Fuel cell device and method for operating fuel cell device

Abstract

A fuel cell single unit including: a fuel cell element in which an anode layer and a cathode layer are formed so as to sandwich an electrolyte layer; a reducing gas supply path for supplying a gas containing hydrogen to the anode layer; an oxidizing gas supply path for supplying a gas containing oxygen to the cathode layer; and an internal reforming catalyst layer, which has a reforming catalyst for steam-reforming a fuel gas, in at least a part of the reducing gas supply path is provided. An external reformer, which has a reforming catalyst for steam-reforming the fuel gas, is provided upstream of the reducing gas supply path, and the fuel gas partially reformed by the external reformer is supplied to the reducing gas supply path.

Claims

1. A fuel cell device comprising: a fuel cell single unit comprising a solid oxide fuel cell element with operating temperature of 650° C. or higher in which an anode layer formed in a thin layer shape and a cathode layer are formed so as to sandwich an electrolyte layer, a reducing gas supply path for supplying a gas containing hydrogen to the anode layer, an oxidizing gas supply path for supplying a gas containing oxygen to the cathode layer, and an internal reforming catalyst layer, which has a reforming catalyst for steam-reforming a hydrocarbon-based raw fuel gas, in at least a part of the reducing gas supply path; an external reformer which has a reforming catalyst for reforming the raw fuel gas and is provided upstream of the reducing gas supply path and outside of the fuel cell single unit; and a control unit configured to control a reforming temperature in the external reformer to be lower than a temperature in the internal reforming catalyst layer provided in the reducing gas supply path, wherein the raw fuel gas partially reformed in the external reformer is supplied to the reducing gas supply path, wherein the fuel cell single unit is configured to include one solid oxide fuel cell element formed in a thin layer shape on a metal support made of a metal material selected from ferritic stainless alloy, austenitic stainless alloy, or an alloy containing chromium, the reducing gas supply path, and the oxidizing gas supply path, wherein the internal reforming catalyst layer for generating at least hydrogen from the raw fuel gas by a steam reforming reaction is included in the fuel cell single unit, wherein a plurality of through-holes penetrating from a front side to a rear side of the metal support are provided by boring processing, wherein the anode layer having a thickness 1 μm to 100 μm is provided on the front side of the metal support, and the reducing gas supply path is provided along the rear side, wherein an internal reforming fuel supply path for discharging steam generated by a power generation reaction from the anode layer to lead the steam to the internal reforming catalyst layer, and to lead at least hydrogen generated in the internal reforming catalyst layer to the anode layer is formed by the through-holes and the reducing gas supply path, and wherein an oxide layer is provided between the metal support and the anode layer to act as a diffusion suppressing layer for suppressing diffusion of the material between the metal support and the anode layer.

2. The fuel cell device according to claim 1, wherein the internal reforming catalyst layer is provided inside at least one of the plurality of through-holes.

3. The fuel cell device according to claim 1, wherein at least one metal separator for partitioning the reducing gas supply path and the oxidizing gas supply path is provided in the fuel cell single unit, and the internal reforming catalyst layer is provided on at least a part of the metal separator on a side of the reducing gas supply path.

4. The fuel cell device according to claim 1, wherein the reforming catalyst contained in the internal reforming catalyst layer is a catalyst in which a metal is supported on a support.

5. The fuel cell device according to claim 1, wherein the reforming catalyst contained in the internal reforming catalyst layer is a catalyst containing Ni.

6. The fuel cell device according to claim 1, wherein a turbulence promotion component for disturbing flow in the reducing gas supply path is provided in the reducing gas supply path.

7. A method for operating the fuel cell device according to claim 1, the method comprising: controlling a reforming temperature in the external reformer to be lower than a temperature in the internal reforming catalyst layer provided in the reducing gas supply path.

8. The method according to claim 7, the method further comprising: performing desulfurization so that a concentration of sulfur contained in the raw fuel gas is 1 vol. ppb or less, and supplying the raw fuel gas to the external reformer.

9. The method according to claim 7, the method further comprising: controlling a steam/carbon ratio (S/C ratio) at an inlet of the external reformer to be within a range of 1.5 to 3.0.

10. The fuel cell device according to claim 1, further comprising: an anode off-gas circulation path for returning an anode off-gas discharged from the reducing gas supply path to the external reformer; and a condenser provided in the anode off-gas circulation path for condensing part of steam contained in the anode off-gas and removing the condensed steam from the anode off-gas circulation path, thereby to adjust a steam partial pressure of the anode off-gas, wherein the steam used for steam reforming in the external reformer serves as the steam returned to the external reformer.

11. The fuel cell device according to claim 10, wherein the control unit regulates the steam/carbon ration (the S/C ration) at the inlet of the external reformer to be within a range of 1.5 to 3.0.

12. The fuel cell device according to claim 1, wherein the internal reforming catalyst layer is provided inside at least one of the plurality of through-holes.

13. The fuel cell device according to claim 1, wherein at least one metal separator for partitioning the reducing gas supply path and the oxidizing gas supply path is provided in the fuel cell single unit, and the internal reforming catalyst layer is provided on at least a part of the metal separator on a side of the reducing gas supply path.

14. The fuel cell device according to claim 1, wherein the reforming catalyst contained in the internal reforming catalyst layer is a catalyst in which a metal is supported on a support.

15. The fuel cell device according to claim 1, wherein the reforming catalyst contained in the internal reforming catalyst layer is a catalyst containing Ni.

16. The fuel cell device according to claim 1, wherein a turbulence promotion component for disturbing flow in the reducing gas supply path is provided in the reducing gas supply path.

17. The fuel cell device according to claim 11, wherein the internal reforming catalyst layer is provided inside at least one of the plurality of through-holes.

18. The fuel cell device according to claim 11, wherein at least one metal separator for partitioning the reducing gas supply path and the oxidizing gas supply path is provided in the fuel cell single unit, and the internal reforming catalyst layer is provided on at least a part of the metal separator on a side of the reducing gas supply path.

19. The fuel cell device according to claim 11, wherein the reforming catalyst contained in the internal reforming catalyst layer is a catalyst in which a metal is supported on a support.

20. The fuel cell device according to claim 11, wherein the reforming catalyst contained in the internal reforming catalyst layer is a catalyst containing Ni.

21. The fuel cell device according to claim 11, wherein a turbulence promotion component for disturbing flow in the reducing gas supply path is provided in the reducing gas supply path.

22. The method according to claim 7, the method further comprising: setting a reforming conversion rate of the raw fuel gas reformed by the external reformer to 30% to 60%.

23. A method for operating the fuel cell device according to claim 10, the method comprising: controlling a reforming temperature in the external reformer to be lower than a temperature in the internal reforming catalyst layer provided in the reducing gas supply path.

24. The method according to claim 23, the method further comprising: performing desulfurization so that a concentration of sulfur contained in the raw fuel gas is 1 vol. ppb or less, and supplying the raw fuel gas to the external reformer.

25. The method according to claim 23, the method further comprising: controlling a steam/carbon ratio (S/C ratio) at an inlet of the external reformer to be within a range of 1.5 to 3.0.

26. The method according to claim 23, the method further comprising: setting a reforming conversion rate of the raw fuel gas reformed by the external reformer to 30% to 60%.

27. A method for operating the fuel cell device according to claim 11, the method comprising: controlling a reforming temperature in the external reformer to be lower than a temperature in the internal reforming catalyst layer provided in the reducing gas supply path.

28. The method according to claim 27, the method further comprising: performing desulfurization so that a concentration of sulfur contained in the raw fuel gas is 1 vol. ppb or less, and supplying the raw fuel gas to the external reformer.

29. The method according to claim 27, the method further comprising: controlling a steam/carbon ratio (S/C ratio) at an inlet of the external reformer to be within a range of 1.5 to 3.0.

30. The method according to claim 27, the method further comprising: setting a reforming conversion rate of the raw fuel gas reformed by the external reformer to 30% to 60%.

Description

BRIEF DESCRIPTION OF DRAWINGS

(1) FIG. 1 is a diagram showing a schematic configuration of a fuel cell device according to a first embodiment.

(2) FIG. 2 is a top view showing a structure of a fuel cell single unit according to the first embodiment.

(3) FIGS. 3(a) and 3(b) are cross-sectional views showing the structure of the fuel cell single unit according to the first embodiment.

(4) FIGS. 4(a) and 4(c) are perspective cross-sectional views showing a structure of a current-collector plate with projections.

(5) FIG. 5 is a cross-sectional view showing a structure of a fuel cell module according to the first embodiment.

(6) FIG. 6 is an explanatory view of a cell reaction and a reforming reaction in the first embodiment.

(7) FIG. 7 is a diagram showing a configuration of a fuel cell device according to a second embodiment.

(8) FIGS. 8(a) and 8(b) are a front view and a plane cross-sectional view, respectively, showing a structure of a fuel cell module according to the second embodiment.

(9) FIG. 9 is a perspective view showing a structure of a fuel cell single unit according to a second embodiment.

(10) FIGS. 10(a)-10(c) are an explanatory view of a process of forming the fuel cell single unit according to the second embodiment.

(11) FIG. 11 is an explanatory view of a cell reaction and a reforming reaction in the second embodiment.

(12) FIG. 12 is a diagram showing a schematic configuration of a fuel cell device according to a third embodiment.

(13) FIG. 13 is a perspective cross-sectional view of a main part of a fuel cell module including a pair of fuel cell single units in the third embodiment.

(14) FIG. 14 is another perspective cross-sectional view of the main part of the fuel cell module including the pair of fuel cell single units in the third embodiment.

(15) FIG. 15 is a graph showing a comparison of power generation efficiency of a fuel cell in a case of performing internal reforming in the fuel cell single unit with power generation efficiency of a fuel cell in a case of not performing the internal reforming.

(16) FIG. 16 is a graph showing a partial pressure of a fuel gas for power generation at an inlet of a fuel cell element in each of a case of performing internal reforming in the fuel cell single unit and a case of not performing the internal reforming.

(17) FIG. 17 is a graph showing a partial pressure of a fuel gas for power generation at an outlet of the fuel cell element in each of the case of performing internal reforming in the fuel cell single unit and the case of not performing the internal reforming.

(18) FIG. 18 is a graph showing a difference in the partial pressures of the fuel gases for power generation between the inlet and the outlet of the fuel cell element in each of the case of performing internal reforming in the fuel cell single unit and the case of not performing the internal reforming.

(19) FIGS. 19(a)-19(c) are a comparative explanatory view showing a disposition configuration of an internal reforming catalyst layer in the fuel cell single unit.

(20) FIG. 20 is a view showing another embodiment of a turbulence promotion component.

(21) FIG. 21 is a view showing another embodiment in which the internal reforming catalyst layer is provided on a surface of the turbulence promotion component.

(22) FIG. 22 is a cross-sectional view of the fuel cell single unit according to the second embodiment, which includes the turbulence promotion component.

DESCRIPTION OF THE INVENTION

(23) Embodiments of the present invention will be described with reference to the drawings.

(24) Hereinafter, as the embodiments of the present invention, a first embodiment, a second embodiment, and a third embodiment will be presented. In the description, for each embodiment, the entirety of a fuel cell device Y adopting each embodiment will be described, and then a fuel cell module M included in the fuel cell device Y and a fuel cell single unit U for constructing the fuel cell module M in a stacked state will be described.

(25) A feature of the first embodiment is in that a fuel cell module M has a disc shape, and the fuel cell module M itself receives supply of a reducing gas and an oxidizing gas to operate as a cell, whereas the second embodiment has a feature in which a fuel cell module M has a substantially rectangular parallelepiped shape, and the fuel cell module M is housed in a housing 10 which houses an external reformer 34 and a vaporizer 33 to operate as a cell. In the third embodiment, a structure basically follows the structure of the first embodiment, and the fuel cell module M, which has a disc shape in the first embodiment, has a square shape. Fuel cell elements R according to the first embodiment and the third embodiment can be very thinly manufactured. On the other hand, a fuel cell element R according to the second embodiment can also be made thicker than the fuel cell element R according to the first embodiment. Needless to say, the fuel cell element R according to the second embodiment may be made relatively thin.

(26) Providing an internal reforming catalyst layer D in the fuel cell single unit U and providing the external reformer 34, which are the features of the present invention, are common to all the embodiment.

First Embodiment

(27) FIG. 1 shows a configuration of the fuel cell device Y according to this embodiment.

(28) <Fuel Cell Device>

(29) The fuel cell device Y is a so-called “cogeneration system”, which is capable of generating and supplying both electric power and heat. The electric power is output via an inverter 38, and as the heat, heat held by an exhaust gas can be recovered as warm water and utilized by a heat exchanger 36. The inverter 38 converts, for example, a direct current of the fuel cell module M into electric power having the same voltage and the same frequency as those of electric power received from a commercial system (not shown), and outputs the electric power. A control unit 39 appropriately controls the inverter 38, and also controls operations of respective machines configuring the fuel cell device Y.

(30) The fuel cell device Y includes a boost pump 30, a desulfurizer 31, a reforming water tank 32, the vaporizer 33, and the external reformer 34, as a main machine for supplying a reducing gas to the fuel cell module M, which is responsible for power generation. A main machine for supplying an oxidizing gas is a blower 35, and the blower 35 is capable of sucking an air to supply an oxidizing gas containing oxygen.

(31) A supply system (this system serves as a fuel supply unit in the fuel cell device) of the reducing gas will be further described. A hydrocarbon-based raw fuel gas such as a city gas (a gas which contains methane as a main component, and also contains ethane, propane, butane, and the like) is sucked and boosted by the boost pump 30, and sent to the fuel cell module M. Since the city gas contains a sulfur compound component, it is necessary to remove (desulfurize) the sulfur compound component in the desulfurizer 31. A copper-zinc-based desulfurizing agent is stored in the desulfurizer 31, and a sulfur component contained in the raw fuel gas is reduced so that a content of the sulfur is 1 vol. ppb or less (more preferably 0.1 vol. ppb or less). As this type of copper-zinc-based desulfurizing agent, a desulfurizing agent obtained by hydrogen reduction of a copper oxide-zinc oxide mixture prepared by a coprecipitation method using a copper compound (for example, copper nitrate, copper acetate, or the like) and a zinc compound (for example, zinc nitrate, zinc acetate, or the like), or a desulfurizing agent obtained by hydrogen reduction of a copper oxide-zinc oxide-aluminum oxide mixture prepared by a coprecipitation method using a copper compound, a zinc compound, and an aluminum compound (for example, aluminum nitrate, sodium aluminate, or the like) can be typically used.

(32) The desulfurized raw fuel gas is mixed with reforming water supplied from the reforming water tank 32 on a latter stage side of the vaporizer 33, and water becomes steam in the vaporizer 33. The raw fuel gas and the steam are sent to the external reformer 34, and the raw fuel gas is steam-reformed. The steam reforming reaction is a reaction by a reforming catalyst stored in the reformer, and similarly to an internal reforming reaction described later, a part of a hydrocarbon-based raw fuel gas (for example, methane) is reformed, and gas (reformed gas) containing at least hydrogen is generated and provided for power generation.

(33) The reforming by the external reformer 34 does not reform the entire raw fuel gas, but reforms the raw fuel gas at an appropriate ratio. Therefore, in the present invention, a gas, which is sent to an anode layer A configuring the fuel cell element R included in the fuel cell module M, is a mixed gas of the raw fuel gas (the gas which is not yet reformed) and the reformed gas. The reformed gas contains hydrogen and carbon monoxide, which are the fuel gases for power generation described above. The mixed gas is supplied to a reducing gas supply path L1 included in the fuel cell single unit U.

(34) More specifically, as shown in FIGS. 3 and 4, the reducing gas supply path L1 for supplying a gas containing hydrogen for power generation to the anode layer A is provided, the mixed gas (containing the raw fuel gas (the gas which is not yet reformed) and the reformed gas) is supplied to the reducing gas supply path L1, and at least hydrogen contained in the mixed gas is used in the fuel cell reaction in the fuel cell element R. An exhaust gas containing residual hydrogen, which has not been used in the reaction, is discharged from the fuel cell single unit U.

(35) As described above, the heat exchanger 36 exchanges heat between the exhaust gas from the fuel cell module M and the supplied cold water to generate warm water. The heat exchanger 36 serves as an exhaust heat utilization unit of the fuel cell device Y. Instead of the exhaust heat utilization form, a form in which the exhaust gas discharged from the fuel cell module M is utilized for heat generation may be used. That is, the exhaust gas contains residual hydrogen and carbon monoxide, which have not been used in the reaction in the fuel cell single unit U, and raw fuel gas, and thus heat generated by combustion of these combustible gases can be utilized. In the second embodiment described later, residual combustion components are utilized, as a fuel, for heating the external reformer 34 and the vaporizer 33.

(36) <Fuel Cell Single Unit>

(37) FIGS. 2 and 3 show a top view and a cross-sectional view of the fuel cell single unit U according to the present embodiment.

(38) The fuel cell single unit U is configured to include the fuel cell element R formed on a metal support 1, and a metal separator (current-collector plate 3 with projections) bonded to a side opposite to the fuel cell element R. The metal support 1 in the present embodiment has a disc shape, the fuel cell element R is configured to include at least the anode layer A, an electrolyte layer B, and a cathode layer C, and is formed and disposed on a front side 1e of the metal support 1, and the electrolyte layer B is sandwiched between the anode layer A and the cathode layer C. When the fuel cell element R is formed on the front side 1e of the metal support 1, the metal separator 3 is positioned on a rear side 1f of the metal support 1. That is, the fuel cell element R and the metal separator 3 are positioned so as to sandwich the metal support 1.

(39) When the fuel cell single unit U includes the fuel cell element R and metal separator 3 formed on the metal support 1 as described above, a gas containing at least hydrogen is supplied to the anode layer A through the reducing gas supply path L1, a gas containing oxygen is supplied to the cathode layer C through an oxidizing gas supply path L2, and thus power can be generated. Moreover, as a structural feature of the fuel cell single unit U, a metal oxide layer x is provided on the front side 1e of the metal support 1, an intermediate layer y is provided on a surface (including an interface between the anode layer A and the electrolyte layer B covering the anode layer A) of the anode layer A, and a reaction preventing layer z is provided on a surface (including an interface between the electrolyte layer B and the cathode layer C covering the electrolyte layer B) of the electrolyte layer B. The metal oxide layer x, the intermediate layer y, and the reaction preventing layer z are layers provided for suppressing diffusion of constituent materials between material layers sandwiching these layers x, y, and z, and are shown in FIG. 6 for easier understanding.

(40) <Metal Support>

(41) The metal support 1 is a flat plate which is made of a metal and has a disc shape.

(42) As is also clear from FIGS. 2 and 3, an opening part 1b concentric with the metal support 1 is formed in a center of the metal support 1. In the metal support 1, a plurality of through-holes 1a penetrating the front side 1e and the rear side 1f are formed. A gas can flow between the front side 1e and the rear side 1f of the metal support 1 through the through-hole 1a. The gas flowing through the through-hole 1a is specifically the reformed gas (containing hydrogen H.sub.2) described above, and steam H.sub.2O generated by the power generation reaction in the fuel cell element R (see FIG. 6).

(43) As a material for the metal support 1, a material having excellent electron conductivity, heat resistance, oxidation resistance, and corrosion resistance is used. For example, ferritic stainless alloy, austenitic stainless alloy, a nickel-based alloy, or the like is used. In particular, an alloy containing chromium is suitably used. In the present embodiment, a Fe—Cr-based alloy containing 18% by mass to 25% by mass of Cr is used for the metal support 1, but a Fe—Cr-based alloy containing 0.05% by mass or greater of Mn, a Fe—Cr-based alloy containing 0.15% by mass to 1.0% by mass of Ti, a Fe—Cr-based alloy containing 0.15% by mass to 1.0% by mass of Zr, a Fe—Cr-based alloy containing Ti and Zr and having a total content of Ti and Zr of 0.15% by mass to 1.0% by mass, and a Fe—Cr-based alloy containing 0.10% by mass to 1.0% by mass of Cu are particularly suitable.

(44) The metal support 1 has a plate shape as a whole. Moreover, in the metal support 1, a surface on which the anode layer A is provided is the front side 1e, and the plurality of through-holes 1a penetrating from the front side 1e to the rear side 1f are provided. The through-hole 1a has a function of allowing a gas to permeate from the rear side 1f to the front side 1e of the metal support 1. Furthermore, by bending the plate-shaped metal support 1, for example, the plate-shaped metal support 1 can also be deformed in a shape such as a box shape and a cylindrical shape and used.

(45) The metal oxide layer x as a diffusion suppressing layer is provided on the surface of the metal support 1 (see FIG. 6). That is, the diffusion suppressing layer is formed between the metal support 1 and the anode layer A described later. The metal oxide layer x is provided not only on the surface of the metal support 1 which is exposed to the outside but also on a contact surface (interface) with the anode layer A. Moreover, the metal oxide layer x can also be provided on an inner surface of the through-hole 1a. Element interdiffusion between the metal support 1 and the anode layer A can be suppressed by the metal oxide layer x. For example, when ferritic stainless containing chromium is used for the metal support 1, the metal oxide layer x mainly contains a chromium oxide. Furthermore, diffusion of an chromium atom or the like of the metal support 1 into the anode layer A or the electrolyte layer B is suppressed by the metal oxide layer x which contains a chromium oxide as a main component. The thickness of the metal oxide layer x may be any thickness as long as both a high diffusion preventing performance and low electric resistance are achieved.

(46) The metal oxide layer x can be form by various methods, but a method for oxidizing the surface of the metal support 1 to form a metal oxide is suitably utilized. Moreover, on the surface of the metal support 1, the metal oxide layer x may be formed by a spray coating method (a method such as a thermal spraying method, an aerosol deposition method, an aerosol gas deposition method, a powder jet deposition method, a particle jet deposition method, and a cold spraying method), a PVD method such as a sputtering method and a PLD method, a CVD method, or the like, and may be formed by plating and an oxidation treatment. Furthermore, the metal oxide layer x may contain a spinel phase having high conductivity.

(47) When a ferritic stainless material is used for the metal support 1, a thermal expansion coefficient of the metal support 1 is close to that of yttria-stabilized zirconia (YSZ) or gadolinium-doped ceria (GDC, also referred to as CGO) used as a material for the anode layer A or the electrolyte layer B. Therefore, even when a temperature cycle of a low temperature and a high temperature is repeated, the fuel cell element R is less likely to be damaged. Accordingly, a fuel cell element R having excellent long-term durability can be obtained, which is preferable.

(48) As also described above, the metal support 1 has the plurality of the through-holes 1a provided so as to penetrate the front side 1e and the rear side 1f. Furthermore, for example, the through-hole 1a can be provided in the metal support 1 by mechanical, chemical, or optical boring processing. As also shown in (b) of FIG. 3, the through-hole 1a substantially has a tapered shape in which the front side 1e of the metal support 1 is narrow. The through-hole 1a has a function of allowing a gas to permeate from both the front and rear sides of the metal support 1. In order to impart gas permeability to the metal support 1, it is also possible to use a porous metal. For example, for the metal support 1, a sintered metal, a foamed metal, or the like can also be used.

(49) <Fuel Cell Element>

(50) As also described above, the fuel cell element R is configured to have: the anode layer (anode electrode layer) A; the electrolyte layer B; the cathode layer (cathode electrode layer) C; and the intermediate layer y and the reaction preventing layer z, which are appropriately provided between these layers. The fuel cell element R is a solid oxide fuel cell SOFC. As described above, the fuel cell element R shown as the embodiment includes the intermediate layer y and the reaction preventing layer z, and thus the electrolyte layer B is indirectly sandwiched between the anode layer A and the cathode layer C. From the viewpoint that only cell power generation is caused, power can be generated by forming the anode layer A on one surface of the electrolyte layer B, and forming the cathode layer C on the other surface.

(51) <Anode Layer>

(52) As shown in FIGS. 3 and 6 or the like, the anode layer A can be provided as a thin layer in a region which is on the front side 1e of the metal support 1 and is larger than a region where the through-holes 1a are provided. In a case of being provided as a thin layer, a thickness thereof can be, for example, about 1 μm to 100 μm and preferably 5 μm to 50 μm. When the thickness is set as described above, a sufficient electrode performance can be ensured while reducing a cost by reducing a used amount of an expensive material for the electrode layer. The entire region where the through-holes 1a are provided is covered with the anode layer A. That is, the through-hole 1a is formed inside a region of the metal support 1 where the anode layer A is formed. In other words, all the through-holes 1a are provided so as to face the anode layer A.

(53) As a material for the anode layer A, for example, a composite material such as NiO-GDC, Ni-GDC, NiO-YSZ, Ni-YSZ, CuO—CeO.sub.2, and Cu—CeO.sub.2 can be used. In these examples, GDC, YSZ, and CeO.sub.2 can be referred to as a composite aggregate.

(54) In addition, the anode layer A is preferably formed by a low-temperature calcination method (for example, a wet method using a calcination treatment in a low-temperature range without performing a calcination treatment in a high-temperature range of higher than 1,100° C.), a spray coating method (a method such as a thermal spraying method, an aerosol deposition method, an aerosol gas deposition method, a powder jet deposition method, a particle jet deposition method, and a cold spraying method), a PVD method (a sputtering method, a pulsed laser deposition method, or the like), a CVD method, or the like. By these processes which can be used in a low-temperature range, a favorable anode layer A can be obtained without using calcination in a high-temperature range of higher than 1,100° C., for example. For the reason, the element interdiffusion between the metal support 1 and the anode layer A can be suppressed without damaging the metal support 1, and an electrochemical element having excellent durability can be obtained, which is preferable. Moreover, using the low-temperature calcination method is more preferable because handling of raw materials becomes easy.

(55) Furthermore, an amount of Ni contained in the anode layer A can be in a range of 35% by mass to 85% by mass. Moreover, the amount of Ni contained in the anode layer A is more preferably greater than 40% by mass and still more preferably greater than 45% by mass because a power generation performance can be further enhanced. On the other hand, the amount of Ni is more preferably 80% by mass or less because a cost is easily reduced.

(56) The anode layer A has a plurality of pores (not shown) inside and on the surface thereof so as to have gas permeability. That is, the anode layer A is formed as a porous layer. The anode layer A is formed, for example, so that the denseness is 30% or greater and less than 80%. As a size of the pore, a size suitable for allowing an electrochemical reaction to smoothly proceed during the reaction can be appropriately selected. Moreover, the denseness is a proportion of a material constituting a layer to a space, can be expressed as (1−porosity), and is equivalent to a relative density.

(57) (Intermediate Layer)

(58) As shown in FIG. 6, the intermediate layer y can be formed as a thin layer on the anode layer A in a state of covering the anode layer A. In a case of being provided as a thin layer, a thickness thereof can be, for example, about 1 μm to 100 μm, preferably about 2 μm to 50 μm, and more preferably about 4 μm to 25 μm. When the thickness is set as described above, a sufficient performance can be ensured while reducing a cost by reducing a used amount of an expensive material for the intermediate layer. As a material for the intermediate layer y, for example, yttria-stabilized zirconia (YSZ), scandia-stabilized zirconia (SSZ), gadolinium-doped ceria (GDC), yttrium-doped ceria (YDC), samarium-doped ceria (SDC), or the like can be used. In particular, ceria-based ceramics are suitably used.

(59) The intermediate layer y is preferably formed by a low-temperature calcination method (for example, a wet method using a calcination treatment in a low-temperature range without performing a calcination treatment in a high-temperature range of higher than 1,100° C.), a spray coating method (a method such as a thermal spraying method, an aerosol deposition method, an aerosol gas deposition method, a powder jet deposition method, a particle jet deposition method, and a cold spraying method), a PVD method (a sputtering method, a pulsed laser deposition method, or the like), a CVD method, or the like. By these film formation processes which can be used in a low-temperature range, the intermediate layer y can be obtained without using calcination in a high-temperature range of higher than 1,100° C., for example. For the reason, the element interdiffusion between the metal support 1 and the anode layer A can be suppressed without damaging the metal support 1, and a fuel cell element R having excellent durability can be obtained. Moreover, using the low-temperature calcination method is more preferable because handling of raw materials becomes easy.

(60) The intermediate layer y has oxygen ion (oxide ion) conductivity. Moreover, the intermediate layer y more preferably has mixed conductivity of an oxygen ion (oxide ion) and an electron. The intermediate layer y having these properties is suitable for application to the fuel cell element R.

(61) (Electrolyte Layer)

(62) The electrolyte layer B is formed as a thin layer on the intermediate layer y in a state of covering the anode layer A and the intermediate layer y. Moreover, the electrolyte layer can also be formed as a thin layer having a thickness of 10 μm or less. Specifically, as shown in FIGS. 3 and 6 or the like, the electrolyte layer B is provided over (straddling) the intermediate layer y and the metal support 1. With such a configuration, by bonding the electrolyte layer B to the metal support 1, the electrochemical element as a whole can have excellent fastness properties.

(63) In addition, the electrolyte layer B is provided in a region which is on the front side 1e of the metal support 1 and is larger than a region where the through-holes 1a are provided. That is, the through-hole 1a is formed inside a region of the metal support 1 where the electrolyte layer B is formed.

(64) Furthermore, at the periphery of the electrolyte layer B, gas leakage from the anode layer A and the intermediate layer y can be suppressed. Specifically, during power generation, gas is supplied to the anode layer A from the rear side of the metal support 1 through the through-hole 1a. At a site where the electrolyte layer B is in contact with the metal support 1, gas leakage can be suppressed without providing a separate member such as a gasket. Moreover, in the present embodiment, the electrolyte layer B covers the entire periphery of the anode layer A, but a configuration in which the electrolyte layer B is provided on an upper part of the anode layer A and the intermediate layer y, and a gasket or the like is provided at the periphery may be adopted.

(65) As a material for the electrolyte layer B, yttria-stabilized zirconia (YSZ), scandia-stabilized zirconia (SSZ), gadolinium-doped ceria (GDC), yttrium-doped ceria (YDC), samarium-doped ceria (SDC), strontium- and magnesium-doped lanthanum gallate (LSGM), or the like can be used. In particular, zirconia-based ceramics are suitably used. When the electrolyte layer B is made of the zirconia-based ceramics, an operating temperature of SOFC using the fuel cell element R can be made higher than that in a case of ceria-based ceramics. When SOFC is used, and a system configuration in which a material, such as YSZ, which can exhibit a high electrolyte performance even in a high-temperature range of about 650° C. or higher is used as the material for the electrolyte layer B, a hydrocarbon-based raw fuel such as a city gas and LPG is used as a raw fuel of the system, and the raw fuel is steam-reformed to become a reducing gas of SOFC is adopted, it is possible to construct a high-efficiency SOFC system in which heat generated in a cell stack of SOFC is used for reforming the raw fuel gas.

(66) The electrolyte layer B is preferably formed by a low-temperature calcination method (for example, a wet method using a calcination treatment in a low-temperature range without performing a calcination treatment in a high-temperature range of higher than 1,100° C.), a spray coating method (a method such as a thermal spraying method, an aerosol deposition method, an aerosol gas deposition method, a powder jet deposition method, a particle jet deposition method, and a cold spraying method), a PVD method (a sputtering method, a pulsed laser deposition method, or the like), a CVD method, or the like. By these film formation processes which can be used in a low-temperature range, an electrolyte layer B which is dense and has high gastightness and gas barrier properties can be obtained without using calcination in a high-temperature range of higher than 1,100° C., for example. For the reason, the damage of the metal support 1 can be suppressed, the element interdiffusion between the metal support 1 and the anode layer A can be suppressed, and the fuel cell element R which is excellent in a performance and durability can be obtained. In particular, using a low-temperature calcination method, a spray coating method, or the like is preferable because a low-cost element can be obtained. Furthermore, using the spray coating method is more preferable because the electrolyte layer which is dense and has high gastightness and gas barrier properties can be easily obtained in a low-temperature range.

(67) The electrolyte layer B is densely configured so as to shield a gas such as a reducing gas or an oxidizing gas from being leaked and exhibit high ionic conductivity. A denseness of the electrolyte layer B is preferably 90% or greater, more preferably 95% or greater, and still more preferably 98% or greater. When the electrolyte layer B is a uniform layer, the denseness thereof is preferably 95% or greater and more preferably 98% or greater. Moreover, when the electrolyte layer B is formed in a form of a plurality of layers, at least some of these layers preferably include a layer (dense electrolyte layer) having a denseness of 98% or greater, and more preferably include a layer (dense electrolyte layer) having a denseness of 99% or greater. This is because when such a dense electrolyte layer is included in a part of the electrolyte layer, the electrolyte layer which is dense and has high gastightness and gas barrier properties can be easily formed even in a case where the electrolyte layer is formed in a form of a plurality of layers.

(68) (Reaction Preventing Layer)

(69) The reaction preventing layer z can be formed as a thin layer on the electrolyte layer B. In a case of being provided as a thin layer, a thickness thereof can be, for example, about 1 μm to 100 μm, preferably about 2 μm to 50 μm, and more preferably about 3 μm to 15 μm. When the thickness is set as described above, a sufficient performance can be ensured while reducing a cost by reducing a used amount of an expensive material for the reaction preventing layer. A material for the reaction preventing layer z may be any material as long as the material can prevent a reaction between the components of the electrolyte layer B and the components of the cathode layer C, but for example, a ceria-based material or the like is used. Moreover, as the material for the reaction preventing layer z, a material containing at least one element selected from the group consisting of Sm, Gd, and Y is suitably used. Furthermore, the material may contain at least one element selected from the group consisting of Sm, Gd, and Y, and a total content ratio of these elements may be 1.0% by mass to 10% by mass. By introducing the reaction preventing layer z between the electrolyte layer B and the cathode layer C, a reaction between the constituent materials of the cathode layer C and the constituent materials of the electrolyte layer B can be effectively suppressed (diffusion suppression), and long-term stability of the performance of the fuel cell element R can be improved. Forming the reaction preventing layer z by appropriately using a method in which the reaction preventing layer z can be formed at a treatment temperature of 1,100° C. or lower is preferable because the damage of the metal support 1 can be suppressed, the element interdiffusion between the metal support 1 and the anode layer A can be suppressed, and the fuel cell element R which is excellent in a performance and durability can be obtained. For example, the formation can be performed by appropriately using a low-temperature calcination method (for example, a wet method using a calcination treatment in a low-temperature range without performing a calcination treatment in a high-temperature range of higher than 1,100° C.), a spray coating method (a method such as a thermal spraying method, an aerosol deposition method, an aerosol gas deposition method, a powder jet deposition method, a particle jet deposition method, and a cold spraying method), a PVD method (a sputtering method, a pulsed laser deposition method, or the like), a CVD method, or the like. In particular, using a low-temperature calcination method, a spray coating method, or the like is preferable because a low-cost element can be obtained. Moreover, using the low-temperature calcination method is more preferable because handling of raw materials becomes easy.

(70) (Cathode Layer)

(71) The cathode layer C can be formed as a thin layer on the electrolyte layer B or the reaction preventing layer z. In a case of being provided as a thin layer, a thickness thereof can be, for example, about 1 μm to 100 μm and preferably 5 μm to 50 μm. When the thickness is set as described above, a sufficient electrode performance can be ensured while reducing a cost by reducing a used amount of an expensive material for the cathode layer. As a material for the cathode layer C, for example, a complex oxide such as LSCF and LSM, a ceria-based oxide, and a mixture thereof can be used. In particular, the cathode layer C preferably contains a perovskite-type oxide containing two or more elements selected from the group consisting of La, Sr, Sm, Mn, Co, and Fe. The cathode layer C formed of the above materials functions as a cathode.

(72) In addition, forming the cathode layer C by appropriately using a method in which the cathode layer C can be formed at a treatment temperature of 1,100° C. or lower is preferable because the damage of the metal support 1 can be suppressed, the element interdiffusion between the metal support 1 and the anode layer A can be suppressed, and the fuel cell element R which is excellent in a performance and durability can be obtained. For example, the formation can be performed by appropriately using a low-temperature calcination method (for example, a wet method using a calcination treatment in a low-temperature range without performing a calcination treatment in a high-temperature range of higher than 1,100° C.), a spray coating method (a method such as a thermal spraying method, an aerosol deposition method, an aerosol gas deposition method, a powder jet deposition method, a particle jet deposition method, and a cold spraying method), a PVD method (a sputtering method, a pulsed laser deposition method, or the like), a CVD method, or the like. In particular, using a low-temperature calcination method, a spray coating method, or the like is preferable because a low-cost element can be obtained. Moreover, using the low-temperature calcination method is more preferable because handling of raw materials becomes easy.

(73) In the fuel cell single unit U, electrical conduction properties between the metal support 1 and the anode layer A are ensured. Moreover, an insulating coating film may be formed on a required portion of the surface of the metal support 1, as needed.

(74) <Power Generation in Fuel Cell Element>

(75) The fuel cell element R receives supply of both a reducing gas containing hydrogen and an oxidizing gas containing oxygen to generate power. As described above, by supplying both the gases to respective electrode layers (the anode layer A and the cathode layer C) of the fuel cell element R, as shown in FIG. 6, in the cathode layer C, an oxygen molecule O.sub.2 reacts with an electron e.sup.− to generate an oxygen ion O.sup.2−. The oxygen ion O.sup.2− moves to the anode layer A through the electrolyte layer B. In the anode layer A, each of (hydrogen H.sub.2 and carbon monoxide CO), which are the fuel gas for power generation, reacts with an oxygen ion O.sup.2− to generate steam H.sub.2O, carbon dioxide CO.sub.2, and an electron e.sup.−. By the above reaction, an electromotive force is generated between the anode layer A and the cathode layer C to perform power generation. The power generation principle is the same also in the second embodiment (see FIG. 11).

(76) Hereinafter, a structure for supplying the reducing gas and the oxidizing gas will be described, and a configuration relating to internal reforming unique to the present invention will be described.

(77) As shown in FIG. 3, the fuel cell single unit U is configured to include the current-collector plate 3 with projections as a metal separator. As shown in (a) of FIG. 4, the current-collector plate 3 with projections is a plate which is made of a metal and has a disc shape, has a concave-convex structure site 3a including one or more concave portions or convex portions, is disposed so as to face the rear side 1f of the metal support 1, and is bonded to the metal support 1 via a bonding site W. The concave-convex structure site 3a is connected to the cathode layer C of another fuel cell single unit U when the plurality of the fuel cell single units U are stacked. Therefore, the current-collector plate 3 with projections is electrically connected to the metal support 1, and further to the anode layer A. In the current-collector plate 3 with projections, a gas does not flow between front and back thereof. As will be described later, a metal support 1 side (in other words, an anode layer A side) of the current-collector plate 3 with projections can be the reducing gas supply path L1 described above, and a rear side (a side spaced from the metal support 1) thereof can be the oxidizing gas supply path L2 described above.

(78) The supply and the discharge of these gases will be described below.

(79) The fuel cell single unit U includes a gas supply pipe 2.

(80) The gas supply pipe 2 separately supplies the reducing gas and the oxidizing gas to spaces (each serving as a supply path through which a gas flows outward in a radial direction) formed above and below the current-collector plate 3 with projections. The gas supply pipe 2 is a member which is made of a metal and has a cylindrical shape, and is inserted into the opening part 1b of the metal support 1 in a state where a central axis Z of the gas supply pipe 2 is aligned with a central axis Z of the metal support 1 and fixed by welding. Moreover, the metal support 1 may be biased against the gas supply pipe 2 with a seal material sandwiched therebetween. As a material for the gas supply pipe 2, the same material as that for the metal support 1 described above can be used. Furthermore, forming a diffusion preventive layer, which is the same as that for the metal support 1, on a surface of the gas supply pipe 2 is suitable because Cr scattering can be suppressed.

(81) In addition, the gas supply pipe 2 may have a sufficient strength for configuring the fuel cell single unit U and the fuel cell module M described later. Moreover, a sintered metal, a foamed metal, or the like can also be used for the gas supply pipe 2, but in this case, a treatment such as surface coating may be applied in order to prevent gas permeation.

(82) The gas supply pipe 2 has a partition wall 2a which is disposed inside thereof in parallel with the central axis Z, and is partitioned into a first flow path 2b and a second flow path 2c. The first flow path 2b and the second flow path 2c have a form in which a gas does not flow between both flow paths so that different gases can flow through the respective flow paths.

(83) A first flow hole 2d and a second flow hole 2e, which penetrate the inside and the outside, are formed in the gas supply pipe 2. The first flow hole 2d connects a space (serving as the reducing gas supply path L1 of the present invention) between the metal support 1 and the current-collector plate 3 with projections to the first flow path 2b so that a gas can flow between the both. The second flow hole 2e connects a space (serving as the oxidizing gas supply path L2 of the present invention) on a side opposite to the metal support 1 with respect to the current-collector plate 3 with projections to the second flow path 2c so that a gas can flow between the both. The first flow hole 2d and the second flow hole 2e are formed at different positions in a direction along the central axis Z of the gas supply pipe 2, and are formed on both sides of the current-collector plate 3 with projections sandwiched therebetween.

(84) Therefore, in the present embodiment, the first flow path 2b is connected to the reducing gas supply path L1 formed on an upper side of the current-collector plate 3 with projections, and the second flow path 2c is connected to the oxidizing gas supply path L2 formed on a lower side of the current-collector plate 3 with projections.

(85) As shown in FIG. 4, in the current-collector plate 3 with projections, a plurality of the concave-convex structure sites 3a are formed so as to project in a vertical direction from a disc surface of the current-collector plate 3 with projections. The concave-convex structure site 3a has a vertex having a gentle conical shape.

(86) As shown in FIG. 3, the current-collector plate 3 with projections is disposed so as to face the rear side 1f of the metal support 1, and is bonded to the metal support 1 via the bonding site W. For example, the current-collector plate 3 with projections can be directly biased against and bonded to the metal support 1, but in this case, a portion where the vertex of the concave-convex structure site 3a and the metal support 1 contact each other serves as the bonding site W. Moreover, the current-collector plate 3 with projections can be biased against and bonded to the metal support 1 with the bonding site W which is formed by applying a ceramic paste or the like having excellent conductivity to the vertex of the concave-convex structure site 3a, or the current-collector plate 3 with projections can be biased against and bonded to the metal support 1 with a metal felt or the like which is sandwiched between the current-collector plate 3 with projections and the metal support 1. Alternatively, the current-collector plate 3 with projections and the metal support 1 can be boned to each other while forming the bonding site W by brazing a part or the whole of the vertex of the concave-convex structure site 3a. In addition, the current-collector plate 3 with projections is disposed so that the gas supply pipe 2 passes through an opening part 3b. The current-collector plate 3 with projections and the gas supply pipe 2 are bonded to each other by welding at the periphery of the opening part 3b. Furthermore, the current-collector plate 3 with projections may be biased against the gas supply pipe 2 with a seal material sandwiched therebetween.

(87) As a material for the current-collector plate 3 with projections, the same material as that for the metal support 1 described above can be used. Moreover, forming a diffusion preventive layer, which is the same as that for the metal support 1, on a surface of the current-collector plate 3 with projections is suitable because Cr scattering can be suppressed. The current-collector plate 3 with projections configured as described above can be manufactured at a low cost by press molding or the like. Furthermore, the current-collector plate 3 with projections is made of a material, which does not allow a gas to permeate, so that a gas cannot flow between the front side 1e and the rear side 1f.

(88) With this structure, the current-collector plate 3 with projections as the metal separator is electrically connected to the anode layer A, which configures the fuel cell element R, via metal support 1. As will be described later, in a state where the fuel cell single units U are stacked to form the fuel cell module M, the current-collector plate 3 with projections is also electrically connected to the cathode layer C.

(89) The current-collector plate 3 with projections may have a sufficient strength for configuring the fuel cell single unit U and the fuel cell module M described later, and the current-collector plate 3 with projections having a thickness of, for example, about 0.1 mm to 2 mm, preferably about 0.1 mm to 1 mm, and more preferably about 0.1 mm to 0.5 mm can be used. Moreover, in addition to the metal plate, a sintered metal, a foamed metal, or the like can also be used for the current-collector plate 3 with projections, but in this case, a treatment such as surface coating may be applied in order to prevent gas permeation.

(90) <Gas Supply>

(91) As described above, the current-collector plate 3 with projections has the concave-convex structure site 3a, and the vertex of the concave-convex structure site 3a is bonded to the rear side 1f of the metal support 1. In the structure, a disc-shaped (doughnut-shaped) space (the reducing gas supply path L1) which is axisymmetric with respect to the central axis Z is formed between the metal support 1 and the current-collector plate 3 with projections. A reducing gas is supplied to the supply path L1 from the first flow path 2b through the first flow hole 2d of the gas supply pipe 2. As a result, the reducing gas is supplied to the through-hole 1a of the metal support 1 and then to the anode layer A.

(92) Similarly, by bonding the vertex of the concave-convex structure site 3a of the current-collector plate 3 with projections to the cathode layer C of the fuel cell single unit U positioned on the lower side, a space (the oxidizing gas supply path L2) in which a gas can be supplied to the cathode layer C through the second flow hole 2e of the gas supply pipe 2 is formed.

(93) Hereinbefore, the basic configuration of the fuel cell according to the present invention has been described, but hereinafter, the feature configurations of the present invention will be described mainly with reference to FIGS. 5 and 6.

(94) As also described above, in the present embodiment, the reducing gas supply path L1 for supplying a gas containing hydrogen to the anode layer A is formed between the current-collector plate 3 with projections and the metal support 1. Moreover, as also indicated by an arrow in FIG. 5, the gas flowing through the supply path L1 is directed in one direction from the side of the gas supply pipe 2 positioned on a center side of the disc to a radially outward side. Furthermore, hydrogen for a power generation reaction can be supplied to the anode layer A through the through-hole 1a, which is provided so as to penetrate the front and rear of the metal support 1.

(95) Here, the power generation reaction in the fuel cell element R is as described above, but due to the reaction, steam H.sub.2O is released from the anode layer A to the through-hole 1a and the reducing gas supply path L1. As a result, the reducing gas supply path L1 of the present invention serves as a supply unit for supplying a gas containing hydrogen H.sub.2 to the anode layer A, and also serves as a discharge destination of steam H.sub.2O.

(96) Therefore, in the present invention, as shown in FIGS. 5 and 6, the internal reforming catalyst layer D is provided on the surface (the surface on the metal support 1 side) of the current-collector plate 3 with projections on the side of the reducing gas supply path L1.

(97) As also described above, in addition to hydrogen H.sub.2 obtained by external reforming, a raw fuel gas (the gas which is not yet reformed: in the illustrated example, methane CH.sub.4) to be reformed flows through the reducing gas supply path L1, but by returning steam H.sub.2O generated in the anode layer A to the reducing gas supply path L1, the steam H.sub.2O can flow into the supply path L1 to reform a fuel gas CH.sub.4. Needless to say, the generated hydrogen H.sub.2 or carbon monoxide CO can be supplied to the anode layer A through the through-hole 1a on a downstream side, and provided for power generation.

(98) As a material for the internal reforming catalyst layer D, for example, a large number of ceramic-made porous granular materials holding a reforming catalyst such as nickel, ruthenium, and platinum can be formed in an air-permeable state.

(99) In addition, when the internal reforming catalyst layer D contains Ni, a content of Ni can be in a range of 0.1% by mass to 50% by mass. Moreover, the content of Ni when the internal reforming catalyst layer D contains Ni is more preferably 1% by mass or greater and still more preferably 5% by mass or greater. This is because a higher internal reforming performance can be obtained by setting the content as described above. On the other hand, the content of Ni when the internal reforming catalyst layer D contains Ni is more preferably 45% by mass or less and still more preferably 40% by mass or less. This is because the cost of the fuel cell device can be further reduced by setting the content as described above. Moreover, it is also preferable to carry Ni on a support.

(100) Furthermore, the internal reforming catalyst layer D is preferably formed by a low-temperature calcination method (for example, a wet method using a calcination treatment in a low-temperature range without performing a calcination treatment in a high-temperature range of higher than 1,100° C.), a spray coating method (a method such as a thermal spraying method, an aerosol deposition method, an aerosol gas deposition method, a powder jet deposition method, a particle jet deposition method, and a cold spraying method), a PVD method (a sputtering method, a pulsed laser deposition method, or the like), a CVD method, or the like. This is because by these processes which can be used in a low-temperature range, a favorable internal reforming catalyst layer D can be obtained while suppressing damage due to high-temperature heating of the reducing gas supply path L1 (for example, the metal support 1 and the current-collector plate 3 with projections) provided with the internal reforming catalyst layer D, and the fuel cell single unit U having excellent durability can be obtained. Moreover, forming the internal reforming catalyst layer D after the diffusion suppressing layer x is formed on the surface of the metal support 1 or the current-collector plate 3 with projections is preferable because scattering of Cr from the metal support 1 or the current-collector plate 3 with projections can be suppressed.

(101) For example, a thickness of such an internal reforming catalyst layer D is preferably 1 μm or greater, more preferably 2 μm or greater, and still more preferably 5 μm or greater. This is because by setting the thickness as described above, a contact area with a fuel gas or steam is increased and thus an internal reforming conversion rate can be increased. Moreover, for example, the thickness is preferably 500 μm or less, more preferably 300 μm or less, and still more preferably 100 μm or less. This is because by setting the thickness as described above, a used amount of an expensive material for the internal reforming catalyst can be reduced to reduce a cost.

(102) Returning to FIG. 6 again, the steam reforming reaction in the internal reforming catalyst layer D will be briefly described. As shown in the same drawing, by providing the internal reforming catalyst layer D in the fuel cell single unit U, the raw fuel gas CH.sub.4 supplied to the reducing gas supply path L1 can be reformed as follows to generate hydrogren H.sub.2 and carbon monoxide CO which serve as a fuel gas for power generation. The reforming reaction is the same also in the embodiment shown in FIG. 11.
CH.sub.4+H.sub.2O.fwdarw.CO+3H.sub.2  [Chem. 1]
CO+H.sub.2O.fwdarw.CO.sub.2+H.sub.2  [Chem. 2]
CH.sub.4+2H.sub.2O.fwdarw.CO.sub.2+4H.sub.2  [Chem. 3]

(103) A temperature of the reducing gas supply path L1 (the internal reforming catalyst layer D) is practically 600° C. to 900° C., which is the operating temperature of the fuel cell element R. A structure which schematically shows the functional configuration of the fuel cell single unit U, as a fuel cell, according to the first embodiment described above is a structure shown in FIG. 19(a).

(104) In the above description, the outline of the fuel cell module M in the first embodiment is described. The structure of the fuel cell module M in this embodiment will be specifically described.

(105) As shown in FIG. 5, the fuel cell module M according to the first embodiment is configured by stacking the plurality of the fuel cell single units U. That is, the fuel cell module M is configured by stacking the plurality of the fuel cell single units U with a gasket 6 sandwiched therebetween. The gasket 6 is disposed between the gas supply pipe 2 of one fuel cell single unit U and the gas supply pipe 2 of another fuel cell single unit U. Moreover, the gasket 6 electrically insulates the metal support 1, the gas supply pipe 2, and the current-collector plate 3 with projections of one fuel cell single unit U from the metal support 1, the gas supply pipe 2, and the current-collector plate 3 of another fuel cell single unit U. Furthermore, the gasket 6 airtightly maintains a connection site (a connection site of the gas supply pipe 2) of the fuel cell single unit U so that a gas flowing through the first flow path 2b and the second flow path 2c of the gas supply pipe 2 is not leaked or mixed. The gasket 6 is formed, for example, by using vermiculite, mica, alumina, or the like as a material so that the electrical insulation and the airtight maintenance are possible.

(106) In addition, as described above, the current-collector plate 3 with projections electrically connects the metal support 1 of one fuel cell single unit U to the cathode layer C. Therefore, in the fuel cell single unit U according to the present embodiment, the fuel cell elements R of respective fuel cell single units U are electrically connected in series.

(107) The gas flow in the fuel cell module M has already been described.

(108) A configuration form of the reducing gas supply path L1 may be the current-collector plate 3 with projections having a shape shown in (a) of FIG. 4, or may be as shown in (b) of FIG. 4 or (c) of FIG. 4. In these configurations, a common technical element may be a configuration in which a reducing gas (specifically, a mixed gas of a gas, which is not yet reformed, and a reformed gas) containing hydrogen and an oxidizing gas (specifically, an air) which is a gas containing oxygen move to an outer diameter side and are exhausted as an exhaust gas.

(109) In the present invention, the reducing gas supply path L1 flows from the supply side of the mixed gas to the discharge side, and a gas containing hydrogen H.sub.2 flows to the anode layer A through the plurality (a large number) of the through-holes 1a provided therebetween. Moreover, by returning steam H.sub.2O generated in the anode layer A to the internal reforming catalyst layer D, the steam reforming is performed to generate hydrogen and carbon monoxide which are fuel gases for power generation, the fuel gas for power generation containing hydrogen H.sub.2 is supplied to the anode layer A from the through-hole 1a positioned on the downstream side, and thus power generation can be performed. Therefore, such a gas path is referred to as an internal reformed fuel supply path L3, a discharge side of the generated steam H.sub.2O is referred to as a discharge unit L3a, and a supply side of hydrogen H.sub.2 subjected to internal reforming is referred to as a supply unit L3b. The discharge unit L3a is also the steam supply path of the present invention. Furthermore, the discharge unit L3a can also simultaneously function as the supply unit L3b, and the supply unit L3b can also simultaneously function as the discharge unit L3a.

Second Embodiment

(110) Hereinafter, a fuel cell device Y, a fuel cell module M, and a fuel cell single unit U according to the second embodiment will be described with reference to the drawings.

(111) <Fuel Cell Device>

(112) FIG. 7 shows an outline of the fuel cell device Y.

(113) The fuel cell device Y is also configured to include the fuel cell module M, and a power generation operation is performed by a reducing gas containing hydrogen and an oxidizing gas containing oxygen, which are supplied to the fuel cell module M.

(114) As shown in FIGS. 7, 8(a), and 8(b), the fuel cell module M is formed in a form of a substantially rectangular parallelepiped, and the fuel cell module M, an external reformer 34, a vaporizer 33, and the like are included in one housing 10. Functions of respective machines (a boost pump 30, a desulfurizer 31, a reforming water tank 32, the vaporizer 33, and the external reformer 34) included in a supply system of the reducing gas are the same as those in the first embodiment described above. However, since the external reformer 34 and the vaporizer 33 are positioned in the housing 10 housing the fuel cell module M, heat of the fuel cell module M is effectively utilized.

(115) The fuel cell module M according to the second embodiment is provided with a combustion unit 101 for an exhaust gas containing hydrogen on an upper part thereof, residual combustion components (specifically, hydrogen, carbon monoxide, and methane) contained in the exhaust gas of the fuel cell can be combusted at the site 101, and heat of the combustion can be utilized for steam reforming and vaporization.

(116) Functions of an inverter 38, a control unit 39, and a heat exchanger 36 are the same as those in the previous embodiment.

(117) Therefore, also in the second embodiment, the fuel cell device Y is a so-called “cogeneration system”, which is capable of generating and supplying both electric power and heat.

(118) Incidentally, the supply of the reducing gas containing hydrogen and the supply of the oxidizing gas containing oxygen with respect to respective electrode layers (an anode layer A and a cathode layer C) included in the fuel cell single unit U or the fuel cell element R have a configuration unique to this embodiment.

(119) The outline thereof will be described with reference to FIGS. 7 and 11. A gas manifold 102 is provided on the downstream side of the external reformer 34, a gas (a raw fuel gas), which is not yet reformed, and a reformed gas are distributed and supplied to the reducing gas supply path L1 included in the fuel cell single unit U, and the reducing gas containing hydrogen is supplied to the anode layer A from the supply path L1.

(120) On the other hand, in the supply of the oxygen to an oxidizing gas supply path L2, an air is sucked by a blower 35 into the housing 10, and the sucked oxidizing gas containing oxygen is supplied to the cathode layer C through the oxidizing gas supply paths L2 respectively provided in the fuel cell single unit U and a current-collector plate CP. In this embodiment, the combustion unit 101 is provided between the fuel cell module M and the external reformer 34, but the air sucked by the blower 35 is also utilized for combustion of the residual fuel in the combustion unit 101.

(121) As described above, the exhaust gas generated by the predetermined cell reaction and combustion reaction is sent to the heat exchanger 36, and is provided for a predetermined heat utilization. Here, a machine 103a provided at an exhaust port 103 of the housing 10 is a machine for treating an exhaust gas.

(122) <Fuel Cell Module M>

(123) Next, the fuel cell module M will be described with reference to FIGS. 8(a) and 8(b).

(124) FIG. 8(a) shows a side view of the fuel cell module M, and FIG. 8(b) shows a cross-sectional view (VIII-VIII cross section of FIG. 8(a)) thereof.

(125) In this embodiment, the fuel cell module M is configured by stacking a plurality of the fuel cell single units U in a lateral direction (a right-left direction of FIGS. 8(a) and 8(b)). Specifically, each of the fuel cell single units U can be installed upright on the gas manifold 102 described above. That is, the fuel cell module M is constructed by erecting the metal support 1 supporting the fuel cell element R on the gas manifold 102.

(126) In the second embodiment, the metal support 1 is configured to include the reducing gas supply path L1 extending in a vertical direction in an erected state, and is formed in a tubular shape. On the other hand, since the current-collector plate CP having a concave-convex shape is provided so as to be electrically connected to the metal support 1, and the current-collector plate CP has air permeability, an oxidizing gas (specifically, an air) sucked to a peripheral part of the fuel cell module M is allowed to reach the cathode layer C of the fuel cell element R (see FIG. 11).

(127) As shown in FIGS. 8(a) and 8(b), the fuel cell module M is configured to include the plurality of the fuel cell single units U, the gas manifold 102, the current-collector plate CP, a terminal member 104, and a current drawing unit 105.

(128) The fuel cell single unit U is configured to include the fuel cell element R on one surface of the metal support 1 which is a hollow tube, and has a long flat plate shape or a flat bar shape as a whole. Moreover, one end part of the fuel cell single unit U in a longitudinal direction is fixed to a gas manifold 102 with an adhesive member such as a glass seal material. The metal support 1 is electrically insulated from the gas manifold 102.

(129) The fuel cell element R is configured in a form of a thin film or layer (in the present invention, a form including the both is referred to as a “thin layer shape”) as a whole. There is no difference in that also in this embodiment, the fuel cell element R is configured to include the anode layer A, an electrolyte layer B, and the cathode layer C. The matter in which a metal oxide layer x, an intermediate layer y, and a reaction preventing layer z described above are provided is also the same. The metal oxide layer x, the intermediate layer y, and the reaction preventing layer z are shown in FIG. 11.

(130) In the second embodiment, the plurality of the fuel cell single units U are stacked in a state where a back surface of the metal support 1 of one fuel cell single unit U is in contact with the current-collector plate CP of another fuel cell single unit U, and thus a predetermined electrical output can be taken out.

(131) For the current-collector plate CP, a member having conductivity, gas permeability, and elasticity in a direction of stacking and parallel arrangement of the fuel cell single units U is used. For example, an expanded metal using a metal foil, a metal mesh, or a felt-like member is used for the current-collector plate CP. Therefore, the air supplied from the blower 35 can permeate or flow through the current-collector plate CP to be supplied to the cathode layer C of the fuel cell element R. In the present invention, a flow path which configures the fuel cell single unit U and passes through the current-collector plate CP and through which a gas containing oxygen flows is referred to as the oxidizing gas supply path L2 (see FIG. 11).

(132) In addition, since the current-collector plate CP has elasticity in a direction of parallel arrangement of the fuel cell single units U, the metal support 1 cantilevered by the gas manifold 102 can also be displaced in the direction of the parallel arrangement, and robustness of the fuel cell module M against disturbances such as vibration and temperature change is enhanced.

(133) The plurality of the fuel cell single units U arranged in parallel are sandwiched between a pair of the terminal members 104. The terminal member 104 is a member which has conductivity and is elastically deformable, and a lower end thereof is fixed to the gas manifold 102. The current drawing unit 105 extending outward in the direction of the parallel arrangement of the fuel cell single unit U is connected to the terminal member 104. The current drawing unit 105 is connected to the in the inverter 38, and sends a current generated by the power generation of the fuel cell element R to the inverter 38.

(134) <Fuel Cell Single Unit U>

(135) FIGS. 9 and 10(a)-10(c) show a schematic configuration of the fuel cell single unit U according to the second embodiment.

(136) FIG. 9 is a perspective view of the fuel cell single unit U, and FIGS. 10(a)-10(c) shows a forming procedure of the unit U.

(137) As also described above, the fuel cell single unit U is configured to include the metal support 1 having conductivity and the fuel cell element R, and the fuel cell element R is configured to have the anode layer A and the cathode layer C which are formed so as to sandwich the electrolyte layer B.

(138) <Metal Support 1>

(139) The metal support 1 is configured to include a rectangular flat plate member 72, a U-shaped member 73 of which cross section orthogonal to a longitudinal direction has a U shape, and a lid part 74. A long side of the flat plate member 72 and a long side of the U-shaped member 73 (sides corresponding to two U-shaped vertexes) are bonded to each other, and one end part (in the drawing, an upper end side) is closed by the lid part 74. Therefore, the metal support 1 which has a flat plate shape or a flat bar shape as a whole and has a space inside is formed. The flat plate member 72 is disposed parallel to the central axis of the metal support 1.

(140) An internal space of the metal support 1 serves as the reducing gas supply path L1 described above. The lid part 74 is provided with an exhaust gas discharge port 77 for discharging a gas flowing through the reducing gas supply path L1 to the outside of the metal support 1. A discharge side (an upper side) of the exhaust gas discharge port 77 serves as the combustion unit 101 described above. An end part on a side (which is a lower side, and a site connected to the gas manifold 102 described above) opposite to the end part where the lid part 74 is provided is opened, and thus serves as the inlet of the reducing gas supply path L1.

(141) As materials for the flat plate member 72, the U-shaped member 73, and the lid part 74, materials having excellent conductivity, heat resistance, oxidation resistance, and corrosion resistance are used. For example, ferritic stainless steel, austenitic stainless steel, a nickel-based alloy, or the like is used. That is, the metal support 1 is robustly configured. In particular, ferritic stainless steel is suitably used.

(142) When the ferritic stainless steel is used as the material for the metal support 1, a thermal expansion coefficient of the metal support 1 is close to that of yttria-stabilized zirconia (YSZ) or gadolinium-doped ceria (GDC, also referred to as CGO) used as a material in the fuel cell element R. Therefore, even when a temperature cycle of a low temperature and a high temperature is repeated, the fuel cell single unit U is less likely to be damaged. Accordingly, a fuel cell element R having excellent long-term durability can be obtained, which is preferable.

(143) In addition, as the material for the metal support 1, a material having a thermal conductivity of greater than 3 Wm.sup.−1K.sup.−1 is preferably used, and a material having a thermal conductivity of greater than 10 Wm.sup.−1K.sup.−1 is more preferable. For example, since stainless steel has a thermal conductivity of about 15 to 30 Wm.sup.−1K.sup.−1, the stainless steel is suitable as the material for the metal support 1.

(144) Furthermore, as the material for the metal support 1, a high toughness material which does not cause brittle fracture is more desirable. A metal material has high toughness compared to a ceramic material or the like, and is suitable as the metal support 1.

(145) As is also clear from FIGS. 10(a)-10(c), the flat plate member 72 is provided with a plurality of through-holes 78 penetrating the front surface and the rear surface of the flat plate member 72. A gas can flow between the inside and the outside of the metal support 1 through the through-hole 78. On the other hand, in a region of the flat plate member 72 or the U-shaped member 73 where the through-holes 78 are not provided, a gas cannot flow between the inside and the outside of the metal support 1.

(146) Hereinbefore, the basic configuration of the fuel cell according to the present invention has been described, but hereinafter, the feature configurations of the present invention will be described mainly with reference to FIGS. 10(a)-10(c) and 11.

(147) As also described above, in the present embodiment, the reducing gas supply path L1 for supplying a gas containing hydrogen to the anode layer A is formed in the metal support 1. Moreover, as also indicated by an alternate long and short dash line arrow in FIG. 9, the gas in the supply path L1 is directed in one direction from an axial opening side (a lower side) of the metal support 1 to an axial lid part side (an upper side). Hydrogen H.sub.2 for a power generation reaction can be supplied to the anode layer A through the through-hole 78, which is provided so as to penetrate the front and rear of the flat plate member 72. Here, the power generation reaction in the fuel cell element R is as described above, but due to the reaction, steam H.sub.2O is released from the anode layer A to the through-hole 78. As a result, a part of the through-hole 78 and the reducing gas supply path L1 of the present embodiment serves as a supply unit L3b for supplying a gas containing hydrogen H.sub.2, and also serves as a discharge unit L3a of steam H.sub.2O.

(148) Accordingly, as shown in FIGS. 10(a)-10(c) and 11, the internal reforming catalyst layer D is provided on a rear surface of 72b of the flat plate member 72 and an inner surface 73b of the metal support 1.

(149) As also described above, in addition to hydrogen obtained by external reforming, a gas (which is a raw fuel gas, and in the illustrated example, methane CH.sub.4), which is not yet reformed, to be reformed flows through the reducing gas supply path L1, but by returning steam H.sub.2O generated in the anode layer A to the internal reforming catalyst layer D, steam reforming is performed, hydrogen H.sub.2 is supplied to the anode layer A from the through-hole 78 positioned on the downstream side (in a case of FIG. 11, a rear side of the paper), and thus power generation can be performed. Therefore, the matter in which the internal reformed fuel supply path L3 according to the present invention includes the discharge unit L3a of the generated steam H.sub.2O and the supply unit L3b of hydrogen H.sub.2 subjected to internal reforming is the same as in the first embodiment. Furthermore, the discharge unit L3a can also simultaneously function as the supply unit L3b, and the supply unit L3b can also simultaneously function as the discharge unit L3a. The discharge unit L3a serves as the steam supply path.

(150) A material for the internal reforming catalyst layer D, a thickness thereof, and the like are the same as described above.

(151) By adopting such a structure, in the metal support 1, steam H.sub.2O discharged from the anode layer A is utilized to cause steam reforming, and hydrogen H.sub.2 and carbon monoxide CO obtained by the reforming can be supplied to and utilized for the anode layer A as the fuel gas for power generation.

(152) The fuel cell single unit according to the second embodiment practically has a structure shown in FIG. 19(a).

Third Embodiment

(153) Hereinafter, a fuel cell device Y, a fuel cell module M, and a fuel cell single unit U according to the third embodiment will be described with reference to the drawings.

(154) <Fuel Cell Device>

(155) FIG. 12 is a schematic diagram showing the entire configuration of the fuel cell device Y, and shows a fuel gas supply system FL, an oxidizing gas supply system AL, and an anode off-gas circulation system RL which are connected to the fuel cell module M, which is a fuel cell main body.

(156) In the fuel cell module M, one of a plurality of the fuel cell single units U which are stacked to configure the fuel cell module M is schematically shown. As also described above, the fuel cell single unit U includes the fuel cell element R. The fuel cell single unit U, the fuel cell element R, and the like will be described in relation to the first embodiment described above. In the first embodiment, the metal support 1 is formed in a disc shape, whereas in the third embodiment, a metal support 1 is formed in a basic square shape, and in a longitudinal direction thereof, the fuel cell element R, a reducing gas supply path L1, and an oxidizing gas supply path L2 are formed.

(157) Features of the third embodiment are the following two points.

(158) 1. In a steady operation state where activation of the fuel cell is completed and power generation is performed according to an electric power load, steam circulated through the anode off-gas circulation system RL is used for reforming.

(159) 2. An internal reforming catalyst layer D and a turbulence promotion component E are provided in the reducing gas supply path L1 provided in the fuel cell single unit U.

(160) Also in this embodiment, the fuel cell device Y is configured as a so-called cogeneration system (heat and electric power supply system), and includes a heat exchanger 36 as an exhaust heat utilization unit which utilizes heat discharged from the fuel cell device Y, and an inverter 38 as an output conversion unit for outputting electric power generated in the fuel cell device Y.

(161) A control unit 39 controls operations of the entire fuel cell device Y according to the electric power load required for the fuel cell device Y. Each machine to be controlled will be described in the description of the machine. Input information to the control unit 39 is information on activation start and activation stop of the fuel cell device Y and the electric power load required for the device Y.

(162) The fuel cell device Y is configured to include the fuel cell module M, the fuel gas supply system FL, the oxidizing gas supply system AL, and the anode off-gas circulation system RL. The fuel gas supply system FL corresponds to the fuel supply path of the present invention.

(163) The fuel gas supply system FL includes a raw fuel gas supply system FLa which is provided with a boost pump 30 and a desulfurizer 31, and a steam supply system FLb which is provided with a reforming water tank 32, a reforming water pump 32p, and a vaporizer 33.

(164) The raw fuel gas supply system FLa and the steam supply system FLb adopt a form of being merged into the anode off-gas circulation system RL, and supply a raw fuel gas and steam to an external reformer 34 provided on a downstream side. The external reformer 34 is connected, on a downstream side, to the reducing gas supply path L1 formed in the fuel cell single unit U configuring the fuel cell module M.

(165) The boost pump 30 boosts a hydrocarbon-based gas, such as a city gas, which is an example of the raw fuel gas, and supplies the gas to the fuel cell device Y. In the supply form, an amount of the raw fuel gas commensurate with the electric power load required for the fuel cell device Y is supplied in accordance with an instruction from the control unit 39.

(166) The desulfurizer 31 removes (desulfurizes) a sulfur compound component contained in a city gas or the like.

(167) The reforming water tank 32 stores reforming water (basically pure water) in order to supply steam required for steam reforming in the external reformer 34. In the supply form, the raw fuel gas is supplied in an amount in accordance with an instruction from the control unit 39 in order to obtain the fuel gas commensurate with the electric power load required for the fuel cell device Y. However, as also will be described later, in the fuel cell device Y according to this embodiment, in the normal steady operation state, steam contained in the anode off-gas can cover the steam required for steam reforming, and thus supply of reforming water from the reforming water tank 32 and vaporization in the vaporizer 33 are fulfilled mainly at the time of activation of the fuel cell device Y.

(168) The vaporizer 33 converts the reforming water supplied from the reforming water tank 32 into steam. The external reformer 34 steam-reforms a raw fuel gas desulfurized in the desulfurizer 31 using the steam generated in the vaporizer 33 to form a reformed gas which is a gas containing hydrogen. However, since the internal reforming catalyst layer D is included in the fuel cell single unit U according to the present invention, reforming of the raw fuel gas is performed also in the unit U. As a result, in the external reformer 34, a part of the raw fuel gas is reformed, and the remainder is supplied, as it is, to the reducing gas supply path L1 of the fuel cell single unit U.

(169) A steam reforming catalyst is stored in the external reformer 34, but examples of this type of catalyst include a ruthenium-based catalyst and a nickel-based catalyst. Moreover, specifically, a Ru/Al.sub.2O.sub.3 catalyst obtained by carrying a ruthenium component on an alumina support, a Ni/Al.sub.2O.sub.3 catalyst obtained by carrying a nickel component on an alumina support, or the like can be used.

(170) Incidentally, an operation in the steady operation state where the fuel cell device Y continuously generates power according to the electric power load will be described below.

(171) Since the fuel cell is of an oxide ion conduction type, steam is contained in an exhaust gas (an anode off-gas) discharged from the reducing gas supply path L1 provided in the fuel cell single unit U. Therefore, an operation form in which excessive moisture is condensed and removed while cooling the gas, and the anode off-gas whose steam partial pressure is adjusted is returned to the external reformer 34 and provided for steam reforming is adopted.

(172) That is, the fuel cell device Y includes the anode off-gas circulation system RL, and the anode off-gas circulation system RL includes a cooler 32a for cooling the anode off-gas flowing inside, a condenser 32b for further cooling the gas and extracting the condensed water to adjust a steam partial pressure of the anode off-gas flowing inside, and a heater 32c for raising a temperature of the anode off-gas returned to the external reformer 34.

(173) By adopting this structure, a circulation pump 32d is caused to work, and the amount of the steam input to the external reformer 34 may depend on the gas circulated through the anode off-gas circulation system RL. By adjusting a condensation temperature in the condenser 32b at a final stage, the partial pressure of the steam circulated through the anode off-gas circulation system RL can be adjusted, and a steam/carbon ratio (a S/C ratio) of the gas input to the external reformer 34 can be controlled.

(174) In the circulation form, an amount of steam required when at least a part of the raw fuel gas is reformed in the external reformer 34 in accordance with the electric power load required for the fuel cell device Y is set so that an appropriate S/C ratio is obtained in the external reformer 34, and the operation is performed in accordance with an instruction from the control unit 39.

(175) Objects to be controlled here are a circulation amount by the circulation pump 32d, pressure setting, and setting and controlling of a condensation temperature (as a result, a steam partial pressure at an outlet) in the condenser 32b which is a final stage of cooling.

(176) The oxidizing gas supply system AL is provided with a blower 35, and, on a downstream side, connected to the oxidizing gas supply path L2 formed in the fuel cell single unit U configuring the fuel cell module M. An air suction amount by the blower 35 also ensures an air amount sufficient to cause a power generation reaction in the fuel cell in accordance with the electric power load, and the operation is performed in accordance with an instruction from the control unit 39.

(177) The above description is a contrivance mainly of the supply side of the reducing gas in the third embodiment, but as in the present invention, in a configuration in which the internal reforming catalyst layer D is included in the fuel cell single unit U and hydrogen or carbon monoxide obtained by internal reforming is used as a cell fuel, steam generated by power generation is consumed by steam reforming, and thus a load on the condenser 32b to be provided for condensing steam contained in the anode off-gas described above is reduced. As a result, the fuel cell device Y according to the present invention is also advantageous in this respect.

(178) Contrivance of Position where Internal Reforming Catalyst Layer is Provided

(179) As shown in FIGS. 13 and 14, the fuel cell single unit U according to the third embodiment is formed in a substantially square box shape when viewed from above, and flow directions of the reducing gas and the oxidizing gas are set to a specific one direction. In FIGS. 13 and 14, the direction is upward to the right in the drawings.

(180) Incidentally, the position where the internal reforming catalyst layer D is provided is as described above, but in this embodiment, as shown in FIG. 14, the position of the internal reforming catalyst layer D is limited to a position which is the same as that of a through-hole 1a on the most upstream side in the flow direction of the reducing gas, among through-holes 1a provided to supply the reducing gas to an anode layer A and discharge steam generated in the anode layer A to the reducing gas supply path L1, and a position on a downstream side of the position.

(181) By providing the internal reforming catalyst layer D at such a position, the steam generated in the anode layer A can be effectively used according to the object of the present invention.

(182) The fuel cell single unit U according to the third embodiment practically has a structure shown in FIG. 19(b).

(183) Contrivance to Provide Turbulence Promotion Component

(184) As shown in FIGS. 12, 13, and 14, the reducing gas supply path L1 for supplying the fuel gas to the anode layer A is provided with the turbulence promotion component E (Ea) for disturbing the flow in the path.

(185) More specifically, a net-like body Ea is provided on a surface of the through-hole 1a, which is formed so as to penetrate the metal support 1, on an inflow side of the reducing gas, which is a gas containing hydrogen, and opposite to a surface on which the fuel cell element R is formed. Specifically, the net-like body Ea is formed by sticking a lath metal or a metal wire mesh on the metal support 1. As a result, the gas containing hydrogen flowing through the reducing gas supply path L1 is disturbed by the net-like body Ea, and induces a flow direction component toward the through-hole 1a and flow flowing out from the through-hole 1a, and thus the supply of the fuel gas to the anode layer A and the leading of the steam from the anode layer A can be favorably caused.

(186) The above description relates to the structure of the fuel cell in which the internal reforming (the steam reforming in the fuel cell element R) is performed by utilizing the steam H.sub.2O generated in the anode layer A of the fuel cell element R in the fuel cell single unit U according to the present invention.

(187) Advantages in a case where the fuel cell is operated with the internal reforming of the present invention will be described below.

(188) FIG. 15 shows a comparison of the power generation efficiency of the fuel cell between a case where internal reforming is performed and a case where the internal reforming is not performed, and FIGS. 16 and 17 show partial pressures of fuel gas for power generation, which contains hydrogen and carbon monoxide, at the inlet and the outlet (specifically, the inlet and the outlet of the reducing gas supply path L1) of the fuel cell element R in both the cases. FIG. 18 is a graph showing a difference in the partial pressures of the fuel gas for power generation between the same inlet and the same outlet.

(189) Regarding the description of the partial pressure of the fuel gas for power generation, a proportion (%) with respect to a total gas pressure is used.

(190) Furthermore, the difference in the partial pressures of the fuel gas for power generation is as follows.

(191) Proportion of partial pressure of fuel gas for power generation at inlet of reducing gas supply path: Rin
Rin=[partial pressure of fuel gas for power generation]/[total gas pressure]×100%

(192) Proportion of partial pressure of fuel gas for power generation at outlet of reducing gas supply path: Rout
Rout=[partial pressure of fuel gas for power generation]/[total gas pressure]×100%
Difference in partial pressures of fuel gas for power generation=Rin−Rout [%]

(193) In these drawings, a black square mark indicates a case where the internal reforming according to the present invention is performed, and a white rhombus mark corresponds to a case where the internal reforming is not performed.

(194) In all the drawings, a horizontal axis represents a molar ratio (a S/C ratio) of steam (S) and carbon (C) introduced into the fuel cell. The S/C ratio is a S/C ratio of the gas (the mixed gas of the raw fuel gas and the steam) introduced into the external reformer 34 in the configurations of the fuel cell devices Y shown in FIGS. 1, 7, and 12, and is an operating parameter which may be changed depending on operating conditions such as the electric power load of the fuel cell. The S/C ratio was changed from 1.5 to 3.0 at an interval of 0.5. The range is a range which may be normally changed in the operation of the fuel cell device Y.

(195) In addition, conditions set for the investigation are shown.

(196) TABLE-US-00001 Generated voltage of fuel cell single unit 0.8 V Temperature (=internal reforming temperature) 700° C. of fuel cell element Total fuel utilization rate of fuel cell 80%

(197) The total fuel utilization rate of the fuel cell is a proportion of the fuel gas (H.sub.2+CO) for power generation consumed by the power generation reaction in the fuel cell device Y, and is expressed by the following expression.
[Number of moles of fuel gas for power generation consumed by power generation reaction]/[total of fuel gases for power generation which is supplied to fuel cell and generated by internal reforming]×100%

(198) TABLE-US-00002 Reducing gas hydrogen and carbon monoxide Electrolyte oxygen ion conduction-type electrolyte

(199) Equilibrium Temperature of External Reformer

(200) TABLE-US-00003 case where internal reforming is performed 700° C. case where internal reforming is not performed 500° C. Process pressure 120 kPa

(201) The process pressure is specifically a gas pressure in the external reformer 34 and the respective gas supply paths L1 and L2.

(202) Investigation Results

(203) <Power Generation Efficiency or the Like>

(204) As is also clear from FIG. 15, in a case where the internal reforming is performed, the fuel gas for power generation is increased due to fuel reforming by the steam generated inside the fuel cell, the power generation amount is increased under conditions of a constant fuel utilization rate, and thus efficiency is increased.

(205) Since the equilibrium temperature of the external reformer 34 in a case where the internal reforming is performed can be suppressed as low as 500° C., even when the S/C ratio is low, thermal decomposition (caulking) of hydrocarbon is less likely to occur, and thus an advantage of enhancing reliability of a process or a system arises.

(206) As a result, due to the design of the fuel cell device Y, lowering the temperature of the external reformer 34 and reducing the S/C ratio can supply steam reforming reaction heat and evaporation heat and reduce a heat transfer area of the condenser (the condenser 32b which is included in the anode off-gas circulation system RL described in the third embodiment) for water self-sustaining (an operation form in which a fuel gas is obtained by performing steam reforming using only steam (water) generated by power generation in an operation state where power generation is performed according to the electric power load), which is also advantageous in terms of a cost. In this investigation, when the S/C ratio in a case where the internal reforming is not performed is set to 2.5, and the S/C ratio in a case where the internal reforming is performed is set to 2.0, due to the design of the fuel cell device Y, a quantity of heat required for the external reformer 34 is reduced by 60%, a quantity of heat transfer of the vaporizer 33 required for steam generation is reduced by 20%, and direct-current power generation efficiency is improved by 3.6%.

(207) <Partial Pressure of Fuel Gas for Power Generation>

(208) As is also clear from FIG. 16, there is a difference of 1.5 to 2 times in the partial pressures of the fuel gas for power generation at the inlet of the fuel cell element R depending on the presence or absence of the internal reforming, and a value in a case where the internal reforming is performed is a lower value. In a case where the internal reforming is not performed, the higher the S/C ratio, the lower the partial pressure. This is because an influence of an increase in the steam is greater than an influence of an increase in the generation amount of the hydrogen or the carbon monoxide.

(209) In a case where the internal reforming is performed, even when the S/C ratio is changed, the partial pressure of the fuel gas for power generation is hardly changed. Since the temperature of the external reformer 34 is low, an increase in the fuel and an increase in the steam due to the high S/C ratio are almost balanced.

(210) In addition, in a case where the internal reforming is performed, the partial pressure of the fuel gas for power generation at the inlet of the fuel cell can be reduced by lowering the temperature (500° C.) of the external reformer 34, but the steam reforming reaction rapidly occurs due to the generated steam in the fuel cell (700° C.), and thus the partial pressure of the fuel gas for power generation at the outlet of the fuel cell is increased. The increase in the partial pressure at the outlet of the cell is advantageous for stabilizing off-gas combustion.

(211) Furthermore, in a case where the internal reforming is performed, by reducing the difference (concentration difference) in the partial pressures of the fuel gas for power generation between the outlet and the inlet of the fuel cell, uneven distribution of power generation amounts in the fuel cell element R is reduced, a temperature difference is also reduced, and thus durability or reliability is improved by relaxing thermal stress of the fuel cell.

(212) <Operation of Fuel Cell Device Y>

(213) According to the investigation conducted by the inventors, the fuel cell device described above is preferably operated under the following conditions.

(214) (1) The steam/carbon ratio (the S/C ratio) at the inlet of the external reformer 34 is controlled to be within a range of 1.5 to 3.0. The S/C ratio is more preferably controlled to be within a range of 1.5 to 2.5. In particular, when the external reformer 34 is operated at a relatively low S/C ratio (1.5 to 2.5) as described above, by setting the concentration of the sulfur contained in the raw fuel gas to 1 vol. ppb or less (more preferably, 0.1 vol. ppb or less), a stable operation can be ensured for a long period of time.

(215) (2) The reforming temperature in the external reformer 34 is controlled to be lower than the temperature in the internal reforming catalyst layer D provided in the reducing gas supply path L1.

(216) (3) The operation is performed so that the partial pressure of the fuel gas for power generation at the inlet of the reducing gas supply path L1 is 50% or less of a total gas pressure.

(217) That is, under the same electric power load, the partial pressure of the fuel gas for power generation at the inlet of the reducing gas supply path L1 is controlled to be lower than the partial pressure of the fuel gas for power generation at the inlet of the reducing gas supply path L1, which is set when the reforming of the fuel gas is mainly performed in the external reformer 34 (for example, at the time of starting the fuel cell device Y).

(218) (4) The operation is performed so that the difference between the proportions (the proportion of the partial pressure of the fuel gas for power generation with respect to the total gas pressure, which is expressed in a percentage) of the partial pressures of the fuel gas for power generation at the inlet and the outlet of the reducing gas supply path L1 is maintained within 40%.

(219) (5) The reforming conversion rate of the fuel gas reformed by the external reformer 34 is set to 30% to 60%.

(220) (6) Under the same electric power load, the steam/carbon ratio (the S/C ratio) at the inlet of the external reformer 34 is controlled to be lower than the steam/carbon ratio (the S/C ratio) set when the reforming of the fuel gas is mainly performed in the external reformer 34 (for example, at the time of starting the fuel cell device Y).

Other Embodiments

(221) (1) In the first embodiment, the anode layer A is disposed between the metal support 1 and the electrolyte layer B, and the cathode layer C is disposed on a side opposite to the metal support 1 when viewed from the electrolyte layer B. A configuration in which the anode layer A and the cathode layer C are disposed in reverse can also be adopted. That is, a configuration in which the cathode layer C is disposed between the metal support 1 and the electrolyte layer B, and the anode layer A is disposed on a side opposite to the metal support 1 when viewed from the electrolyte layer B can also be adopted. In this case, by reversing the positional relationship between the reducing gas supply path L1 and the oxidizing gas supply path L2, and, as also described above, providing the internal reforming catalyst layer D on the side (in this case, the lower side of the metal separator 7) of the reducing gas supply path L1, the object of the present invention can be achieved.

(222) (2) In each of the above-described embodiments, one fuel cell element R is formed on the metal support 1, but a plurality of the fuel cell elements R may be divided and arranged on the front side of the metal support 1.

(223) (3) In the embodiments described above, regarding the formation site of the internal reforming catalyst layer D, a case where the internal reforming catalyst layer D is formed on the rear side 1f of the metal support 1 and the inner surface of the metal separator 3 or 7 on the side of the reducing gas supply path L1 has been described, but when the internal reforming catalyst layer D is formed at a site where the steam generated in the anode layer A flows, the internal reforming catalyst layer D serves for the internal reforming, and thus may be provided on the inner surface of the through-hole 1a provided in the metal support 1.

(224) (4) Regarding the reforming in the external reformer 34, the external reformer 34 performs the steam reforming, but in the present invention, the load on the external reformer 34 can be reduced, and thus a reformer which performs reforming other than the steam reforming, for example, partial combustion reforming or autothermal reforming can also be adopted.

(225) The raw fuel gas used in the present invention is a so-called hydrocarbon-based fuel, which may be any fuel as long as at least hydrogen can be generated by reforming the raw fuel gas.

(226) (6) In the above embodiments, the turbulence promotion component E is formed with the net-like body Ea and is stuck on the surface of the metal support 1, but the turbulence promotion component E may have a function of directing the flow in the reducing gas supply path L1 in the direction of the through-hole 1a, and a large number of obstacle bodies Eb which disturb the flow of the reducing gas supply path L1 may be arranged. The obstacle body Eb may have any shape such as a spherical shape, a triangular pyramid shape, and a columnar shape. FIG. 20 shows an example in which the obstacle body Eb has a spherical shape.

(227) (7) In the above embodiment, the internal reforming catalyst layer D and the turbulence promotion component E are described as being independent from each other, but for example, the internal reforming catalyst layer D may be provided on at least a part of the surface of the net-like body Ea described above or at least a part of the obstacle body Eb. This example is shown in FIG. 21.

(228) That is, by providing the internal reforming catalyst layer D on at least a part (in the illustrated example, a surface) of the turbulence promotion component E, the turbulence promotion component E can be disposed to exhibit both functions of turbulent flow promotion and internal reforming.

(229) (8) In the first embodiment and the second embodiment, the example in which the internal reforming catalyst layer D is provided in the reducing gas supply path L1 has been shown. Also in these embodiments, the turbulence promotion component E may be provided in the reducing gas supply path L1. FIG. 22 shows a configuration example in a case of the second embodiment of the present invention. In this example, the mesh as the net-like body Ea (E) serving as the turbulence promotion component is disposed inside the fuel gas supply path as the reducing gas supply path L1 formed in the tube, and the internal reforming catalyst layer D is also formed on the outer surface thereof.

(230) (9) In the above embodiments, the example in which the hydrocarbon-based gas such as a city gas (a gas which contains methane as a main component, and also contains ethane, propane, butane, and the like) is used as the raw fuel gas has been shown, but as the raw fuel gas, hydrocarbons such as a natural gas, naphtha, and kerosene, alcohols such as methanol and ethanol, and ethers such as DME can be used.

(231) (10) In the above embodiments, the case where the intermediate layer y is disposed between the anode layer A and the electrolyte layer B, and the reaction preventing layer z is disposed between the electrolyte layer B and the cathode layer C has been described, but a configuration in which interposed layers such as the intermediate layer y and the reaction preventing layer z, which are interposed between the electrode layer and the electrolyte layer, is not provided may be adopted, or only one of the interposed layers may be provided. Moreover, the number of the interposed layers can also be increased, as needed.

(232) (11) In the above embodiments, the case where the metal oxide layer x as a diffusion suppressing layer is provided on the surface of the metal support 1 has been described, but as needed, a configuration in which the metal oxide layer x is not provided may be adopted, or a plurality of the metal oxide layers x may be provided. Moreover, a diffusion suppressing layer different from the metal oxide layer can also be provided.

(233) Furthermore, the configurations disclosed in the above-described embodiments can be applied in combination with the configuration disclosed in another embodiment unless inconsistency occurs, and since the embodiments disclosed in the present specification are examples, the embodiments of the present invention are not limited thereto and can be appropriately modified within a range not departing from the object of the present invention.