JP5312008B2 - Fuel cell - Google Patents

Description

  The present invention relates to a fuel cell that can be started up quickly and has high power generation efficiency.

  In recent years, various fuel cells in which a stack of fuel cells is accommodated in a storage container have been proposed as next-generation energy.

  A solid oxide fuel cell is configured by housing a fuel cell stack composed of a plurality of solid electrolyte fuel cells in a storage container, and is operated at a temperature of about 1000 ° C.

  The solid electrolyte fuel cell needs to heat the fuel cell up to this temperature, and has a problem that it takes a long time to substantially generate power.

  Further, as a method for supplying hydrogen used as a fuel when generating electricity, a steam reforming method is used in which hydrogen such as natural gas reacts with steam to generate hydrogen. This reaction is also performed at 500 to 900 ° C. Therefore, there is also a problem that it takes a long time to heat the fuel reformer that performs the reforming reaction.

  The long time required for heating the fuel cell and the fuel reformer in this way is a problem that the power generation efficiency is low.

  In order to solve such a problem, a fuel reformer of a solid oxide fuel cell is disposed in a storage container containing a fuel cell stack, and heat generated during power generation is used for a steam reforming reaction. In order to improve the thermal efficiency, for example, see Patent Document 1.

In polymer fuel cells, fuel is produced by a partial oxidation method, which is an exothermic reaction, or a combination of a partial oxidation method and a steam reforming method (hereinafter referred to as an autothermal method) to shorten the start-up time of the reformer. A reforming apparatus that eliminates the need for a heating source by reforming has been reported (for example, see Patent Document 2).
JP-A-8-287937 JP 2001-185196 A

  However, in the system in which the above-described fuel reformer is disposed in the storage container, the reforming catalyst is filled in the fuel supply chamber above the power generation chamber, and the radiant heat from the power generation chamber and the heat transfer of the exhaust gas are used as a heat source. However, there are problems that the distance from the heat source is increased and it takes time to raise the temperature of the fuel reformer, and that heating to a temperature higher than the power generation temperature is impossible.

  In addition, when the fuel cell output is reduced and the load is low, the amount of heat generated by the power generation reaction is reduced, so that the temperature of the power generation chamber is lowered and the amount of heat necessary for the steam reforming reaction may be insufficient. Furthermore, since an external heating source is required at the time of start-up, there is a problem that the thermal efficiency is lowered.

  In addition, when fuel reforming is always performed by a partial oxidation method or a combination of a partial oxidation method and a steam reforming method, the amount of hydrogen produced is less than that of the steam reforming method, resulting in a decrease in power generation efficiency. There is a problem.

  That is, the conventional method has a problem that the start-up time is not yet shortened and high power generation efficiency is not sufficiently achieved.

  An object of the present invention is to provide a fuel cell that can greatly shorten the startup time and has high power generation efficiency.

The fuel cell of the present invention fixes a plurality of columnar fuel cells having a fuel gas passage along the longitudinal direction inside the storage container, and a lower end portion of the fuel cell, and the fuel gas passage. A fuel gas tank for circulating fuel gas through the fuel cell, a fuel reformer for supplying fuel gas to the fuel cell, the fuel reformer being disposed on the upper end side of the fuel cell, the fuel reformer and the fuel A reformed gas supply pipe for connecting to a gas tank is housed, and the fuel reformer is connected at one end to a pipe for supplying a gas to be reformed and a pipe for supplying steam or water. In addition, a water vapor generation unit, a gas mixing unit , a reformed gas flow channel, a reforming unit, and a reformed gas flow channel are sequentially provided and integrated in order from the side where the pipes are connected. It is of the fuel reformer and the fuel cell During the can are a combustion portion for burning said fuel gas discharged from the upper end portion of the fuel cell, in said fuel reformer, in order from a side closer to the combustion portion, the reforming portion, The reformed gas flow path and the reformed gas flow path are arranged so as to be stacked, and the fuel reformer is directly exposed to the combustion gas in the combustion section.

According to the present invention, along with burning fuel gas discharged from the upper end of the fuel cell, so that the fuel reformer is directly exposed to the fuel gas generated by burning fuel gas, in the storage container Since the fuel reformer is arranged on one end side of the fuel cell, the thermal efficiency can be increased without providing a heating source necessary for the steam reforming reaction, and the surplus fuel gas the by combustion, since the high temperature heat source than the power generation unit of the fuel cell can be a heating source of the fuel reformer can be quickly heat the fuel reformer. In addition, by using a high-temperature heat source, the amount of heat necessary for the steam reforming reaction can be sufficiently provided even during low-load operation where the amount of heat generated by the power generation of the fuel battery cell is reduced.

Further , in the fuel reformer, a steam generation unit, a gas mixing unit, and a reforming unit are arranged in order from the side where the piping for supplying the gas to be reformed and the piping for supplying steam or water are connected. By being continuously provided and integrated, miniaturization is possible. Further, since the fuel reformer is disposed at a position where the temperature becomes high, by integrating the steam generation unit, a large amount of heat necessary for generating the steam can be efficiently supplied.

  In the fuel cell of the present invention, the reforming section is preferably filled with a reforming catalyst in which a base metal catalyst and a noble metal catalyst are mixed.

  Although the base metal catalyst is inexpensive, the partial oxidation reaction start temperature is higher than that of the noble metal catalyst. Therefore, a large amount of heat is required before starting the reaction, and a large amount of catalyst is required, resulting in a large fuel reformer. On the other hand, the noble metal catalyst has a higher activity than the base metal catalyst, so the reaction start temperature is low, and the fuel reformer can be downsized, but the cost is high.

  By mixing both catalysts, the reaction start temperature is lowered, the startability is improved, the fuel reformer can be made smaller than before, and the cost can be further reduced.

The fuel cell of the present invention, the fuel reformer, it is preferable that the reformed gas flow passage and / or the reformed gas flow channel along said reformer is disposed.

  The reforming section is in contact with the gas to be reformed first by performing the reforming reaction, and the reforming section inlet side where the reforming reaction occurs abruptly, and the reaction has almost reached equilibrium and the reformed gas heat transfer And a large temperature gradient occurs between the two.

  During partial oxidation reforming, which is an exothermic reaction, the inlet side is hot and the outlet side is cold, but during steam reforming, which is an endothermic reaction, the inlet side is cold and the outlet side is hot, and the temperature difference for each reaction is about 100 to 300 ° C. Spill.

  Since this temperature gradient lowers the durability of the reforming catalyst and the refractory metal constituting the fuel reformer, it is necessary to relax the temperature gradient. As a means for this, the reformed gas flow along the reforming section is necessary. By forming the path, heat exchange is performed between the reforming catalyst inlet vicinity and the reformed gas.

  Since the reformed gas temperature is the same as or lower than the reforming catalyst outlet temperature, if the vicinity of the reforming catalyst inlet is higher than the outlet temperature, heat is transferred from the catalyst to the reformed gas. Is generated, the vicinity of the reforming catalyst inlet is lowered, and the temperature gradient is alleviated.

  Similarly, when the vicinity of the reforming catalyst inlet is lower than the outlet temperature, heat transfer from the reformed gas to the catalyst part occurs, the vicinity of the reforming catalyst inlet rises, and the temperature gradient is relaxed.

According to the fuel cell of the present invention, a fuel reformer, as is directly exposed to the combustion gas generated by combusting the fuel gas discharged from the upper end of the fuel cell, one of the fuel cell Since the fuel reformer can be efficiently heated with combustion gas having a temperature higher than that of the conventional fuel gas, it is possible to sufficiently cover the amount of heat necessary for the steam reforming reaction even during low load operation. At the same time, improvement in thermal efficiency and reduction in start-up time can be achieved.

  1 and 2 show an embodiment of a fuel cell according to the present invention. Reference numeral 1 denotes a storage container having a heat insulating structure.

  The storage container 1 includes a frame body (not shown) made of a heat-resistant metal and a heat insulating material (not shown) provided on the inner surface of the frame body.

  The storage container 1 stores a plurality of fuel battery cell stacks 7 in which a fuel reformer 3 and an auxiliary heat source (heating device not shown) and a plurality of fuel battery cells 5 are assembled. The lower end portion of the fuel battery cell 5 is supported and fixed to the upper lid 10 of the fuel gas tank 8 that also serves as a support for the fuel battery cell 5.

  For example, as shown in FIG. 2, the fuel cell stack 7 includes a plurality of fuel cells 5 each having a fuel gas passage 11 formed therein, arranged in two rows, and two rows of outermost fuel cells arranged adjacent to each other. The electrodes of the cells 5 are connected by the conductive member 12, whereby a plurality of fuel cells 5 arranged in two rows are electrically connected in series. The fuel cells 5 are connected to each other by a conductive current collecting member 14.

  In FIG. 2, the detailed structure of the fuel cell 5 is omitted. Moreover, the fuel cell stack was described as two rows.

  FIG. 3 specifically illustrates the structure of the fuel cell 5 and the fuel cell stack 7. The fuel cell 5 has, for example, a flat cross section and an elliptic cylinder shape as a whole. A plurality of fuel gas passages 11 are formed in the inside in the longitudinal direction. The fuel cell 5 has a shape that is long in the direction of the fuel gas passage 11, and the length in the longitudinal direction is longer than the length in the width direction orthogonal to the longitudinal direction.

  The fuel cell 5 has a flat cross section, and a dense solid electrolyte 5b, porous conductivity on the outer surface of a fuel-side electrode 5a mainly composed of a porous metal having an elliptical columnar shape as a whole. The oxygen-side electrode 5c made of ceramics is sequentially laminated, and an interconnector 5d is formed on the outer surface of the fuel-side electrode 5a opposite to the oxygen-side electrode 5c. The fuel-side electrode 5a serves as a support. .

  A current collecting member 14 made of metal felt and / or a metal plate is interposed between one fuel cell 5 and the other fuel cell 5, and the fuel side electrode 5 a of one fuel cell 5 is connected to the fuel cell 5. A fuel cell stack 7 is configured by being electrically connected to the oxygen side electrode 5c of the other fuel cell 5 via an interconnector 5d provided on the fuel side electrode 5a and a current collecting member 14.

  In the fuel cell stack 7, a portion where the fuel side electrode 5a, the solid electrolyte 5b, and the oxygen side electrode 5c are superimposed is a portion that generates power.

  A portion where the fuel side electrode 5a, the solid electrolyte 5b, and the oxygen side electrode 5c overlap is present at the center of the power generation chamber 16 as shown in FIG. 1, and the oxygen side electrode 5c is located at both ends of the fuel cell 5. Is not formed, and both end portions of the fuel cell 5 do not contribute to power generation. The lower end portion of the fuel cell 5 in which the oxygen side electrode 5 c is not formed is supported by the upper lid 10 of the fuel gas tank 8. The dense solid electrolyte 5b prevents gas mixing inside and outside the solid electrolyte 5b in the power generation chamber 16.

  In such a fuel cell, in order to generate electric power, it is necessary to supply an oxygen-containing gas to the outside of the fuel cell 5. Therefore, an oxygen-containing gas pipe 18 is connected to the storage container 1. In addition, it is necessary to supply a hydrogen-containing gas to the inside of the fuel battery cell 5. For this reason, the storage container 1 is connected to a gas introduction pipe 28 for supplying a gas necessary for the reforming reaction. The reformed gas introduced from the gas introduction pipe 28 is introduced into the fuel reformer 3, reformed into a gas containing hydrogen gas, and passes through the reformed gas supply pipe 22 and the gas tank chamber 24. Introduced into the fuel cell 5, the power generation unit of the fuel cell 5 causes an electrochemical reaction with the oxygen-containing gas described above, thereby contributing to power generation.

  Excess fuel gas that has not been used for power generation is mixed with the oxygen-containing gas and burned in the combustion section 25 above the fuel cell 5. The combustion heat is used to heat the fuel reformer 3 provided above the fuel cell 5, and the combustion gas is supplied from the exhaust gas pipe 26 provided on the upper side of the storage container 1 to the fuel cell. Exhausted to the outside.

  The fuel reformer 3 is formed of, for example, a heat-resistant metal, has a structure as shown in FIGS. 4A and 4B, and has a flow as shown in FIG. A reformed gas supply pipe 28a for supplying raw fuel such as natural gas subjected to desulfurization treatment to the fuel reformer 3, an oxygen-containing gas supply pipe 28b for supplying oxygen-containing gas, and water vapor or water are supplied. A water supply pipe 28c is connected.

Incidentally, FIG. 4 (b) illustrates a fuel reformer 3 of the present invention. As shown in FIG. 4B , the fuel reformer 3 may have a nested structure. FIG. 4A is a reference example of the fuel reformer 3.

  The three pipes may be directly connected to the fuel reformer 3, but the reformed gas, the oxygen-containing gas, and water vapor or water can be simultaneously introduced into the fuel reformer 3. Is important, and a multiple pipe structure may be used, or three pipes may be connected to form one pipe and connected.

  The fuel reformer 3 includes, for example, a water vapor generating and mixing unit 30 that integrates a water vapor generating unit 30a that generates water vapor and a gas mixing unit 30b that mixes gas when water is directly supplied, and a gas to be reformed. The gas is composed of a flow path 32, a reforming section 34, and a reformed gas flow path 36, and various gases introduced into the fuel reformer 3 pass through these flow paths and are then supplied to the reformed gas supply pipe 22. Led.

The steam generation and mixing unit 30 is filled with a spherical body composed of a heat-resistant member that does not have catalytic ability such as Al ₂ O ₃ , for example, and turbulent flow is generated when gas flows through the gap between the spherical bodies, By using a spherical body in which a plurality of gas types are sufficiently mixed and a heat capacity and a heat transfer area are large, water vapor can be generated smoothly and the reformed gas can be preheated.

  Further, the steam generation / mixing unit 30 is filled with a noble metal catalyst 34a that is unlikely to cause carbon deposition, and a part of the functions of the steam generation / mixing unit 30 and the reforming unit 34 is shared.

  In the reforming section 34, the noble metal catalyst 34a and the base metal catalyst 34b are mixed, the noble metal catalyst 34a is unevenly distributed near the inlet from the reformed gas flow path 32, and the base metal catalyst 34b is otherwise present. Filled. The ratio of the noble metal catalyst 34 a is preferably about 5 to 30% with respect to the total volume of the reforming section 34.

  In order to improve the startability in these mixed states, it is preferable that the noble metal catalyst 34a is unevenly distributed on the inlet side of the reforming section 34 that first contacts with the reformed gas. It may be distributed.

The base metal catalyst 34b is preferably formed by supporting Ru on the surface of spherical Al ₂ O ₃ and the noble metal catalyst 34a is also formed by supporting the surface of the same spherical Al ₂ O _{3 with} a third component such as Mg. May be added.

  The reforming section 34 may be a single noble metal catalyst 34a or a single base metal catalyst 34b.

  By forming the reformed gas flow path 36 along the reforming section 34, heat exchange is performed between the reforming catalyst inlet vicinity and the reformed gas. By arranging a baffle plate or the like in the reformed gas channel 36 to increase the length of the channel and increase the heat transfer area from the reforming unit 34, the heat exchange efficiency is further increased.

  In addition, the reforming section 34 is formed at the highest temperature position in the fuel reformer 3, and the reformed gas flow path 36 is formed along the reforming section 34 to perform heat exchange with the reforming section 34. By forming the reformed gas channel 32 along the reformed gas channel 36, heat exchange occurs with the reformed gas, and the reformed gas is preheated.

  The gas flow at this time is preferably such that the gas to be reformed and the reformed gas flowing in the fuel reformer 3 face each other.

  In addition, by introducing a reformed gas at room temperature into the high temperature reforming section 34 that performs the reforming reaction, the catalyst temperature decreases and the reforming ability decreases. By forming the to-be-reformed gas flow path 32 along the line 34, heat exchange is performed between the reforming unit 34 and the to-be-reformed gas to preheat the to-be-reformed gas.

  Thereby, the temperature difference between the catalyst temperature and the reformed gas temperature is reduced, and the decrease in the catalyst temperature can be suppressed. Further, the object to be heat exchanged by the reformed gas may be a reformed gas.

  As described above, it is not always necessary to form the reformed gas flow path 32 and the reformed gas flow path 36 along the reforming portion 34, and either one or no gas flow path is formed, and the fuel is not formed. The reformer 3 may be composed of only the reforming unit 34.

  The reformed gas supply pipe 22 connected to the fuel gas tank 8 may be connected to a raw fuel supply pipe 41 that is branched in the middle and introduced into the desulfurizer 40. In this way, by partially circulating the reformed gas, it is possible to supply a trace amount of hydrogen necessary for hydrodesulfurization treatment in which the organic sulfur component is converted to hydrogen sulfide. As a method for adjusting the circulation rate, a flow meter may be used, but a method using an ejector is preferable.

  Similarly, by connecting the reformed gas supply pipe 22 to the to-be-reformed gas supply pipe 28a, the amount of steam or water supplied at the same time can be reduced, so that the large heat of vaporization accompanying the generation of steam can be reduced. , Improve thermal efficiency.

  The reformed gas that has passed through the fuel reformer 3 having such a structure is reformed into a hydrogen-containing gas, and the reformed gas generated in the reforming section 34 passes through the reformed gas flow path 36. It passes through and is discharged from the reformed gas supply pipe 22.

  The reformed gas supply pipe 22 is connected to the fuel gas tank 8, and the reformed gas is supplied to the fuel battery cell 5 via the fuel gas tank 8.

  The reformed gas can be used as fuel for an auxiliary heat source (heating device) described later by branching the reformed gas supply pipe 22 in the middle and distributing a part of the reformed gas.

  Similarly, by connecting to the reformed gas supply pipe 28a for supplying the reformed gas to the fuel reformer 3, the amount of oxygen-containing gas, water vapor or water supplied at the same time can be reduced.

  The reformed gas supply pipe 22 may be connected to the number of the fuel reformer 3 and the fuel cell stack 7, but may be branched by the number of the fuel cell stacks 7 in the middle. The shape, connection method, quantity, etc. of the supply pipe 22 are not particularly limited.

  A gas passage (not shown) is formed in the upper cover 10 of the fuel gas tank 8 to which the reformed gas is supplied, and this gas passage communicates with the fuel gas passage 11 of the fuel cell 5. It passes through the gas passage, the fuel gas passage 11 of the fuel battery cell 5 through the quality gas supply pipe 22 and the fuel gas tank chamber 24, and is introduced from the upper end of the fuel battery cell 5 into the combustion unit 25. An ignition device (not shown) is disposed in the combustion unit 25, and is ignited using this to discharge oxygen from the oxygen-containing gas pipe 18 and the upper end of the fuel cell 5. In addition, the surplus gas that was not used for power generation burns and diffuses.

  The fuel cell configured as described above is operated as follows, for example.

  At the start of the fuel cell, the temperature of the fuel reformer 3 is normal temperature. Therefore, from the normal temperature to the partial oxidation reaction start temperature, the reformed gas introduced into the fuel cell 5 via the fuel reformer 3 The reformed gas mixed with the oxygen-containing gas is combusted in the combustion section 25 near one end of the fuel battery cell 5, and the fuel reformer 3 is heated to the partial oxidation reaction start temperature.

  At this time, even if the fuel cell 5 itself is heated by the combustion and the reforming reaction starts inside the fuel cell 5, carbon deposition on the fuel cell 5 is caused by mixing the oxygen-containing gas. Can be prevented.

At this time, O ₂ / C needs to be larger than 0 and equal to or smaller than 1, and when O ₂ / C is small, carbon deposition is likely to occur. Therefore, control is performed so that O ₂ /C=0.4 to 1. It is desirable.

  Further, an auxiliary heat source (heating device) may be used instead of combustion, or both may be used together and heated to the same temperature.

  When the auxiliary heat source (heating device) is a burner, a part of the reformed gas may be used as the fuel, or the raw fuel or the gas to be reformed may be used.

  After the partial oxidation reaction start temperature is reached, the reformed gas mixed with the oxygen-containing gas starts the partial oxidation reaction, so that the fuel reformer 3 rises spontaneously without being heated from the outside by the reaction heat. It will be warmed up.

  When the auxiliary heat source (heating device) is used in this state, the heating from the auxiliary heat source (heating device) may be stopped.

  However, the heating by combustion at one end of the fuel cell 5 is indispensable for raising the temperature of the fuel cell, maintaining the temperature, and further maintaining the temperature of the fuel reformer 3 in a steady state, so that the combustion is continued. There is a need to.

  Therefore, in this temperature range, the fuel reformer 3 is heated by the reaction heat and combustion heat of the partial oxidation reaction.

  After reaching the temperature at which steam reforming is possible, in order to prevent deterioration in durability and destruction of the fuel reformer 3 and degradation of the performance of the reforming catalyst due to excessive heating due to the reaction heat and combustion heat of the partial oxidation reaction, The temperature of the fuel reformer 3 is controlled using an autothermal method in which a steam reforming reaction, which is an endothermic reaction, is performed simultaneously by mixing steam with the reformed gas mixed with the contained gas.

  When switching from the partial oxidation reforming method to the autothermal method, the autothermal method is based on the number of moles of oxygen atoms in the reformed gas based on the ratio of the fuel gas and oxygen-containing gas supplied by the partial oxidation reforming method. Each supply amount is gradually changed so that the sum of the number of moles of oxygen atoms in the oxygen-containing gas supplied when switching to the method and the number of moles of oxygen atoms in water vapor are equal.

  By performing the switching in this way, the reformed gas can be controlled. When the autothermal method is performed, the fuel gas, the oxygen-containing gas, and the water vapor are supplied in various amounts so that the optimum conditions are obtained according to the conditions of the fuel cell 5 and the fuel reformer 3. I do.

  When heating is required, the oxygen-containing gas ratio is increased and the water vapor ratio is decreased, so that the total amount of heat related to the reforming reaction is exothermic. By increasing the ratio, the reaction related to the reforming reaction is made an endothermic reaction, and temperature control is performed.

  After the fuel cell 5 is sufficiently heated and reaches a steady state where power generation is possible, the fuel reforming is performed by switching to the steam reforming method with the largest amount of hydrogen generation and the highest power generation efficiency. In this temperature range, the heating source is only combustion heat.

  In addition, when switching from the autothermal method to the steam reforming method, the fuel gas supplied by the autothermal method based on the ratio (S / C) of the fuel gas and steam required by the steam reforming method. The operation is performed by gradually changing the supply amounts of oxygen-containing gas and water vapor. The S / C at this time is preferably in the range of 1.5 to 3.5. By setting S / C to 1.5 or more from this range, carbon deposition can be suppressed, and performance deterioration and destruction of the reforming catalyst and the fuel battery cell 5 can be prevented. Moreover, by setting it as 3.5 or less, a water vapor partial pressure can be made appropriate and the fall of electric power generation performance can be prevented.

  In addition, fuel gas and oxygen-containing gas and / or steam are circulated at temperatures from normal temperature to the start of partial oxidation reaction or steam reforming reaction, or combined reforming reaction using both partial oxidation reaction and steam reforming reaction. Thus, even if the gas supplied to the fuel cell via the fuel reformer is reformed inside the fuel cell heated to a temperature higher than that of the fuel reformer, the gas is supplied to the fuel cell body. The effects of carbon deposition and the like can be reduced.

  Furthermore, steam is added at a temperature from which the fuel gas and oxygen-containing gas are circulated from room temperature and water does not condense until the combined reforming reaction using the partial oxidation reaction and steam reforming reaction starts. It is preferable to do. As a result, even in a state where the conversion rate is low immediately after reaching the temperature at which the combined reforming reaction starts, the gas composition generated by reforming is assumed to be inside the fuel cell heated to a higher temperature than the fuel reformer. Even if it is modified, it is possible to reduce the influence of carbon deposition or the like on the fuel cell. In addition, it is desirable to add water vapor | steam beforehand by the combined reform start temperature so that S / C of the gas composition produced | generated by modification | reformation may exist in the range of 1.5-3.5.

O ₂ / C at this time is desirably controlled to 0.4 to 1 in order to suppress carbon deposition, and the amount of steam S / C added up to the temperature at which the combined reforming reaction starts is secured. In order to make the partial pressure of water vapor suitable, it is desirable to control it to be within 3.

  By switching in this way, carbon deposition on the reforming catalyst and the fuel cell 5 is surely suppressed, and a rapid temperature change due to rapid start-up is further suppressed, so that the fuel cell and the fuel reformer 3 In addition to being able to operate under optimal conditions according to conditions, high power generation efficiency can be realized.

It is a schematic sectional drawing which shows the fuel cell of this invention. FIG. 2 is a schematic cross-sectional view of FIG. 1. It is sectional drawing for demonstrating the fuel cell stack of FIG. It is sectional drawing for demonstrating the fuel reformer of FIG. It is the schematic for demonstrating the fuel reformer of FIG.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 ... Storage container 3 ... Fuel reformer 5 ... Fuel cell 22 ... Reformed gas supply pipe 28a ... Reformed gas supply pipe 30 ... Steam generation mixing part 32- ..Reformed gas flow path 34 ... reforming part 36 ... reformed gas flow path

Claims (2)

To fix a plurality of columnar fuel cells having fuel gas passages along the longitudinal direction inside the storage container, and a lower end portion of the fuel cells, and to circulate the fuel gas through the fuel gas passages A fuel gas tank, a fuel reformer that is disposed on the upper end side of the fuel cell, and supplies fuel gas to the fuel cell, and a reformer that connects the fuel reformer and the fuel gas tank Containing the gas supply pipe,
The fuel reformer is connected to one end of a pipe for supplying a gas to be reformed and a pipe for supplying steam or water, and in order from the side to which the pipes are connected, The gas mixing section, the reformed gas flow path, the reforming section, and the reformed gas flow path are continuously provided and integrated,
Between the fuel cell and the fuel reformer is a combustion part for burning the fuel gas discharged from the upper end of the fuel cell,
In the fuel reformer, the reforming section, the reformed gas flow path, and the reformed gas flow path are stacked in order from the side closer to the combustion section,
The fuel cell, wherein the fuel reformer is directly exposed to combustion gas in the combustion section.   The fuel cell according to claim 1, wherein the reforming section is filled with a reforming catalyst in which a base metal catalyst and a noble metal catalyst are mixed.

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