Abstract:
Provided is a hydrogen generator which is capable of reducing a size of an entire apparatus and reducing a running cost by utilizing heat of a heat exchanger ( 1 ) for hydrogen reforming in a reformer ( 2 ), and which can particularly preferably be used in a facility such as a hospital, a restaurant, or a hotel utilizing both steam and electricity, and a fuel cell system using the hydrogen generator. The hydrogen generator includes the reformer ( 2 ) for generating hydrogen H 2  from a fuel gas G and steam H 2 O incorporated in a fuel gas passage ( 12 ) of the heat exchanger ( 1 ) provided with a water pipe ( 13 ). The hydrogen generator utilizes a part of heat of the heat exchanger ( 1 ) for hydrogen reforming performed in the reformer ( 2 ). The hydrogen generator includes the reformer ( 2 ), a converter ( 3 ) for generating hydrogen from carbon monoxide generated in the reformer and steam, and a CO remover ( 4 ) for removing a carbon monoxide gas generated in the converter ( 3 ). The reformer ( 2 ), the converter ( 3 ), and the CO remover ( 4 ) are arranged in the flue gas passage ( 12 ) of the heat exchanger ( 1 ).

Description:
BACKGROUND OF THE INVENTION 
       [0001]    1. Field of the Invention 
         [0002]    The present invention relates to a hydrogen generator which is favorably used as a hydrogen supply source to a fuel cell to be provided in a hospital, a hotel, or the like utilizing a large volume of steam, and to a fuel cell system using the hydrogen generator. 
         [0003]    2. Description of the Related Art 
         [0004]    Conventionally, there is known a facility having a boiler (heat exchanger) and a fuel cell and provided with a reformer for generating hydrogen from a gas and steam, to thereby supply hydrogen obtained in the reformer to the fuel cell and provide hydrogen for power generation. A part of steam from the boiler is supplied to the reformer and used for hydrogen generation (see JP 06-13093 A). 
       SUMMARY OF THE INVENTION 
       [0005]    However, the above-mentioned facility has a reformer arranged outside, and thus an entire apparatus has a large size. 
         [0006]    The present invention has been made in view of the above, and therefore an object of the present invention is to provide a hydrogen generator which is capable of reducing a size of an entire apparatus and reducing a running cost by utilizing heat of a heat exchanger for hydrogen reforming in a reformer, and which can be used particularly preferably in a facility such as a hospital, a restaurant, or a hotel utilizing both steam and electricity, and a fuel cell system using the hydrogen generator. 
         [0007]    In order to solve the above-mentioned problem, a hydrogen generator according to a first aspect of the present invention includes: a heat exchanger provided with a water pipe and a reformer for generating hydrogen from a fuel and steam, wherein the reformer is incorporated into a flue gas passage of the heat exchanger. 
         [0008]    In the hydrogen generator according to the first aspect of the present invention, the reformer is incorporated in the flue gas passage of the heat exchanger, and a part of heat of the heat exchanger is used as a heat source for generation of hydrogen from a fuel such as a gas and steam in the reformer. Thus, reduction in size of an entire facility can be realized, and reduction in running cost can be realized. The flue gas passage of the heat exchanger has a large temperature distribution from high temperature to low temperature, and the reformer requires an optimum temperature for efficient generation of hydrogen in accordance with the kind of catalyst to be used. Thus, the reformer can be arranged in a temperature region of the heat exchanger providing an optimum temperature for hydrogen reforming. As a result, the reformer allows efficient generation of hydrogen. 
         [0009]    A hydrogen generator according a second aspect of the present invention, the reformer includes one of a reforming catalyst and a hydrogen separation membrane. 
         [0010]    In the hydrogen generator according to the second aspect of the present invention, a high concentration of hydrogen can be obtained in the reformer. 
         [0011]    A hydrogen generator according to a third aspect of the present invention further includes: a converter for generating hydrogen from carbon monoxide generated in the reformer and steam; and a CO remover for removing a carbon monoxide gas generated in the converter, in which the reformer, the converter, and the CO remover are arranged in the flue gas passage of the heat exchanger. 
         [0012]    In the hydrogen generator according to the third aspect of the present invention, hydrogen can be obtained efficiently with the reformer, the converter, and the CO remover. That is, the reformer, the converter, and the CO remover have different optimum temperature ranges for efficiently exhibiting functions of respective catalysts to be used, and the reformer, the converter, and the CO remover can respectively be arranged in optimum temperature regions of the heat exchanger. Thus, the reformer, the converter, and the CO remover can exhibit respective functions efficiently, to thereby improve a hydrogen generation rate. 
         [0013]    A hydrogen generator according to a fourth aspect of the present invention includes: a converter for generating hydrogen from carbon monoxide generated in the reformer and steam; and a CO remover for removing a carbon monoxide gas generated in the converter, in which the converter and the CO remover are provided downstream of the reformer and outside the flue gas passage of the heat exchanger. 
         [0014]    In the hydrogen generator according to the fourth aspect of the present invention, the heat exchanger requires no portion for the converter and the CO remover, and a large volume of steam generated can be assured. 
         [0015]    A hydrogen generator according to a fifth aspect of the present invention, downstream of the water pipe of the heat exchanger is connected to upstream of the reformer. 
         [0016]    In the hydrogen generator according to the fifth aspect of the present invention, hydrogen can be obtained stably in the reformer. 
         [0017]    According to a sixth aspect of the present invention, there is provided a fuel cell system provided with a hydrogen generator, including a fuel cell connected to downstream of the hydrogen generator according to any one of the first to fifth aspects of the present invention. 
         [0018]    In the fuel cell system according to the sixth aspect of the present invention, a fuel cell system having a small size as an entire facility and a low running cost can be obtained. 
         [0019]    According to a fuel cell system provided with a hydrogen generator according to a seventh aspect of the present invention, a reformed gas from the hydrogen generator is supplied to upstream of the flue gas passage of the heat exchanger. 
         [0020]    In the fuel cell system according to the seventh aspect of the present invention, efficient use of energy can be attempted, or NOx generation can be suppressed. That is, in the case where a large amount of hydrogen is present in a reformed gas from the hydrogen generator, efficient use of energy can be attempted. Meanwhile, in the case where a large amount of carbon dioxide is present in the reformed gas, NOx generation can be suppressed. 
         [0021]    A fuel cell system provided with a hydrogen generator according to an eighth aspect of the present invention further includes: a detector for detecting a concentration of hydrogen or carbon dioxide in a reformed gas supplied from the hydrogen generator to the fuel cell; and adjusting means for adjusting a supply volume of the reformed gas to the upstream of the flue gas passage of the heat exchanger based on a detection result of the detector. 
         [0022]    In the fuel cell system according to the eighth aspect of the present invention, efficient use of energy or suppression of NOx generation can be selected in accordance with a state of a fuel in the hydrogen generator. 
         [0023]    According to the hydrogen generator and the fuel cell system using the same, a size of an entire apparatus and a running cost can be reduced. Further, the hydrogen generator and the fuel cell system can preferably be used in a facility such as a hospital or a hotel utilizing both steam and electricity. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0024]    In the accompanying drawings: 
           [0025]      FIG. 1  is a piping block diagram showing a fuel cell system provided with a hydrogen generator according to an embodiment of the present invention; 
           [0026]      FIG. 2  is a piping block diagram showing a fuel cell system employing a membrane reactor-type reformer according to another embodiment of the present invention; 
           [0027]      FIG. 3  is a sectional diagram showing a catalyst device used for a membrane reactor-type reformer; 
           [0028]      FIG. 4  is a schematic diagram showing a formation example of a reformer in the case where a cylindrical body is used as a heat exchanger; 
           [0029]      FIG. 5  is a schematic diagram showing an example employing the same heat exchanger as that of  FIG. 4  and having a reformer provided outside of the cylindrical body; 
           [0030]      FIG. 6  is a schematic diagram showing a formation example of a reformer in the case where a rectangular body is used as a heat exchanger; 
           [0031]      FIG. 7  is a schematic diagram showing another formation example of the reformer in the case where a rectangular body is used as a heat exchanger; 
           [0032]      FIG. 8  is a schematic diagram showing still another formation example of the reformer in the case where a rectangular body is used as a heat exchanger; 
           [0033]      FIG. 9  is a graph showing an inside temperature distribution of a rectangular body used as a heat exchanger by section; and 
           [0034]      FIG. 10  is a graph showing an inside temperature distribution of a cylindrical body used as a heat exchanger by section. 
       
    
    
     DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS 
       [0035]    Next, embodiments of the present invention will be described. 
         [0036]    A hydrogen generator according to each embodiment of the present invention includes a reformer incorporated in a flue gas passage of a heat exchanger provided with a water pipe. A rectangular or cylindrical heat exchanger may be used. The rectangular heat exchanger includes a plurality of water pipes arranged vertically in a flue gas passage of a rectangular body, and a cylindrical heat exchanger includes a plurality of water pipes arranged vertically along a flue gas passage formed in a circumferential direction of a cylindrical body. Heat exchange is conducted between water flowing inside each of the water pipes and a flue gas flowing through the flue gas passage, and steam is taken out of the heat exchanger. 
         [0037]    The reformer is provided by removing a water pipe provided in the heat exchanger, and inserting a metal pipe, which is different from the water pipe, filled with a hydrogen reforming catalyst. A membrane reactor-type reformer may also be used. The membrane reactor-type reformer may include a tubular hydrogen separation membrane subjected palladium plating or the like on a surface of a porous metal pipe, and the hydrogen separation membrane is inserted into the metal pipe together with the hydrogen reforming catalyst. Alternatively, the membrane reactor-type reformer may include a sheet-like hydrogen separation membrane subjected to palladium plating or the like, opposing a metal sheet, and having the hydrogen reforming catalyst filled between the opposing parts. In this case, the reformer is arranged inside the flue gas passage of the heat exchanger, or arranged outside the flue gas passage and connected to the flue gas passage. 
         [0038]    The hydrogen generator preferably includes, in addition to the reformer described above, the converter for generating hydrogen from carbon monoxide generated in the reformer and steam, and the CO remover for removing a carbon monoxide gas generated in the converter. The reformer, the converter, and the CO remover are preferably arranged in the flue gas passage of the heat exchanger. 
         [0039]    An example of the hydrogen reforming catalyst to be used for the reformer is NiO(Al 2 O 3 ). Examples of the catalyst to be used in the converter include: Fe 2 O 3  and Cr 2 O 3 ; and CuO, ZnO, and Al 2 O 3 . An example of the catalyst to be used in the CO remover is Ru. A temperature at which NiO(Al 2 O 3 ) most effectively functions is 600 to 800° C., and a temperature at which Fe 2 O 3  and Cr 2 O 3  most effectively function is 320 to 400° C. A temperature at which CuO, ZnO, and Al 2 O 3  most effectively function is 180 to 250° C., and a temperature at which Ru most effectively functions is 150 to 200° C. Meanwhile, the rectangular heat exchanger has a temperature range of about 300 to 1,500° C., and the cylindrical heat exchanger has a temperature range of about 300 to 1,200° C. The reformer employing NiO(Al 2 O 3 ) as a catalyst is arranged upstream of the flue gas passage of the heat exchanger at a position having a temperature range of 600 to 800° C., and the converter employing Fe 2 O 3  and Cr 2 O 3  as catalysts is arranged midstream of the flue gas passage at a position having a temperature range of 320 to 400° C. The converter employing CuO, ZnO, and Al 2 O 3  as catalysts is arranged at a position having a temperature range of 180 to 250° C., and the CO remover employing Ru as a catalyst is arranged downstream of the flue gas passage at a position having a temperature range of 150 to 200° C. 
         [0040]    For use of steam generated in the heat exchanger for hydrogen generation in the reformer, downstream of the water pipe provided in the heat exchanger is connected to upstream of the reformer, to thereby generate hydrogen from a part of steam generated in the heat exchanger and a fuel such as a gas. 
         [0041]    A fuel cell is connected to downstream of the hydrogen generator, and hydrogen generated in the hydrogen generator is supplied for power generation in the fuel cell. 
         [0042]    A pipe is provided between the fuel cell and the flue gas passage of the heat exchanger for connecting the fuel cell and the flue gas passage. A gas allowed to flow through the fuel cell is supplied to upstream of the flue gas passage through this pipe, to thereby attempt efficient use of energy or suppress NOx generation. That is, in the case where a large amount of hydrogen is present in a gas from the hydrogen generator, efficient use of energy can be attempted, and in the case where a large amount of carbon dioxide is present in the gas, NOx generation can be suppressed. The above-mentioned hydrogen generator can be used for not only the fuel cell but also a semiconductor production device in which a large amount of hydrogen is used, for example. 
       Embodiment 1 
       [0043]    Hereinafter, a specific embodiment of a hydrogen generator according to the present invention will be described based on figures.  FIG. 1  is a piping block diagram showing a fuel cell system provided with a hydrogen generator according to the embodiment of the present invention. In the embodiment shown in  FIG. 1 , a rectangular heat exchanger  1  having a plurality of water pipes  13  arranged in a flue gas passage  12  inside a rectangular body  11  is used, and a reformer  2  is arranged upstream of the flue gas passage  12 . A converter  3  is arranged midstream of the flue gas passage  12 , and a CO remover  4  is arranged downstream of the flue gas passage  12 . 
         [0044]    To an inlet side of the reformer  2 , a first pipe  51  extending from a supply source of a fuel gas G such as a city gas is connected, and a desulfurizer  6  is provided in the first pipe  51 . A second pipe  52  is connected between an outlet side of the reformer  2  and an inlet side of the converter  3 . A third pipe  53  is connected between an outlet side of the converter  3  and the CO remover  4 , and a fuel cell  7  is connected to an outlet side of the CO remover  4  through a fourth pipe  54 . To an inlet side of the heat exchanger  1 , a fifth pipe  55  extending from a water supply source is connected. A first heat exchanger  5 A is provided in a middle of each of the fifth pipe  55  and the second pipe  52 , and a second heat exchanger  5 B is provided in a middle of each of the fifth pipe  55  and the fourth pipe  54  such that a reformed gas flowing from the reformer  2  to the converter  3  and a reformed gas flowing from the CO remover  4  to the fuel cell  7  exchange heat with supply water flowing through the fifth pipe  55  in the first heat exchanger  5 A and the second heat exchanger  5 B to be supplied to the inlet side of the heat exchanger  1 . Thus, a heat exchange rate of the heat exchanger  1  can be improved. 
         [0045]    A sixth pipe  56  is provided between an outlet side of the heat exchanger  1  and upstream of the first pipe  51  in the reformer  2  such that a part of steam S obtained in the heat exchanger  1  is used for hydrogen generation in the reformer  2 . In the embodiment shown in  FIG. 1 , a gas discharge side of the fuel cell  7  is connected to upstream of the flue gas passage  12  of the heat exchanger  1  through a seventh pipe  57 . The gas allowed to flow through the fuel cell  7  is supplied to the heat exchanger  1  and combusted. Thus, in the case where a large amount of hydrogen is present in a gas from the hydrogen generator, efficient use of energy can be attempted, and in the case where a large amount of carbon dioxide is present in the gas, NOx generation can be suppressed. Thus, efficient use of energy can be attempted or NOx generation can be suppressed. 
         [0046]    Note that in  FIG. 1 , the gas discharge side of the fuel cell  7  is connected to the upstream of the flue gas passage  12  of the heat exchanger  1  through the seventh pipe  57  but the gas can be introduced to upstream of the heat exchanger  1  by branching the fourth pipe  54  before the gas enters the fuel cell  7  and connecting the branched fourth pipe  54  to the upstream of the flue gas passage  12  of the heat exchanger  1 . 
         [0047]    In the above-mentioned fuel cell system, the fuel gas G is supplied and combusted in the fuel gas passage  12  of the heat exchanger  1 . The flue gas flowing through the flue gas passage  12  toward the discharge side exchanges heat with water supplied to the water pipe  13  to generate the steam S, and the steam S is taken out of the heat exchanger  1  for a purpose of various operations. A part of the fuel gas G is delivered to the desulfurizer  6  through the first pipe  51 , and a sulfur content which is a corroding component mixed in the fuel gas G is removed therefrom in the desulfurizer  6  and delivered to the reformer  2 . To the upstream of the first pipe  51  in the reformer  2 , the steam S is supplied from the sixth pipe  56 , and the steam S and the fuel gas G are delivered to the reformer  2 . In the reformer  2 , a hydrogen rich gas is generated from the steam S and the fuel gas G with a reforming catalyst such as NiO (Al 2 O 3 ) heated to an optimum temperature with a flue gas flowing through the flue gas passage  12 . The hydrogen rich gas is delivered to the converter  3  through the second pipe  52 , and CO 2  and H 2 O are generated from CO generated in the reformer  2  with catalysts such as Fe 2 O 3  and Cr 2 O 3 , or CuO, ZnO, and Al 2 O 3  filled in the converter  3  and heated to an optimum temperature with the flue gas while the hydrogen rich gas flows through the converter  3 . The reformed gas is delivered to the CO remover  4  with injected air through the third pipe  53 , and unreacted CO is converted into CO 2  with a catalyst such as Ru heated to an optimum temperature with the flue gas. A gas consisting of H 2  and CO 2  is delivered to the fuel cell  7  through the fourth pipe  54 , and H 2  is used for power generation in the fuel cell  7 . 
       Embodiment 2 
       [0048]      FIG. 2  is a piping block diagram showing another embodiment of the present invention. In the embodiment shown in  FIG. 2 : a membrane reactor-type reformer  2  is incorporated in the upstream of the heat exchanger  1 ; the first pipe  51  is connected to the inlet side of the reformer  2 ; and the outlet side of the reformer  2  is connected to the fuel cell  7  through an eighth pipe  58 . 
         [0049]      FIG. 3  is a sectional diagram showing a catalyst device used for the membrane reactor-type reformer  2 . A catalyst device  8 A is formed by: inserting a tubular hydrogen separation membrane  84  subjected to palladium plating or the like on a surface of a porous metal pipe into a cylinder  83  having an inlet  81  in an upper part and an outlet  82  of an off gas in a side of a lower part; projecting downwardly a lower outlet  85  of the hydrogen separation membrane  84  from the; and filling a reforming catalyst  86  such as NiO(Al 2 O 3 ) inside the cylinder  83  such that the reforming catalyst  86  surrounds the hydrogen separation membrane  84 . The heat exchanger  1  includes such the catalyst device  8 A incorporated in the reformer  2 . 
         [0050]    As shown in  FIG. 3 , in the hydrogen generator of this embodiment, CH 4  and H 2 O are delivered from the first pipe  51 , through the inlet  81  of the catalyst device  8 A, and into the cylinder  83 , are brought into contact with the reforming catalyst  86  filled inside the cylinder  83 , pass through the hydrogen separation membrane  84 , and convert into H 2 . Thus, H 2  is supplied from the outlet  85  of the catalyst device  8 A to the fuel cell  7  through the eighth pipe  58  for power generation. The off gas (CO, CO 2 , CH 4 ) generated in the catalyst device  8 A is delivered from the outlet  82  of the catalyst device  8 A to downstream of the seventh pipe  57  through a ninth pipe  59 , and is supplied to the inlet side of the heat exchanger  1  together with a gas (unreacted H 2 ) flowing through the seventh pipe  57  and combusted. 
         [0051]      FIG. 4  shows a formation example of a reformer in the case where a cylindrical body is used as the heat exchanger  1 . In this embodiment, a plurality of water pipes  13  are provided inside a cylindrical body  11  on an inner diameter side and an outer diameter side, and the flue gas passage  12  is formed between the water pipes  13  on the inner diameter side and the outer diameter side. One of the water pipes  13  positioned on the outer diameter side is removed, and the reformer  2  formed of a metal pipe  21 , which is different from the water pipe, filled with a hydrogen reforming catalyst is incorporated in this position. 
         [0052]      FIG. 5  is a schematic diagram showing an example employing the same heat exchanger as that of  FIG. 4  and having the reformer  2  provided outside of the cylindrical body  11 . The reformer  2  is connected to the flue gas passage  12  in the cylindrical body  11  through a bypass passage  14 . 
         [0053]      FIG. 6  is a schematic diagram showing a formation example of the reformer  2  in the case where a rectangular body is used as the heat exchanger  1 . In this example, a plurality of water pipes  13  are provided in the fuel gas passage  12  of the rectangular body  11 . The reformer  2  includes the catalyst device  8 A as shown in  FIG. 3  in which a plurality of tubular hydrogen separation membranes  84  are inserted in the cylinder  83 , and a plurality of catalyst devices  8 A are arranged in a width direction of the rectangular body  11  and in an upstream region of the flue gas passages  12 . On both sides of the width direction, different catalyst devices  8 B in which a plurality of tubular hydrogen separation membranes  84  are inserted between metal sheets  87  opposing each other, and a hydrogen reforming catalyst  86  such as NiO(Al 2 O 3 ) is filled between the metal sheets  87  such that the hydrogen reforming catalyst  86  surrounds the tubular hydrogen separation membranes  84  are provided such that hydrogen is generated in two catalyst devices  8 A and  8 B. Alternatively, one of the catalyst devices  8 A and  8 B may be used. 
         [0054]      FIG. 7  is a schematic diagram showing another formation example of the reformer  2  in the case where a rectangular body is used as the heat exchanger  1 . This example employs a catalyst device  8 C in which a metal sheet  88  and a sheet-like hydrogen separation membrane  89  subjected to palladium plating or like on a surface of a porous metal pipe are arranged so as to oppose each other, and the hydrogen separation catalyst  86  is filled between the opposing parts. A plurality of pairs of two catalyst devices  8 C arranged such that respective hydrogen separation membranes  89  oppose each other are arranged in a width direction and in an upstream region of the heat exchanger  1 . In the case where such the catalyst devices  8 C are used, hydrogen passes through sheet-like hydrogen separation membranes  89  opposing each other and is guided out through a passage formed between the hydrogen separation membranes  89  in the catalyst devices  8 C. The hydrogen separation membranes  89  maybe formed into a corrugated shape to increase a surface area, to thereby increase a hydrogen generation rate. 
         [0055]      FIG. 8  is a schematic diagram showing still another formation example of the reformer  2  in the case where a rectangular body is used as a heat exchanger  1 . In this example, a catalyst device  8 D having the hydrogen reforming catalyst  86  such as NiO(Al 2 O 3 ) simply filled inside a metal pipe  90 , or a catalyst device  8 E having the hydrogen reforming catalyst  86  filled between metal sheets  91  opposing each other is arranged in an upstream region of the heat exchanger  1 . Further, a catalyst device  8 F having a plurality of tubular hydrogen separation membranes  93  inserted inside a metal pipe  92  is arranged in a midstream region of the heat exchanger  1 , in addition to the catalyst devices  8 D and  8 E. In this example, hydrogen is generated due to the catalyst device  8 D or  8 E, and the catalyst device  8 F. 
         [0056]      FIG. 9  is a graph showing an inside temperature distribution of a rectangular body serving as a heat exchanger by section, and  FIG. 10  is a graph showing an inside temperature distribution of a cylindrical body serving as a heat exchanger by section. The figures show results of temperature measurement of the flue gas passage in the heat exchanger divided into a plurality of sections from the inlet to the outlet. As the figures show, the rectangular heat exchanger has a temperature range of about 300 to 1,500° C., and the cylindrical heat exchanger has a temperature range of about 300 to 1,200° C. NiO(Al 2 O 3 ) to be used as a hydrogen reforming catalyst in the reformer  2  most effectively functions in a temperature range of 600 to 800° C., and Fe 2 O 3  and Cr 2 O 3  to be used as catalysts in the converter  3  most effectively function in a temperature range of 320 to 400° C. CuO, ZnO, and Al 2 O 3  to be used as catalysts in the converter  3  most effectively function in a temperature range of 180 to 250° C., and Ru to be used as a catalyst in the CO remover  4  most effectively functions in a temperature range of 150 to 200° C. 
         [0057]    Thus, in the fuel cell system as shown in  FIG. 1 , the reformer  2  employing NiO(Al 2 O 3 ) as a catalyst is arranged in an upstream region of the flue gas passage  12  of the heat exchanger  1  at a position having a temperature of about 700° C. The converter  3  employing CuO, ZnO, and Al 2 O 3  as catalysts is arranged in a midstream region of the flue gas passage  12  at a position having a temperature of about 250° C., and the converter  3  employing Fe 2 O 3  and Cr 2 O 3  as catalysts is arranged in a midstream region of the flue gas passage  12  at a position having a temperature of about 350° C. The CO remover  4  employing Ru as a catalyst is arranged in a downstream region of the flue gas passage  12  at a position having a temperature of about 200° C. Those allow the catalysts arranged at respective positions to exhibit respective catalytic abilities efficiently, to thereby improve a hydrogen generation rate. The hydrogen separation membrane most effectively functions at a temperature of about 550° C., and thus the hydrogen separation membrane is arranged in a midstream region of the flue gas passage  12  of the heat exchanger  1  at a position having a temperature of about 550° C. 
         [0058]    In the embodiment shown in  FIG. 1 , the fourth pipe  54  from the CO remover  4  to the fuel cell  7  is provided with a detector  60  such as a sensor for detecting a concentration of hydrogen or carbon dioxide in a gas flowing through the fourth pipe  54 . Further, the seventh pipe  57  is provided with adjusting means  61  for adjusting a gas supply volume from the seventh pipe  57  to the flue gas passage  12  of the heat exchanger  1  based on a detection result of the detector  60 . 
         [0059]    According to the structure described above, the concentration of hydrogen or carbon dioxide in the gas from the CO remover  4  of the hydrogen generator to the fuel cell  7  is detected by the detector  60 , and the gas supply volume to the heat exchanger  1  through the seventh pipe  57  is adjusted by the adjusting means  61  based on the detection result. In this way, in accordance with a state of a fuel in the hydrogen generator, in the case where a large amount of hydrogen is present in the gas from the hydrogen generator, excess hydrogen is supplied to the upstream of the heat exchanger  1  through the seventh pipe  57  for attempting efficient use of energy. Meanwhile, in the case where a large amount of carbon dioxide is present, an NOx amount can be reduced.