 of the fuel cell body (not shown) is introduced into the combustor 10 and burned in the combustion space container 9 to generate high temperature heat of 1000 ° C. or higher. The combustion gas transfers heat to the reforming catalyst layer 14, and the combustion gas itself is discharged in a state where the temperature is lowered, and after being used as a heat source of the evaporator 13, it is exhausted as the post-combustion exhaust gas 3. [0040] At this time, since the center plug 11 is installed in the combustion space container 9, heat transfer to the reformer A is effectively performed by radiant heat transfer and convective heat transfer. [0041] On the other hand, the reforming fuel 8 such as natural gas is mixed with the water vapor 6 generated in the gas-liquid separator 26 and then distributed to the reforming catalyst layer 14 in a state of substantially atmospheric pressure. In the reforming catalyst layer 14, the reforming reaction occurs by receiving the heat of the combustion gas described above, and the fuel reacts almost 100% to generate hydrogen, carbon monoxide, and carbon dioxide. Since the reformed gas containing these components and the steam that was not used in the reaction has a high temperature, it exchanges heat with the reformed catalyst layer 14 while passing through the regeneration flow path 15, and the exhaust heat is recovered. [0042] Immediately after passing through the regeneration channel 15, the reformed gas is still at a high temperature of about 400 ° C to 500 ° C, so that it is around the cooler 16 before entering the carbon monoxide metamorphic catalyst layer 17 of the first stage. It passes through and is cooled to 200 ° C to 300 ° C. The reformed gas that has been cooled and lowered in temperature is circulated to the carbon monoxide metamorphic catalyst layer 17, and the carbon monoxide generated in the reforming catalyst layer 14 reacts with steam to generate carbon dioxide and hydrogen. So-called shift reaction occurs. Since this reaction is an exothermic reaction, the temperature of the reformed gas rises while passing through the catalyst layer, and when it leaves the carbon monoxide metamorphic catalyst layer 17, the reaction reaches an almost equilibrium state. [0043] The reformed gas that has passed through the carbon monoxide metamorphic catalyst layer 17 in the first stage is cooled while passing around the cooler 18, the temperature drops, and the state suitable for the shift reaction is restored. Since the equilibrium concentration of the cooled reformed gas decreases as the temperature decreases, the shift reaction proceeds again while the second stage carbon monoxide transformation catalyst 19 is flowing, and the temperature rises while the carbon monoxide is carbon monoxide. The concentration decreases to about 5000 ppm. After that, a small amount of air was mixed into the reformed gas from the air introduction header 62 through the pores 64, and then passed around the cooler 20 to lower the temperature, and then carbon monoxide selective oxidation in the first stage. It flows into the catalyst layer 21. [0044] While passing through the carbon monoxide selective oxidation catalyst layer 21, carbon monoxide in the reformed gas reacts with oxygen in the air to become carbon dioxide. This reaction has a large calorific value, and the temperature of the reformed gas rises rapidly. Then, after being cooled by the cooler 22, a small amount of air is mixed in again from the air introduction header 622, and then the selective oxidation reaction proceeds again while the second stage carbon monoxide selective oxidation catalyst 23 is flowing, and the temperature is increased. While rising, the carbon monoxide concentration becomes 10ppm or less. After that, the reformed gas is cooled by the cooler 24 and supplied to the fuel cell body (not shown). [0045] According to the first embodiment described above, the reformed catalyst layer 14, the regeneration flow path 15, the heat insulating layer 25, the carbon monoxide metamorphic catalyst layers 17 and 19, and the carbon monoxide selective oxidation are centered on the combustion space container 9. When the catalyst layers 21 and 23 are arranged outward in this order, the one with the higher temperature is in the center, and the temperature gradually decreases toward the periphery. Since the temperature difference is minimized, the heat leak between the elements is minimized, and even if the elements are installed adjacent to each other, the temperature level at which the reaction efficiency in each catalyst layer is maximized can be secured, and the fuel is reformed. The function can be retained. As a result, the fuel reformer can be integrated and made compact. [0046] In addition, with such a configuration, the carbon monoxide selective oxidation reactor (carbon monoxide selective oxidation catalyst layers 21, 23, air headers 621, 622) C, which is the lowest temperature element, is installed on the outermost side. Therefore, the heat loss can be minimized, and therefore the power generation efficiency of the polymer electrolyte fuel cell can be improved. [0047] Further, as shown in FIG. 1, an evaporator (steam generator) 13 composed of, for example, a spiral heat transfer tube can be installed in a part of the center plug 11 in the combustion space container 9 cut out. .. In this case, since the evaporator 13 is also integrated, the entire apparatus can be made more compact. [0048] Further, as shown in FIG. 1, a space is formed in the lower part of the center plug 11 in the combustion space container 9, and a cylindrical partition wall 12 is installed in this space, and between the outer peripheral surface of the partition wall 12 and the center plug 11. If the evaporator 13 is installed as shown in the figure, the reforming performance is maintained without hindering the heat transfer to the reformer A. Therefore, the entire apparatus is made compact and the polymer electrolyte fuel cell is used. Power generation efficiency can be increased. [0049] Further, as shown in FIG. 1, the conventional carbon monoxide metamorphic catalyst layer is divided into the first stage and the second stage carbon monoxide metamorphic catalyst layers 17 and 19 and the cooler 18 is arranged in the middle thereof. As described above, it is not necessary to bury the heat transfer tube in the catalyst layer, and the width of the catalyst layer can be narrowed, so that the fuel reformer of the polymer electrolyte fuel cell can be made smaller. At this time, it goes without saying that the same effect can be obtained even if the catalyst layer is further subdivided and a cooler is provided in the middle of each. [0050] Further, as shown in FIG. 1, the conventional carbon monoxide selective oxidation catalyst is divided into the first stage and the second stage carbon monoxide selective oxidation catalysts 21 and 23, and the cooler 22 is arranged in the middle thereof. Compared to the case where the heat transfer tube is embedded in the catalyst layer for cooling, the part that becomes locally hot in the catalyst layer is reduced, so that the amount of catalyst is the minimum necessary and the entire device is made compact. be able to. At this time, it goes without saying that if the catalyst layer is further subdivided and a cooler is provided in the middle of each, the number of local high temperature portions is further reduced. [0051] Further, as shown in FIG. 1, by arranging the cooler 24 downstream of the carbon monoxide selective oxidation catalyst layer 23, the catalyst is compared with the case where the heat transfer tube is embedded in the catalyst layer for cooling as in the conventional case. Since the portion of the layer that becomes locally hot is reduced, the amount of catalyst can be minimized, and the entire apparatus can be made compact. [0052] Further, as shown in FIG. 1, since a gap (insulation layer) 25 is formed between the reformer C and the carbon monoxide metamorphizer B, the reformer usually has a high temperature of 500 ° C to 1000 ° C. Even if the vessel part and another carbon monoxide modifier B or carbon monoxide selective oxidation reactor C with a temperature of about 100 ° C to 300 ° C are installed adjacent to each other, they can be thermally separated. There is no load increase on the coolers 16, 18, 20, 22, and 24 due to heat leakage, and the cooler can be made smaller. Furthermore, it is possible to absorb the elongation difference due to the thermal expansion of the partition wall that occurs between the high temperature level reformer and the low temperature level carbon monoxide metamorphic device B, and it is possible to reduce the thermal stress, so that the structure and strength can be improved. Since the problem of can be solved, the fuel reformer can be made smaller. [0053] Further, in the embodiment shown in FIG. 1, a mixture of reforming fuel 8 and reforming steam 6 can be circulated inside the cooler 16 upstream of the carbon monoxide metamorphic catalyst layer 17 in the first stage. .. With such a configuration, the reformed gas can be cooled and heat can be recovered, so that the system efficiency of the fuel cell system can be improved. Further, in the embodiment shown in FIG. 1, a gas-liquid mixture after leaving the evaporator 13 can be circulated inside the cooler 18 installed in the middle of the carbon monoxide metamorphic catalyst layer, for example. With such a configuration, the reformed gas can be cooled and heat can be recovered, so that the system efficiency of the fuel cell system can be improved. [0054] Further, in the embodiment shown in FIG. 1, the coolers 20, 22, and 24 of the carbon monoxide selective oxidation catalyst layer can be integrally formed by one heat transfer tube, and the inside thereof is, for example, the cooling of the battery body. Part of the water can also be used. With such a configuration, heat can be recovered at the same time as cooling without preparing a new cooling medium, so that the power generation efficiency of the fuel cell system can be improved. [0055] FIG. 2 is a schematic view showing a horizontal cross section of only the air introduction header portion 62 into the carbon monoxide selective oxidation reactor C in the fuel reformer of the polymer electrolyte fuel cell of FIG. 1, and is the second stage in the figure. The portion inside the flow path containing the carbon monoxide reforming catalyst layer 19 is omitted. Air 2 is introduced from one place into the air introduction header 62 by the air introduction pipe 68. The inner wall (partition wall) 63 of the air header between the air header 62 and the annular flow path 65 including the carbon monoxide selective oxidation catalyst layer is configured to have at least eight pores 64. [0056] The air introduced into the air passage header 62 from the air introduction pipe 68 which is fixed through a part of the air header outer wall 61 enters the annular flow path 65 from the air header 62 through the pore 64 and enters the second stage. It is mixed with the reformed gas that has passed through the carbon monoxide metamorphic catalyst layer. After being mixed, the air diffuses in the reformed gas and flows into the carbon monoxide selective oxidation catalyst layer 21 of the first stage while passing through the outer circumference of the cooler 20 of FIG. [0057] At this time, if the number of pores 64 is small, the diffusion of air in the reformed gas does not proceed, and an uneven distribution of air is formed, so that the reaction with the carbon monoxide selective oxidation catalyst is one in the catalyst layer. There is a possibility that the carbon monoxide concentration does not drop below the specified amount as a whole. [0058] [0058] Therefore, it is necessary to sufficiently diffuse the air into the reformed gas, and for that purpose, there is also a method of increasing the distance from the air introduction pipe 68 to the carbon monoxide selective oxidation catalyst. However, this method makes the device large. [0059] However, according to the configuration of the embodiment of the present invention, air can be sufficiently diffused into the reformed gas even if the diffusion distance is short. Figure 3 is an example of the analysis results showing the reason. FIG. 3 shows the results of calculating the state of oxygen diffusion in the air by changing the number of pores 64 in the embodiment of FIG. In FIG. 3, the horizontal axis represents the angle indicating the position in the annular flow path, and the vertical axis represents the oxygen concentration at the inlet of the carbon monoxide selective oxidation catalyst layer 22. FIG. 3A shows the case where the pore 64 is set to one place, FIG. 3B shows the case where the pore 64 is set to two places, FIG. 3C shows the case where the pore 64 is set to four places, and FIG. 3D shows the case where the pore 64 is set to eight places. If this is the case. As is clear from the figure, it is possible to diffuse almost uniformly by opening eight pores 64. [0060] Therefore, according to the configuration of the present embodiment, even if the mixing distance between the air and the reformed gas is short, the air diffuses uniformly into the reformed gas, so that the fuel reformer of the polymer electrolyte fuel cell can be used. It can be made compact. [0061] The method of introducing air into the carbon monoxide selective oxidation catalyst layer 21 in the first stage has been described above, but the method of introducing air into the carbon monoxide selective oxidation catalyst layer 23 in the second stage is exactly the same as in the case of the first stage. is there. [0062] FIG. 4 is a vertical schematic cross-sectional view for explaining a second embodiment of the fuel reformer for the polymer electrolyte fuel cell of the present invention. This is a cylindrical carbon monoxide metamorphic inlet that is concentrically arranged close to the outer peripheral surface of the cylindrical body 9a having the arc surface of the reformer and takes in and cools carbon monoxide from the reformer. Cooler 16 and It is arranged at a substantially central position on the outer peripheral surface of the cooler 16, respectively, at a position above and below the cylindrical carbon monoxide selective oxidation catalyst layer intermediate cooler 18 except for the substantially central position on the outer peripheral surface of the cooler 16. It is provided with cylindrical first-stage and second-stage carbon monoxide metamorphic catalyst layers 17, 19. [0063] Further, close to the carbon monoxide metamorphic catalyst layer 19, the carbon monoxide selective oxidation catalyst layer pre-cooler, the first stage carbon monoxide selective oxidation catalyst layer 21, the carbon monoxide selective oxidation catalyst layer intermediate cooler 22, The second stage carbon monoxide selective oxidation catalyst layer 23 and the carbon monoxide selective oxidation catalyst layer post-cooler 24 are sequentially arranged. [0064] In the configuration as shown in FIG. 4, the reforming fuel 8 is supplied together with the reforming steam 6 to the reforming catalyst layer 14 having a concentric cylindrical shape, and a hydrogen-rich reforming gas is supplied from hydrocarbons. A reforming reaction occurs. Taking the case where the reforming fuel is methane as an example, CH₄+ H₂O 3H₂+ CO The reforming reaction is an endothermic reaction, and heat must be supplied in order to proceed the reaction and maintain the reaction temperature. Therefore, the combustion space container 9 is arranged inside the reforming catalyst layer. [0065] The combustion fuel 1 is sent to the combustor 10 together with the air 2 and is burned in the combustion space container 9 to become a high-temperature combustion gas. As the combustion fuel 1, in addition to a substance having the same composition as the reforming fuel, a flammable gas that has not been consumed in the reaction in the fuel cell can also be used. [0066] The combustion gas exchanges heat with the reforming catalyst layer 14 through the partition wall while passing through the radiant heat transfer section 91 and the convective heat transfer section 92 to supplement the heat required for the reforming reaction. [0067] The combustion gas after passing through the convective heat transfer section 92 maintains a high temperature of several hundred ° C. Therefore, the evaporator 13 may be installed below the radiant heat transfer unit 91 and inside the convection heat transfer unit 92, and heat recovery may be performed here. [0068] To exemplify the flow of combustion gas in FIG. 4, the combustion gas flowing downward through the convective heat transfer section 92 is inverted and flows upward, and heat exchanges with water or a water / steam mixture in the evaporator 13. After heat exchange, it reverses further and flows downward to the outside of the composite reactor. [0069] In such a configuration, a center plug 11 is arranged between the radiant heat transfer section 91, the convection heat transfer section 92, and the evaporator 13 to dissipate heat from the combustion gas during heat exchange with the reforming catalyst layer. It is desirable to dissipate heat from the hot combustion gas before heat exchange in the evaporator 13 to the cold combustion gas after heat exchange by arranging the partition wall 12 and stopping the heat exchange. [0070] On the other hand, the reforming gas that has passed through the reforming catalyst layer 14 enters the regeneration flow path 15. In the example of FIG. 4, the reformed gas that has passed through the reformed catalyst layer 14 from the bottom to the top reverses and enters the regeneration channel 15 and descends. In the configuration illustrated in FIG. 4, the temperature at the outlet of the reforming catalyst layer 14 is higher than that at the inlet and the middle because the combustion reaction occurs at the upper part. [0071] Therefore, heat can be recovered to the reformed catalyst layer by passing the high-temperature gas emitted from the outlet of the reformed catalyst layer through the regeneration flow path 15 adjacent to the reformed catalyst layer 14. The reformed gas after heat recovery is inverted upward in the example shown in FIG. Heat is exchanged by the carbon monoxide metamorphic catalyst layer inlet cooler 16. Examples of the refrigerant of the carbon monoxide transformation catalyst layer inlet cooler 16 include the reforming fuel 8 and the reforming steam 6 before being introduced into the reforming catalyst layer 14. As described above, the carbon monoxide transformation catalyst Thermal efficiency can be increased by using the layer inlet cooler 16 as a preheater for the reforming fuel 8. [0072] Among the devices described above, it is desirable that the combustion space container 9 is arranged inside the reforming catalyst layer 14 and the regeneration flow path 15 is arranged outside the reforming catalyst layer 15 due to the necessity of heat exchange. In addition, the combustion space container 9 is preferably cylindrical because the uniform distance from the flame existing inside to the wall surface of the container contributes to the uniformity of heat conduction, and the reforming catalyst layer 14 and the regeneration flow path 15 are It is desirable to form an annulus around it and integrate it. Moreover, although the evaporator 13 can be installed outside, it is more preferable to install the evaporator 13 inside the combustion space container 9 because the occupied space can be reduced. Further, when the carbon monoxide metamorphic catalyst layer inlet cooler 16 is used as a preheater for the reforming fuel 8, it is desirable that the carbon monoxide metamorphic catalyst layer inlet cooler 16 is installed as close to the reforming catalyst layer 14 as possible. It is desirable to arrange them in an annulus shape on the outside of the regeneration flow path 15 as illustrated in. However, the reformed gas passing through the regeneration channel 15 has a higher temperature than the carbon monoxide metamorphic catalyst layer inlet cooler 16, and if it is adjacent to the reformed gas, the high-quality heat to be recovered in the reformed catalyst layer 14 is monoxide. Since it may be transmitted to the carbon reforming catalyst layer inlet cooler 16 and reduce the thermal efficiency, it is necessary to provide a heat insulating layer 25 in between to insulate. [0073] The reformed gas cooled by the carbon monoxide transformation catalyst layer inlet cooler 16 enters the carbon monoxide transformation catalyst layer 17 of the first stage, and the CO concentration of about 10% is reduced to several% by the following carbon monoxide transformation reaction. Reduce to a degree. [0074] CO + H₂ CO₂+ H₂The higher the temperature, the faster the reaction rate, and the reaction can occur with a smaller amount of catalyst. However, since this reaction is an equilibrium reaction of exotherm, there is a lower limit to the CO concentration, and the higher the temperature, the higher the lower limit CO concentration. When carbon monoxide metamorphism occurs, H₂However, it is desirable that the CO concentration is low in order to increase the efficiency, but the high temperature first stage carbon monoxide metamorphic catalyst layer 17 alone cannot sufficiently reduce the CO concentration. [0075] Therefore, a carbon monoxide transformation catalyst layer intercooler 18 is arranged further downstream to lower the temperature, and the CO concentration in the second stage carbon monoxide transformation catalyst layer 19 is reduced to the level of several thousand ppm. Although the reaction rate is slow due to the low temperature, the reaction amount is small because it is reduced to about several percent in the first stage, and it is significantly compared to the case where the carbon monoxide transformation reaction occurs only under the temperature conditions of the second stage. The reaction can be completed with a small amount of catalyst. [0076] The carbon monoxide transformation catalyst layer 17 in the first stage, the carbon monoxide transformation catalyst layer intermediate cooler 18 in the first stage, and the carbon monoxide transformation catalyst layer 19 in the second stage are configured in an annular shape in order to make the equipment compact. It is preferable that the carbon oxide metamorphic catalyst layer inlet cooler 16 is further configured in an annular shape on the outer periphery. [0077] The CO concentration at the outlet of the carbon monoxide metamorphic catalyst layer 19 in the second stage is Although it is at the level of several thousand ppm, the CO level must be at the level of several to several tens of ppm in order to supply it to a polymer electrolyte fuel cell that operates at low temperatures. As a means for achieving this purpose, a method is known in which a small amount of oxygen or air is mixed with the reformed gas and the CO is oxidized by passing through a carbon monoxide selective oxidation catalyst. [0078] CO + 1 / 2O₂ CO₂However, the higher the temperature of the catalyst layer, the more as a side reaction. H₂+ 1 / 2O₂ H₂O Reaction occurs, H2 that should be used in the fuel cell is consumed, which is disadvantageous in terms of efficiency. Therefore, the reformed gas mixed with oxygen or air needs to be introduced into the carbon monoxide selective oxidation catalyst in a state of being cooled to an appropriate temperature. [0079] In the example of FIG. 4, the reformed gas at 200 ° C or higher at the outlet of the carbon monoxide metamorphic catalyst layer 19 in the second stage is brought to an optimum temperature of 100 to 150 ° C at the carbon monoxide selective oxidation catalyst layer inlet cooler 20. It is cooled. Oxygen or air may be mixed on either the inlet side or the outlet side of the carbon monoxide selective oxidation catalyst layer inlet cooler 20, but the one mixed on the inlet side is inside the carbon monoxide selective oxidation catalyst layer inlet cooler 20. It is more desirable because it can be expected to have a stirring effect. The reformed gas cooled to an appropriate temperature has a CO concentration reduced to a level of several to several hundred ppm by an oxidation reaction by O2 in the carbon monoxide selective oxidation catalyst layer 21 of the first stage. After that, it is cooled to an appropriate temperature of 100 to 150 ° C again by the carbon monoxide selective oxidation catalyst layer intercooler 22, and then sent to the second stage carbon monoxide selective oxidation catalyst layer 23 together with oxygen or air, and O₂The CO concentration is reduced to the level of several to several tens of ppm by the oxidation reaction. Oxygen or air may be mixed on either the inlet side or the outlet side of the carbon monoxide selective oxidation catalyst layer intercooler 23, but the one mixed on the inlet side is inside the carbon monoxide selective oxidation catalyst layer intercooler 23. It is more desirable because it can be expected to have a stirring effect. Since the gas after the selective oxidation reaction has a high temperature of 100 to 250 ° C due to the oxidation reaction, the operating temperature of the polymer electrolyte fuel cell is about 50 to 90 ° in the carbon monoxide selective oxidation catalyst layer outlet cooler 24. The temperature is lowered to about C to prevent the temperature balance in the polymer electrolyte fuel cell from being lost. [0080] [0080] FIG. 5 is a vertical schematic cross-sectional view for explaining a third embodiment of the fuel reformer for the polymer electrolyte fuel cell of the present invention. [0081] In this embodiment, as compared with FIG. 4, the outside of the carbon monoxide metamorphic catalyst layer inlet cooler 16, the first stage carbon monoxide metamorphic catalyst layer 17, the carbon monoxide metamorphic catalyst layer intermediate cooler 18 and the first stage A heat insulating layer 47 composed of gaps is provided inside the carbon monoxide metamorphic catalyst layer 19 to prevent heat leakage from the inside at a high temperature to the outside at a low temperature. [0082] In particular, the inlet portion of the carbon monoxide metamorphic catalyst layer inlet cooler 16 at the highest temperature and the outlet of the second stage carbon monoxide metamorphic catalyst layer 19 are adjacent to each other, and carbon monoxide metamorphosis is not provided unless the heat insulating layer 47 is provided. The heat to be recovered in the catalyst layer inlet cooler 16 is transferred to the outlet gas of the carbon monoxide metamorphic catalyst layer 19 in the second stage, and goes out from the concentrically formed composite reformer to reduce the thermal efficiency. .. The heat insulating layer 47 provided in the portion in this way contributes to the improvement of thermal efficiency. [0083] FIG. 6 is a vertical schematic cross-sectional view for explaining a fourth embodiment of the fuel reformer for the polymer electrolyte fuel cell of the present invention. [0084] In this embodiment, as compared with FIG. 4, the carbon monoxide metamorphic catalyst layer 17 of the first stage is installed in the same annulus portion as the carbon monoxide metamorphic catalyst layer inlet cooler 16. As a result, the amount of the carbon monoxide metamorphic catalyst layer 19 in the second stage can be increased. The carbon monoxide metamorphic catalyst layer in the second stage is operated at a low temperature due to a decrease in CO concentration, but the reaction rate decreases at a low temperature, so a larger amount of catalyst is generally required than in the first stage. The configuration of FIG. 6 can increase the amount of carbon monoxide metamorphic catalyst layer in the second stage and achieve lower levels of CO concentration. [0085] FIG. 7 is a vertical schematic cross-sectional view for explaining a fifth embodiment of the fuel reformer for the polymer electrolyte fuel cell of the present invention. [0086] In this embodiment, as compared with FIG. 6, the carbon monoxide metamorphic catalyst layer inlet cooler 16 and the outside of the carbon monoxide metamorphic catalyst layer 17 of the first stage, the carbon monoxide metamorphic catalyst layer intermediate cooler 18 and the first stage A heat insulating layer is provided inside the carbon monoxide metamorphic catalyst layer 19 to prevent heat leakage from the inside at a high temperature to the outside at a low temperature. This merit is the same as that described in the embodiment of FIG. [0087] FIG. 8 is a vertical schematic cross-sectional view for explaining a sixth embodiment of the fuel reformer for the polymer electrolyte fuel cell of the present invention. [0088] In this embodiment, the carbon monoxide transformation catalyst layer 17 and the carbon monoxide transformation catalyst are arranged in a concentric cylindrical shape near the outer peripheral surface of the reformer. The layer intermediate cooler 18 and the second stage carbon monoxide reforming catalyst layer 19 are arranged as follows. That is, the outer peripheral surface of the first-stage carbon monoxide metamorphic catalyst layer 17 having a cylindrical outer shape, which are concentric and arranged in parallel in the axial direction, and the cylindrical carbon monoxide metamorphic catalyst layer intermediate cooler 18 and A cylindrical carbon monoxide transformation container 19 containing a cylindrical second-stage carbon monoxide transformation catalyst layer is arranged. [0089] With this configuration, the following effects can be obtained. That is, the reformed gas cooled by the carbon monoxide transformation catalyst layer inlet cooler 16 enters the cylindrical first stage carbon monoxide transformation catalyst layer 17, and the CO concentration of about 10% is reduced to about several%. After lowering, it is cooled by entering the carbon monoxide reforming catalyst layer intermediate cooler 18 configured in an annular shape on the outside thereof. After that, CO is reduced to about several thousand ppm in the second stage carbon monoxide metamorphic catalyst layer 19, and then sent to the carbon monoxide selective oxidation catalyst layer inlet cooler 20. The operation and effect of the equipment after the carbon monoxide selective oxidation catalyst layer inlet cooler 20 are the same as those in the embodiment of FIG. [0090] In the examples of FIGS. 4 to 7, since they are arranged concentrically, the diameter is large, and the occupied volume tends to increase particularly in the configurations of FIGS. 5 and 7. Therefore, by configuring the carbon monoxide metamorphic catalyst layer 17 in the first stage to the carbon monoxide metamorphic catalyst layer 19 in the second stage in a separate device, the occupied volume can be rather reduced. [0091] In addition to this, in general, the catalyst layer length is required to be 3 times or more the representative diameter in the design of the catalyst layer, but in the examples of FIGS. 4 to 7, the catalyst layer located on the outer periphery, especially the second stage carbon monoxide. In the carbon metamorphic catalyst layer 19, even if the width is narrow, the cross-sectional area is large, so that it may be difficult to keep the catalyst layer length. [0092] By configuring as shown in FIG. 8, the ratio of the catalyst layer length to the representative diameter can be kept above a certain level. Moreover, since there is no heat transfer from the high-temperature regeneration flow path 15, temperature control becomes easier. [0093] FIG. 9 is a vertical schematic cross-sectional view for explaining a seventh embodiment of the fuel reformer for the polymer electrolyte fuel cell of the present invention. [0094] In this embodiment, the carbon monoxide selective oxidation catalyst layer inlet cooler 20 is further integrated with the carbon monoxide metamorphic catalyst layer 17 of the embodiment of FIG. [0095] As a result, the occupied volume of the equipment can be further reduced, and the heat radiation in the carbon monoxide selective oxidation catalyst layer inlet cooler 20 and the front and rear pipes can be reduced. [0096] FIG. 10 is a vertical schematic cross-sectional view for explaining an eighth embodiment of the fuel reformer for the polymer electrolyte fuel cell of the present invention. [0097] (7) Explanation of Fig. 10 Compared to FIG. 8, the cylindrical first-stage carbon monoxide transformation catalyst layer 17 and the carbon monoxide transformation catalyst layer intermediate cooler 18 and the second-stage carbon monoxide transformation catalyst layer formed in an annulus shape on the outside thereof. A heat insulating layer 49 composed of gaps is formed between the nineteen. [0098] The heat insulating layer 49 blocks heat transfer from the first-stage carbon monoxide metamorphic catalyst layer 17 in the central portion to the outer carbon monoxide metamorphic catalyst layer intermediate cooler 18 and the second-stage carbon monoxide metamorphic catalyst layer 19. .. The heat insulating layer 49 has an effect of keeping the carbon monoxide transformation catalyst layer 17 of the first stage at a desired high temperature and keeping the carbon monoxide transformation catalyst layer 19 of the second stage at a desired low temperature. [0099] FIG. 11 is a vertical schematic cross-sectional view for explaining a ninth embodiment of the fuel reformer for the polymer electrolyte fuel cell of the present invention. [0100] In the embodiment of FIG. 9, a cylindrical first-stage carbon monoxide metamorphic catalyst layer 17 and an annulus-shaped carbon monoxide metamorphic catalyst layer intermediate cooler 18 and a second-stage carbon monoxide metamorphosis are formed on the outside thereof. A heat insulating layer 50 composed of gaps is formed between the catalyst layers 19. [0101] The effect of the heat insulating layer 50 is similar to that of the embodiment of FIG. [0102] FIG. 12 is a vertical schematic cross-sectional view for explaining a tenth embodiment of the fuel reformer for the polymer electrolyte fuel cell of the present invention. In this embodiment, the first stage carbon monoxide transformation catalyst layer 17, the carbon monoxide transformation catalyst layer intermediate cooler 18, the second stage carbon monoxide transformation catalyst layer 19, and the carbon monoxide selective oxidation catalyst layer are described. The inlet cooler 20 and the carbon monoxide selective oxidation catalyst layer 23B are formed in a rectangular shape, respectively, and the carbon monoxide metamorphic catalyst layer intermediate cooler 18 and the carbon monoxide metamorphic catalyst layer intermediate cooler 18 and the carbon monoxide metamorphic catalyst layer intermediate cooler 18 and The carbon monoxide selective oxidation catalyst layer inlet cooler 20 is brought into contact with each other, and the carbon monoxide metamorphic catalyst layer intermediate cooler 18 is brought into contact with the second stage carbon monoxide metamorphic catalyst layer 19 to make the carbon monoxide selective oxidation catalyst. The carbon monoxide selective oxidation catalyst layer 23B is brought into contact with the layer inlet cooler 20. [0103] The following effects can be obtained by configuring as shown in FIG. That is, the reformed gas cooled by the carbon monoxide transformation catalyst layer inlet cooler 16 is introduced into the rectangular first-stage carbon monoxide transformation catalyst layer 17, and the CO concentration of about 10% is reduced to about several%. After lowering to, it is cooled by entering the carbon monoxide reforming catalyst layer intermediate cooler 18 configured in a rectangular shape through a connecting pipe. After that, CO was reduced to about several thousand ppm in the second stage carbon monoxide metamorphic catalyst layer 19 configured in a rectangular parallelepiped shape, and then the carbon monoxide selective oxidation catalyst layer inlet cooler 20 configured in a rectangular parallelepiped shape was used. It is sent and cooled. The reformed gas mixed with oxygen or air was formed in a rectangular shape and was installed on the opposite side of the carbon monoxide metamorphic catalyst layer 19 of the second stage with the carbon monoxide metamorphic catalyst layer 17 of the first stage interposed therebetween. It is introduced into the carbon monoxide selective oxidation catalyst layer 23B to oxidize CO and reduce the CO concentration to the level of several to several tens of ppm. Oxygen or air mixed in the reformed gas may be mixed in either the inlet side or the outlet side of the carbon monoxide selective oxidation catalyst layer inlet cooler 20, but it is more preferable to mix in the inlet side. [0104] The reformed gas with reduced CO concentration is cooled to about 50 to 90 ° C, which is the operating temperature of the polymer electrolyte fuel cell, by the carbon monoxide selective oxidation catalyst layer outlet cooler 24, and the solid height is increased. Prevents the temperature balance of molecular fuel cells from being lost. [0105] In the examples of FIGS. 8 to 11, the carbon monoxide metamorphic catalyst layer 17 in the first stage to the carbon monoxide metamorphic catalyst layer 19 in the second stage or the carbon monoxide selective oxidation catalyst layer inlet cooler 20 are integrally formed in a cylindrical shape. However, these are formed in a rectangular shape and integrated, and the carbon monoxide selective oxidation catalyst layer in the subsequent stage is integrated to reduce the occupied volume of the entire device. [0106] In addition, the hottest first-stage carbon monoxide transformation catalyst layer 17 is placed at a position sandwiched between the lower-temperature second-stage carbon monoxide transformation catalyst layer 19 and the carbon monoxide selective oxidation catalyst layer 23B. Therefore, heat dissipation can be minimized. [0107] FIG. 13 is a vertical schematic cross-sectional view for explaining the eleventh embodiment of the fuel reformer for the polymer electrolyte fuel cell of the present invention. In this embodiment, the carbon monoxide selective oxidation catalyst layer 23B of the embodiment is brought into contact with the carbon monoxide selective oxidation catalyst layer outlet cooler 24 having a rectangular parallelepiped outer shape, and each of these components is integrated. It was done. As a result, the occupied volume of the entire device can be further reduced. [0108] FIG. 14 is a vertical schematic cross-sectional view for explaining a twelfth embodiment of the fuel reformer for the polymer electrolyte fuel cell of the present invention. In this embodiment, as compared with FIG. 12, the carbon monoxide selective oxidation catalyst layer 23B is divided into two to form the first stage carbon monoxide selective oxidation catalyst layer 21 and the second stage carbon monoxide selective oxidation catalyst layer 23. An intermediate carbon monoxide selective oxidation catalyst layer intermediate cooler 22 is added, and each is configured in a rectangular shape and integrated. [0109] Oxygen or air is modified and mixed upstream of each of the carbon monoxide selective oxidation catalyst layer 21 and the carbon monoxide selective oxidation catalyst layer 23 of the first stage. Oxygen or air corresponding to this may be mixed in and out of either the inlet side or the outlet side of the carbon monoxide selective acid reactor inlet cooler 20, but it is more preferable to mix it in the inlet side. Similarly, oxygen or air corresponding to the second stage may be mixed on either the inlet side or the outlet side of the carbon monoxide selective oxidation catalyst layer intercooler 22, but it is more likely that the oxygen or air flows in on the inlet side. desirable. [0110] Dividing the carbon monoxide selective oxidation catalyst layer 23B in this way is disadvantageous in terms of occupied volume, but it is easy to suppress the temperature rise of the carbon monoxide selective oxidation catalyst and reduces the amount of H2 consumed in the side reaction. effective. [0111] Although it is disadvantageous in terms of occupied volume, the carbon monoxide selective oxidation catalyst layer 23 in the second stage is divided into three or four parts beyond two divisions, and an intercooler is installed between the division stages. May be good. [0112] FIG. 15 is a vertical schematic cross-sectional view for explaining a thirteenth embodiment of the fuel reformer for the polymer electrolyte fuel cell of the present invention. In this embodiment, as compared with FIG. 13, the carbon monoxide selective oxidation catalyst layer 23B is divided into two to form the first stage carbon monoxide selective oxidation catalyst layer 21 and the second stage carbon monoxide selective oxidation catalyst layer 23. An intermediate carbon monoxide selective oxidation catalyst layer intermediate cooler 22 is added, and each is configured in a rectangular shape and integrated. [0113] By dividing the carbon monoxide selective oxidation catalyst layer 23B into 22 parts, the same effect as that described in FIG. 14, that is, H consumed in the side reaction, is obtained.₂You can reduce the amount of. [0114] 16 and 17 are for explaining the 14th embodiment of the fuel reformer of the polymer electrolyte fuel cell of the present invention, FIG. 16 is a vertical sectional view thereof, and FIG. 17 is FIG. It is a horizontal cross-sectional view taken in the direction of the arrow cut along the lines 17-17 of. [0115] The fuel reformer of the polymer electrolyte fuel cell shown in FIGS. 16 and 17 includes a reformer A, a carbon monoxide modifier B, a carbon monoxide selective oxidation reactor C, and a carbon monoxide modifier having the configurations described below. The inlet cooler 16 and the carbon monoxide selective oxidation reactor 20 are configured in a rectangular shape, and the reformer A, the carbon monoxide metaphor B, and the carbon monoxide selective oxidation reactor C are arranged side by side in this order. , The entire device is integrated. [0116] In the reformer A, the openings at both ends of the square cylinder 9d are closed by the lid member 9e and the bottom member 9f, and the combustion space container 9 for forming the radiant heat transfer portion 91 and the convection heat transfer portion 92 inside, and the combustion space container 9 A heat insulating material 44 is placed on the outer peripheral surface of the metal plate 43 on one side surface (right side side in the figure) of the square cylinder 9d, and side members 9f and are placed and fixed, and on the other side surface (left side side in the figure) of the square cylinder 9d. The plate-shaped partition wall 37A fixed to the square cylinder 9d and the bottom member 9f, the plate-shaped partition wall 38A arranged at a predetermined distance from the partition wall 37A and fixed to the bottom member 9f, and the partition wall 37A and the partition wall 38A. A plate-shaped modified catalyst layer 14A arranged between them, and partition walls 39A and 40A arranged and fixed at predetermined positions of the partition 38A and the partition 37A, which are arranged at the lower and upper positions of the modified catalyst layer 14A, respectively. A gas inlet 41 and a partition wall 40A, which are formed in a part of the lower end side of the reforming catalyst layer 14, for example, guide the reforming fuel 8 made of natural gas and the reforming steam 6 into the reforming catalyst layer 14A. Above, the outer periphery of the modified catalyst layer 14A and the partition wall 38A, and above the modified catalyst layer 14A (opposite the portion where the gas inlet 41 is formed), fixed to the lid member 9e, and the regenerated flow. It is for forming the road 15A and is composed of a modified L-shaped flow path forming member 32A having an L-shaped flange on one end side. [0117] A deformation that is arranged so as to form a rectangular gap (insulation layer) 25A on the outside of the flow path forming member 32A, has an L-shaped flange on one end side, and is joined to the lower end of the flow path forming member 32A. An L-shaped partition 33A, a cooler 16A such as a cooling jacket configured in a box shape, and a plate shape, for example, arranged above the partition 33A. One end of the bottom member 42A, which is arranged on the side surface of the first stage carbon monoxide metamorphic catalyst layer 17A, the carbon monoxide metamorphic catalyst layer 17A, and the carbon monoxide transformation inlet cooler 16A, and is joined to the bottom member 9f. Is arranged on the plate-shaped heat insulating material 45 to which the catalyst is fixed, and the cooler 18A such as a cooling jacket configured in a box shape and arranged on the lower side of the heat insulating material 45, for example. A fixed plate-shaped heat insulating material 46 arranged on the side surface of the plate-shaped second stage carbon monoxide metamorphic catalyst layer 19A and the cooler 18A and the carbon monoxide metamorphic catalyst layer 19A and joined to the flange of the partition 33A. And the rectangular carbon monoxide selective oxidation catalyst layer inlet cooler (carbon monoxide selective oxidation catalyst layer pre-cooler) 20A on the side surface of the heat insulating material 46 from the lower side to the upper side, and the first stage of the rectangular shape. Carbon monoxide selective oxidation catalyst layer 21A, rectangular carbon monoxide selective oxidation catalyst layer intermediate cooler 22A, rectangular second stage carbon monoxide selective oxidation catalyst layer 23A, and rectangular carbon monoxide Selective oxidation catalyst layer outlet cooler (carbon monoxide selective oxidation catalyst layer post-cooler) 24A, cooler 20A, carbon monoxide selective oxidation catalyst layer 21A, carbon monoxide selective oxidation catalyst layer intermediate cooler 22A and monoxide It is composed of a plate-shaped partition wall 36A which is arranged on the side surface of the carbon selective oxidation catalyst layer 23A and the cooler 24A, and both ends thereof are fixed to the flange of the partition wall 33A and the bottom member 42A, respectively. Air headers 621A and 622A are arranged on the outer peripheral surface of the partition wall 36A as described below. [0118] The operation of the 14th embodiment is the same as that of the 1st embodiment. First, the combustion fuel 1 of the fuel cell main body (not shown) is introduced into the combustor 10 and burned in the combustion space container 9 at 1000 °. Generates heat with a high temperature of C or higher. The combustion gas transfers heat to the reforming catalyst layer 14A, and the reforming catalyst layer 14A itself is discharged as combustion exhaust gas 3 in a state where the temperature is lowered, and is exhausted after being used as a heat source for the evaporator 13. [0119] At this time, since the center plug 11 is installed in the combustion space container 9, radiant heat transfer and convective heat transfer to the reformer are effectively performed, while the reforming fuel 8 is a gas-liquid separator. After being mixed with the water vapor 6 generated in 26, it is circulated to the reforming catalyst layer 14 in a state of almost atmospheric pressure. In the reforming catalyst layer 14A, the reforming reaction occurs by receiving the heat of the combustion gas described above, and the fuel reacts almost 100% to generate hydrogen, carbon monoxide, and carbon dioxide. Since the reformed gas containing these components and the steam that was not used in the reaction has a high temperature, it exchanges heat with the reformed catalyst layer 14 while passing through the regeneration flow path 15A, and the exhaust heat is recovered. [0120] Immediately after passing through the regeneration flow path 15A, the reformed gas is still at a high temperature of about 400 ° C to 500 ° C. It passes through and is cooled to 200 ° C to 300 ° C. The reformed gas that has been cooled and lowered in temperature is circulated to the carbon monoxide metamorphic catalyst layer 17A, and the carbon monoxide generated in the reformed catalyst layer reacts with water vapor to generate carbon dioxide and hydrogen. A so-called shift reaction occurs. [0121] Since this reaction is an exothermic reaction, the temperature of the reformed gas rises while passing through the catalyst layer, and when it exits the carbon monoxide metamorphic catalyst layer 17A, the reaction reaches an almost equilibrium state. The reformed gas that has passed through the carbon monoxide metamorphic catalyst layer 17A in the first stage is cooled while passing around the cooler 18A, the temperature drops, and the state suitable for the shift reaction is restored. Since the equilibrium concentration of the cooled reformed gas decreases as the temperature decreases, the shift reaction proceeds again during the flow of the second stage carbon monoxide transformation catalyst 19A, and the temperature rises while carbon monoxide carbon monoxide. The concentration decreases to about 5000 ppm. [0122] After that, air is mixed into the reformed gas from the air introduction header 621A, and then flows into the carbon monoxide selective oxidation catalyst layer 21 of the first stage in a state where the temperature drops after passing around the cooler 20. .. While passing through the carbon monoxide selective oxidation catalyst layer 21A, carbon monoxide in the reformed gas reacts with oxygen in the air to become carbon dioxide. This reaction has a large calorific value, and the temperature of the reformed gas rises sharply. [0123] Then, after being cooled by the cooler 22A, a small amount of air is mixed in again from the air header 622A, and then the selective oxidation reaction proceeds again while the second stage carbon monoxide selective oxidation catalyst 23A is flowing, and the temperature is increased. While rising, the carbon monoxide concentration becomes 10ppm or less. After that, the reformed gas is cooled by the cooler 24A and supplied to the fuel cell body. [0124] According to the fourteenth embodiment described above, by configuring as shown in FIG. 16, the entire apparatus becomes rectangular, and the fuel reforming apparatus can be made compact as in the case of the cylindrical type shown in the first embodiment. it can. [0125] Further, in the present embodiment as in the first embodiment, as shown in FIG. 16, the carbon monoxide metamorphic catalyst layer is divided into the first stage and the second stage carbon monoxide metamorphic catalyst layers 17A and 19A. By arranging the cooler 18A in the middle, it is not necessary to bury the heat transfer tube in the catalyst layer as in the conventional case, and the width of the catalyst layer can be narrowed. The device can be made smaller. At this time, it goes without saying that the same effect can be obtained even if the catalyst layer is further subdivided and a cooler is provided in the middle of each. [0126] Further, in the present embodiment as in the first embodiment, as shown in FIG. 16, the carbon monoxide selective oxidation catalysts of the first and second stages are separately cooled as the carbon monoxide selective oxidation catalysts 21A and 23A. By arranging the vessel 22A in the middle, the amount of catalyst is reduced because the part that becomes locally hot in the catalyst layer is reduced compared to the case where the heat transfer tube is embedded in the catalyst layer and cooled as in the conventional case. Is the minimum required, and the entire device can be made compact. At this time, it goes without saying that if the catalyst layer is further subdivided and a cooler is provided in the middle of each, the number of local high temperature portions is further reduced. [0127] Further, in the present embodiment as in the first embodiment, as shown in FIG. 16, by arranging the cooler 24A downstream of the carbon monoxide selective oxidation catalyst layer 23A, the cooler 24A is arranged in the catalyst layer as in the conventional case. Compared with the case where the heat transfer tube is embedded and cooled, the portion of the catalyst layer that becomes locally hot is reduced, so that the amount of catalyst can be minimized and the entire apparatus can be made compact. [0128] Further, in the present embodiment as in the first embodiment, as shown in FIG. 16, the reformer which usually has a high temperature of 500 ° C to 1000 ° C by installing the gap (insulation layer) 25A. Even if the part and another carbon monoxide transformer or carbon monoxide selective oxidation reactor with a temperature of about 100 ° C to 300 ° C are installed adjacent to each other, they can be thermally separated, so that due to heat leakage. The load on the coolers 16A, 18B, 20B, 22B and 24B can be reduced. In addition, it is possible to absorb the elongation difference due to the thermal expansion of the partition wall that occurs between the high temperature level reformer and the low temperature level carbon monoxide metamorphizer, and it is possible to reduce the thermal stress, so that the structure and strength are improved. Since the problem can be solved, the fuel reformer can be made smaller. [0129] Further, in the present embodiment as in the first embodiment, the mixture of the reforming fuel 8 and the steam 6 is circulated inside the cooler 16A upstream of the carbon monoxide transformation catalyst layer in the first stage. You can also. With such a configuration, the reformed gas can be cooled and heat can be recovered, so that the system efficiency of the fuel cell system can be improved. Further, in the present embodiment as in the first embodiment, the gas-liquid mixture after leaving the evaporator 13 is circulated inside the cooler 18A installed in the middle of the carbon monoxide metamorphic catalyst layer, for example. You can also do it. With such a configuration, the reformed gas can be cooled and heat can be recovered, so that the system efficiency of the fuel cell system can be improved. [0130] 18 and 19 are diagrams for explaining a fifteenth embodiment of the fuel reformer of the polymer electrolyte fuel cell of the present invention, FIG. 18 is a vertical sectional view thereof, and FIG. 19 is FIG. It is a horizontal cross-sectional view taken in the direction of the arrow cut along the lines 19-19 of. [0131] In the fifteenth embodiment, the reformer A is configured in a cylindrical shape as in the first embodiment, and the devices other than the reformer A are configured in a rectangular parallelepiped shape as in the fourteenth embodiment. Is. That is, the carbon monoxide metamorphic reactor B, the carbon monoxide selective oxidation reactor C, the carbon monoxide metabolizer inlet cooler 16A, and the carbon monoxide selective oxidation reactor inlet cooler 20A are configured in a rectangular shape, and the reformer A, The carbon monoxide metamorphizer B and the carbon monoxide selective oxidation reactor C are arranged side by side in this order, and the entire equipment is integrated. [0132] The operation of the fifteenth embodiment apparatus configured in this way is the same as that of the first embodiment and the second embodiment. First, the combustion fuel 1 of the fuel cell main body is introduced into the combustor 10 and burned. It burns in the space container 9 to generate high-temperature heat of 1000 ° C or higher. The combustion gas transfers heat to the reforming catalyst layer 14, and the reforming catalyst layer 14 itself is discharged as combustion exhaust gas 3 in a state where the temperature is lowered, and is exhausted after being used as a heat source for the evaporator 13. [0133] At this time, since the center plug 11 is installed in the combustion space container 9, heat transfer to the reformer A is effectively performed by radiant heat transfer and convective heat transfer. [0134] On the other hand, the reforming fuel 8 is mixed with the steam 6 generated in the gas-liquid separator 26 and then distributed to the reforming catalyst layer 14 in a state of substantially atmospheric pressure. In the reforming catalyst layer 14, the reforming reaction occurs by receiving the heat of the combustion gas described above, and the fuel reacts almost 100% to generate hydrogen, carbon monoxide, and carbon dioxide. Since the reformed gas containing these components and the steam that was not used in the reaction has a high temperature, it exchanges heat with the reformed catalyst layer 14 while passing through the regeneration flow path 15, and the exhaust heat is recovered. [0135] Immediately after passing through the regeneration channel 15, the reformed gas is still at a high temperature of about 400 ° C to 500 ° C. Therefore, before entering the first stage carbon monoxide metamorphic catalyst layer 17A, the area around the cooler 16A. It passes through and is cooled to 200 ° C to 300 ° C. The reformed gas that has been cooled and lowered in temperature is circulated to the carbon monoxide metamorphic catalyst layer 17A, and the carbon monoxide generated in the reformed catalyst layer reacts with water vapor inside this to generate carbon dioxide and hydrogen. A so-called shift reaction occurs. Since this reaction is an exothermic reaction, the temperature of the reformed gas rises while passing through the catalyst layer, and when it exits the carbon monoxide metamorphic catalyst layer 17A, the reaction reaches an almost equilibrium state. [0136] The reformed gas that has passed through the carbon monoxide metamorphic catalyst layer 17A in the first stage is cooled while passing around the cooler 18A, the temperature drops, and the shift reaction can occur again. Since the equilibrium concentration of the cooled reformed gas decreases as the temperature decreases, the shift reaction proceeds again during the flow of the second stage carbon monoxide transformation catalyst 19A, and the temperature rises while carbon monoxide carbon monoxide. The concentration decreases to about 5000 ppm. [0137] After that, air was mixed into the reformed gas from the air introduction headers 621A and 622A, and then passed around the cooler 20A to lower the temperature, and then the carbon monoxide selective oxidation catalyst layer 21A of the first stage was formed. Inflow. While passing through the carbon monoxide selective oxidation catalyst layer 21A, carbon monoxide in the reformed gas reacts with oxygen in the air to become carbon dioxide. This reaction has a large calorific value, and the temperature of the reformed gas rises rapidly. [0138] After that, after being cooled by the cooler 22A, a small amount of air is mixed from the air header 622, and the selective oxidation reaction proceeds again while the second stage carbon monoxide selective oxidation catalyst 23A is flowing, and the temperature rises. The carbon monoxide concentration is 10 ppm or less. After that, the reformed gas is cooled by the cooler 24A and supplied to the fuel cell body. [0139] As shown in the fifteenth embodiment, the heat generated in the combustion space container 9 is efficiently transferred to the catalyst layer by forming the combustion space container 9, the modified catalyst layer 14A, and the regeneration flow path 15 in a cylindrical shape. Therefore, fuel consumption can be saved. [0140] Separately, the carbon monoxide metamorphic catalyst layers 17A, 19A, coolers 16A, 18A, 20A, 22A, 24A, and carbon monoxide selective oxidation catalyst layers 21A, 23A are formed in a rectangular parallelepiped shape to form the first and first carbon monoxide. Similar to the second embodiment, the fuel reformer can be made compact. [0141] Furthermore, by connecting the reformer A and other equipment such as carbon monoxide transformer B and carbon monoxide selective oxidation reactor C with pipe 31, the high temperature level of 500 ° C to 1000 ° C And the part of the medium temperature level of about 100 ° C to 300 ° C can be thermally separated without any ingenuity such as a heat insulating layer. Since it can be thermally separated, it is possible to suppress a heat leak from the high temperature reformer A side to the medium temperature carbon monoxide transformer, so that the cooler can be miniaturized. [0142] Further, as shown in FIG. 18, in the present embodiment as in the first and 14th embodiments, the carbon monoxide metamorphic catalyst layers are divided into the first and second carbon monoxide metamorphic catalyst layers 17A and 19A. By arranging the cooler 18A in the middle of the catalyst layer, it is not necessary to bury a heat transfer tube in the catalyst layer as in the past, and the width of the catalyst layer can be narrowed. The quality device can be made smaller. At this time, it goes without saying that the same effect can be obtained even if the catalyst layer is further subdivided and a cooler is provided in the middle of each. [0143] Further, in the present embodiment as in the first and 14th embodiments, as shown in FIG. 18, the carbon monoxide selective oxidation catalyst layer 21A of the first and second stages is used as the carbon monoxide selective oxidation catalyst layer. By arranging the cooler 22A in the middle of the catalyst layer, the temperature of the part that becomes locally high in the catalyst layer becomes higher than that in the conventional case where the heat transfer tube is embedded in the catalyst layer for cooling. Since the amount is reduced, the amount of catalyst can be minimized, and the entire device can be made compact. At this time, it goes without saying that if the catalyst layer is further subdivided and a cooler is provided in the middle of each, the number of local high temperature portions is further reduced. [0144] Further, in the present embodiment as in the first and 14th embodiments, as shown in FIG. 18, the conventional heat transfer tube is provided by arranging the cooler 24A downstream of the carbon monoxide selective oxidation catalyst layer 23A. Compared with the method of burying a heat transfer tube inside the carbon monoxide selective oxidation catalyst layer for cooling, the portion of the catalyst layer that becomes locally hot is reduced, so that the entire device can be made compact. [0145] Further, in the present embodiment as in the first and 14th embodiments, a mixture of reforming fuel 8 and steam 6 is placed inside the cooler 16A upstream of the carbon monoxide transformation catalyst layer in the first stage. It can also be distributed. With such a configuration, the reformed gas can be cooled and heat can be recovered, so that the system efficiency of the fuel cell system can be improved. Further, in the present embodiment as in the first and 14th embodiments, the gas-liquid mixture after leaving the evaporator 13 is inside the cooler 18A installed in the middle of the carbon monoxide metamorphic catalyst layer, for example. Can also be distributed. With such a configuration, the reformed gas can be cooled and heat can be recovered, so that the system efficiency of the fuel cell system can be improved. [0146] [Industrial applicability] The fuel reformer of the polymer electrolyte fuel cell of the present invention can also be used as various power sources such as an in-vehicle power source and a stationary power source. [0147] [Effect of the invention] According to the present invention described above, it is possible to provide a compact fuel reformer for a polymer electrolyte fuel cell, regardless of the raw material and fuel, without increasing the required fuel. [Simple explanation of drawings] FIG. 1 is a vertical cross-sectional view of a fuel reformer for a polymer electrolyte fuel cell showing a first embodiment of the present invention. FIG. 2 is a schematic view showing a horizontal cross section of only the air introduction header portion of the fuel reformer of the polymer electrolyte fuel cell showing the first embodiment of the present invention. FIG. 3 is a graph showing the number of introduction holes for carbon monoxide selective oxidation reaction air according to the present invention and the degree of oxygen diffusion. FIG. 4 is a vertical schematic cross-sectional view of a fuel reformer for a polymer electrolyte fuel cell showing a second embodiment of the present invention. FIG. 5 is a vertical schematic cross-sectional view of a fuel reformer for a polymer electrolyte fuel cell showing a third embodiment of the present invention. FIG. 6 is a vertical schematic cross-sectional view of a fuel reformer for a polymer electrolyte fuel cell showing a fourth embodiment of the present invention. FIG. 7 is a vertical schematic cross-sectional view of a fuel reformer for a polymer electrolyte fuel cell showing a fifth embodiment of the present invention. FIG. 8 is a vertical schematic cross-sectional view of a fuel reformer for a polymer electrolyte fuel cell showing a sixth embodiment of the present invention. FIG. 9 is a vertical schematic cross-sectional view of a fuel reformer for a polymer electrolyte fuel cell showing a seventh embodiment of the present invention. FIG. 10 is a vertical schematic cross-sectional view of a fuel reformer for a polymer electrolyte fuel cell showing an eighth embodiment of the present invention. FIG. 11 is a vertical schematic cross-sectional view of a fuel reformer for a polymer electrolyte fuel cell showing a ninth embodiment of the present invention. FIG. 12 is a vertical schematic cross-sectional view of a fuel reformer for a polymer electrolyte fuel cell showing a tenth embodiment of the present invention. FIG. 13 is a vertical schematic cross-sectional view of a fuel reformer for a polymer electrolyte fuel cell showing the eleventh embodiment of the present invention. FIG. 14 is a vertical schematic cross-sectional view of a fuel reformer for a polymer electrolyte fuel cell showing a twelfth embodiment of the present invention. FIG. 15 is a vertical schematic cross-sectional view of a fuel reformer for a polymer electrolyte fuel cell showing a thirteenth embodiment of the present invention. FIG. 16 is a vertical sectional view of a fuel reformer of a polymer electrolyte fuel cell showing a 14th embodiment of the present invention. FIG. 17 is a horizontal cross-sectional view taken along the lines 17-17 of FIG. 16 and viewed in the direction of the arrow. FIG. 18 is a vertical sectional view of a fuel reformer for a polymer electrolyte fuel cell showing a fifteenth embodiment of the present invention. FIG. 19 is a horizontal cross-sectional view taken along the line 19-19 of FIG. 18 and viewed in the direction of the arrow. FIG. 20 is a schematic view showing an example of a fuel reformer of a conventional polymer electrolyte fuel cell. Conceptual diagram of.