JP2929034B2 - Molten carbonate fuel cell power generator - Google Patents

Description

Description: FIELD OF THE INVENTION The present invention relates to a power generation device for a combustion battery used in an energy sector for directly converting chemical energy of fuel into electric energy, and in particular, a molten carbonate fuel cell. It relates to a power generator.

[Prior Art] As a typical example of a natural gas reforming molten carbonate fuel cell power generator among conventional power generators using a molten carbonate fuel cell, as shown in a system diagram in FIG. The cathode 2 of the combustion battery I having a structure in which the electrolyte plate 1 is sandwiched between the cathode 2 and the anode 3 and both of which are stacked with a separator interposed therebetween is compressed by the compressor 4 and then cooled. Air A cooled by 5 and further compressed by a compressor 6 is preheated by an air preheater 7 and supplied by an air supply line 8 and a part of the air is supplied to a combustion chamber of a reformer 10 by a branch line 9. The cathode gas discharged from the cathode 2 is led to a turbine 12 through a cathode gas outlet line 11 and further discharged to the atmosphere through the air preheater 7. On the other hand, natural gas (CH ₄ ) NG is supplied to the anode 3 of the combustion battery I by the fuel gas preheater 1.
After reforming by introducing to the reformer 10 via 3, 14 and the desulfurizer 15,
The reformed gas is supplied from the fuel gas supply line 16 as the natural gas FG, and the anode gas discharged from the anode 3 is supplied to the heat exchanger 17, the natural gas preheater 14, the evaporator 18,
After passing through the natural gas preheater 13, it is cooled and condensed in the condenser 19 and led to the gas-liquid separator 20, where H ₂ O in the anode gas is
After the gas is pressurized by the blower 21, the gas is led to the combustion chamber side of the reformer 10 through the line 22 to the heat exchanger 17, and is supplied from the reformer 10 to the cathode 2. The separated H ₂ O is pressurized by a pump 23 and sent to a feed water heater 24, where it is heated and vaporized as steam.
25, natural gas NG at the inlet side of the reformer 10 via the evaporator 18
So that it can be mixed with 26 is a cathode recycling blower.

When the molten carbonate fuel cell is operated to generate power, natural gas (CH ₄ ) is reformed and supplied to the anode 3. In the reformer 10, CH ₄ + H ₂ O → CO + 3H ₂ Is performed.

At the cathode 2 side of the fuel cell _{I, CO 2 + 1 / 2O} 2 + 2e - → CO 3 - the reaction is performed, the carbonate ion CO ₃ ^- is produced, the carbonate ion CO ₃ ^- electrolyte plate 1 It reaches the anode 3 through the inside. The anode 3 side and reformed fuel gas is supplied by the reformer 10 above carbonate ion CO ₃ ^- it comes into contact ^{_{with, CO 3 - + H 2 →}} CO 2 + H 2 O + 2e - CO 3 - + CO → 2CO ₂ + 2e ^- reaction is carried out in, 5CO ₂ + 3H ₂ O is to be discharged as the anode gas.

[Problems to be Solved by the Invention] However, in the above-mentioned molten carbonate fuel cell power generator, in order to increase the power transmission end efficiency of the power generation system,
Although it is necessary to increase the fuel utilization rate at the anode 3, the cells in each stage are not necessarily uniform in the cell stacking direction of the battery as shown in FIG.
As shown in the figure, when the electrode area is large, the fuel flow distribution may be uneven. These non-uniform flow rates cause a shortage of fuel in a portion of the cell under conditions of high fuel utilization, causing a voltage drop. Therefore, conventionally, in order to operate the battery in a stable state, the fuel utilization rate has to be reduced to a certain value or less. Moreover, in the conventional power generation device, the heat generated by the battery is cooled by using the sensible heat of the cathode, so that the inlet temperature of the fuel cell I cannot be made too high. The S / C (steam / carbon) ratio cannot be reduced to prevent this.
In fact, about = 3 is adopted.

Therefore, the present invention is to improve the fuel utilization rate as a whole in a fuel cell power generator so that the efficiency of the power transmission end can be increased even when the one-pass fuel utilization rate is low, and to improve the fuel flow distribution. In addition, the operating temperature of the battery is increased, and the amount of water vapor required for reforming the reforming raw material gas can be reduced. Further, unreacted components contained in the anode gas are burned by the reformer to obtain the gas. It is intended to increase the amount of recovered steam by using the generated heat for generating steam.

[Means for Solving the Problems] In order to solve the above-mentioned problems, the present invention provides a plurality of molten carbonate fuel cells and a plurality of reformers, and performs reforming of an upstream reformer. Chamber, the anode of the upstream fuel cell, the reforming chamber of the downstream reformer, and the anode of the downstream fuel cell are connected in series so that the gas flows in that order, and the anode and the cathode of the downstream fuel cell are connected. Only each outlet side is connected to the combustion chamber of the downstream reformer via a catalytic combustor, and further, the combustion heat of the combustion chamber of the downstream reformer is transferred to the combustion chamber of the upstream reformer. The combustion chambers of the upstream and downstream reformers are connected by lines so as to be used as a heating source.

Furthermore, a plurality of molten carbonate fuel cells and a plurality of reformers are installed, and the reforming chamber of the upstream reformer, the anode of the upstream fuel cell, and the reforming of the downstream reformer are provided. Chamber, connected in series so that gas flows in the order of the anode of the fuel cell on the downstream side,
A cathode gas outlet line is connected to introduce the cathode gas discharged from the cathode of the upstream fuel cell into the combustion chamber of the upstream reformer, and the cathode gas is discharged from the combustion chamber of the upstream reformer. An exhaust gas line is provided to supply the exhaust gas to the cathode of the downstream fuel cell, and only the outlets of the anode and the cathode of the downstream fuel cell are provided with a catalytic combustor in the combustion chamber of the downstream reformer. In this configuration, the exhaust gas line is passed through a steam generator so that the heat of the combustion chamber of the downstream reformer is used as a heat source for generating steam. A steam line is provided so as to supply to the upstream reformer inlet side for raw material reforming.

[Operation] When a plurality of fuel cells are connected in series and the fuel gas reformed in the reforming chamber of the reformer is supplied to the anode of the upstream fuel cell, the anode of the upstream fuel cell uses fuel. Even if the rate is low, the unused fuel is used at the anode of the fuel cell on the downstream side, so that the fuel utilization rate as a whole can be increased, and since the gas flow rate at the anode side is small, the gas flow rate distribution is improper. However, if the fuel cells are arranged in series, the amount of gas passing through the anode increases,
The gas flow distribution is improved. On the other hand, only a part of the anode gas from the anode of the downstream fuel cell and a part of the cathode gas from the cathode are supplied to the combustion chamber of the reformer, and are supplied through the catalytic combustor. Thermal reforming can be performed. A plurality of reformers and a plurality of fuel cells are alternately installed, and the reforming chamber of the upstream reformer, the anode of the upstream fuel cell, the reforming chamber of the downstream reformer, and the downstream When connected in series in the order of the anode of the fuel cell, the anode of the fuel cell on the upstream side consumes hydrogen in the fuel gas by the anode reaction, and the generated steam required for reforming is reformed in the downstream reformer. Since it is supplied to the chamber, the reforming rate of the downstream reformer can be increased, and accordingly, the amount of steam for reforming supplied to the raw material can be reduced and the S / C ratio can be reduced. Can be. Further, by utilizing the sensible heat of the cathode gas emitted from the cathode of the upstream fuel cell as a heat source of the upstream reformer, the cathode gas can be intercooled using the upstream reformer as a cooler, so that the fuel When the batteries are arranged in series, a cooler installed on the cathode outlet side of the upstream fuel cell can be omitted. Further, the amount of recovered steam can be increased by inputting the heat generated by burning the unreacted components at the anode of the downstream fuel cell in the downstream reformer to the steam generation.

Embodiments Hereinafter, embodiments of the present invention will be described with reference to the drawings.

FIG. 1 shows a cell in which an electrolyte plate 1 is sandwiched between both electrodes of a cathode 2 and an anode 3 to supply air A as an oxidizing gas to the cathode 2 and a fuel gas FG to the anode 3 side. Are stacked to form a stack by interposing a separator (not shown)
The case of connecting them in series will be described.

That is, the fuel cells I and II are installed, and the anode 3 of the fuel cell I on the upstream side and the anode 3 of the fuel cell II on the downstream side are installed.
Are connected in series, and a supply line 31 for the fuel gas FG reformed by the reformer 30 is connected to the anode 3 and the inlet side of the fuel cell I, and natural gas NG as a reforming raw material gas is
After being desulfurized by the desulfurizer 33 on the natural gas supply line 32 and then supplied to the reforming chamber 30a of the reformer 30 via the natural gas preheater 34, it is reformed in the reforming chamber 30a of the reformer 30. The fuel is supplied to the anode 3 of the fuel cell I on the upstream side, and the fuel is sequentially used by the anodes 3 of the fuel cells I and II connected in series, from the anode 3 of the fuel cell II on the downstream side. The discharged anode gas is supplied to the combustion chamber 30b of the reformer 30 through the catalytic combustor 61 at the anode gas outlet line 35. On the other hand, the air A as the oxidizing gas passes through the filter 36, is pressurized by the air blower 38 on the air supply line 37, is heated by the air preheater 39, and is supplied to the cathode 2 of the fuel cell I on the upstream side. In this way, the cathode gas that has exited the cathode 2 of the fuel cell I is cooled by the cooler 40 and supplied to the cathode 2 of the fuel cell II on the downstream side, and is discharged from the cathode 2 of the fuel cell II. The high-temperature cathode gas is branched from the cathode gas outlet line 41 and a part is introduced into the combustion chamber 30b of the reformer 30 through the catalytic combustor 61 from the outlet branch line 42, and the remaining portion is introduced. The cathode gas is discharged from the cathode gas outlet line 41 to the atmosphere through the air preheater 39, and a part of the air is supplied to the air supply line by a cathode gas blower 43 for recycling.
Return to 37 for recycling. Further, the gas discharged from the combustion chamber 30b of the reformer 30 is supplied to an exhaust gas line 44.
More steam superheater 45, steam generator 46, reforming steam generator 4
7, through the condenser 48 so as to guide the gas-liquid separator 49, the gas-liquid separator 49, the clean water H ₂ O to each other so as to supply treated with the water treatment device 50, gas-liquid The water separated by the separator 49 is pressurized by the feed water pump 51 together with the tap water H ₂ O, and guided to the steam generator 46, the reforming steam generator 47, and the steam generator 46. The generated steam can be recovered from the steam recovery line 52, and the steam generated by the reforming steam generator 47 is superheated by the steam superheater 45 to be led from the steam line 53 to the natural gas supply line 32. The excess reforming steam is returned to the upstream side of the condenser 48, and the gas separated by the gas-liquid separator 49 is supplied to the gas-liquid separator 49 so as to be absorbed by the air supply line 37. The top portion is connected to the air supply line 37 on the air blower 38 inlet side.
Incidentally, in the combustion chamber 30b of the reformer 30, there is a case where only the heating gas passes without combustion.

When natural gas NG is reformed into fuel gas FG in the reformer 30,
Fuel gas FG is supplied to the anode 3 of the fuel cell I of the upstream side, where it is produced by reaction at the cathode 2 side carbonate electrolyte plate 1 came to as electrophoretic CO ₃ ^- and reaction Is performed and fuel is used. The anode gas discharged from the anode 3 of the fuel cell I on the upstream side is supplied to the anode 3 of the fuel cell II on the downstream side as it is, where the reaction using unused fuel is performed at the anode 3 on the upstream side. Are discharged. At this time, since the anodes 3 of the fuel cells I and II are connected in series, the total fuel utilization can be increased even if the fuel utilization at each anode 3 is low.
For example, the fuel utilization at anode 3 of fuel cells I and II
Assuming that both Vf are 70%, in fuel cell I, 100% × 0.7 = 70% In fuel cell II, (100−70)% × 0.7 = 21%, and a high fuel utilization rate of 91% is obtained in total. Will be. Since the fuel utilization rate can be increased in this way, it is possible to increase the power transmission end efficiency of the system.In this case, the fuel utilization rate of one-pass of the plurality of fuel cells I and II connected in series is as described above. As described above, it is not necessary to increase the height of the fuel cell. Therefore, as shown in FIG. 4 and FIG. No voltage drop occurs.

In addition, the flow rate of the gas supplied to the anode of the fuel cell is generally smaller than that of the cathode gas, so that the distribution of the flow rate is not uniform. However, when the fuel cells I and II are arranged in series, the fuel cells are arranged in parallel. The amount of anode gas passing through each cell is greater in the series arrangement than in the arrangement. Therefore, the flow distribution of the anode gas is improved.
When the fuel cells are arranged in series as described above, a cooler 40 is installed on the outlet side of the cathode 2 of the upstream fuel cell I, and the cathode gas cooled by the cooler 40 is supplied to the cathode 2 of the downstream fuel cell II. The amount of cathode gas on the upstream side can be directly supplied to the cathode on the downstream side by supplying the gas to the downstream side.Therefore, when the fuel cells are arranged in parallel, the total cathode gas flow rate is smaller than the total gas amount flowing through each cathode. With the decrease in the amount of cathode gas, the CO ₂ concentration in the cathode gas increases, the battery voltage increases, and the power of the cathode gas blower for recycling can be reduced. Furthermore, assuming that the cathode gas flow rate is the same as the total gas flow rate when the fuel cells I and II are arranged in series and the fuel cells are arranged in parallel, the gas flow rate increases in the series arrangement. Therefore, the temperature difference between the inlet side and the outlet side of the battery cell can be reduced by the amount.
Now, assuming that the outlet temperature of the battery cell is the same whether the fuel cells I and II are arranged in series or arranged in parallel due to electrolyte loss, if the fuel cells I and II are arranged in series, they pass through the battery cell. Since the gas amount increases as compared with the parallel arrangement and the temperature difference between the inlet side and the outlet side can be reduced as described above, the inlet side temperature of the battery cell increases. As a result, the operating temperature of the battery increases, and the battery voltage can be increased. Also, as the operating temperature of the battery is higher, the carbon deposition reaction (2CO → CO ₂ + C) at the anode inlet is less likely to occur, so that the operating temperature of the battery can be increased to lower the S / C ratio. Therefore, even if the amount of steam required for reforming is reduced and the S / C ratio is reduced, there is no concern about carbon deposition at the anode inlet, so the amount of steam for reforming can be reduced and the efficiency of the system increased. Can be.

The sensible heat of the gas discharged from the combustion chamber 30b of the reformer 30 is supplied to a steam superheater 45, a steam generator 46, and a reforming steam generator 47 in order to generate steam, and is used for steam generation. The generated steam is mixed into the natural gas NG through the steam line 53.

FIG. 2 shows an embodiment of the present invention. In a configuration in which fuel cells I and II are connected in series similarly to FIG. 1, another reformer 54 is provided in addition to the reformer 30. The reforming chamber 30a of the reformer 30 on the upstream side, the anode 3 of the fuel cell I on the upstream side, the reforming chamber 54a of the reformer 54 on the downstream side, and the anode 3 of the fuel cell II on the downstream side A fuel gas supply line 31 connects the reforming chamber 30a of the reformer 30 and the inlet side of the anode 3 of the fuel cell I to the anode 3 of the fuel cell I so that they are connected in series in this order.
Between the outlet side of the reformer 54 and the inlet side of the reforming chamber 54a of the reformer 54.
Also, the outlet side of the reforming chamber 54a of the reformer 54 and the inlet side of the anode 3 of the downstream fuel cell II are connected by a fuel gas supply line 57, respectively, and the anode of the downstream fuel cell II is connected. The anode gas discharged from the reactor 3 is supplied to the combustion chamber 54b of the reformer 54 on the downstream side via the anode gas outlet line 35 in the catalytic combustor 61.
And the combustion chamber 30b of each of the upstream and downstream reformers 30 and 54 to use the heat of combustion of the downstream reformer 54 as a heating source of the upstream reformer 30. 54b are connected to each other by a line 58, and an exhaust gas line 44 is arranged so that sensible heat of the gas discharged from the upstream reformer 30 is used for steam generation. Other configurations are the same as those shown in FIG.
The same components as those shown in FIG. 1 are denoted by the same reference numerals.

According to the practical example shown in FIG. 2, a plurality of reformers 30, 54
And the raw material gas is supplied from the upstream reformer 30 to the fuel cell I.
Flows through the anode 3 to the reformer 54 on the downstream side. In addition to the advantages obtained in the practical example shown in FIG. The reforming rate may be lower than that of the upstream reformer 54.Therefore, the heat source of the upstream reformer 30 uses another heat source besides utilizing the combustion heat of the downstream reformer 54 as shown in the figure. It is also possible to use it. Further, although a high reforming rate is required in the downstream reformer 54, hydrogen is generated by the reaction at the anode 3 of the fuel cell I on the upstream side.
H ₂ is consumed and steam H ₂ O required for reforming generated in the reaction
Is supplied to the reforming chamber 54a of the downstream reformer 54, and the reformer 54 burns unreacted components in the anode gas discharged from the anode 3 of the fuel cell II on the downstream side. Since this is used as the heat source, the reforming heating temperature is high, and the reforming rate can be increased in the reformer 54 on the downstream side. Further, since the steam required for reforming is supplied from the anode 3 of the upstream fuel cell I to the downstream reformer 54, the amount of reforming steam supplied to the raw material can be reduced, The S / C ratio can be reduced. If this S / C ratio is reduced, carbon deposition may occur at the anode inlet of the fuel cell. However, the operating temperature of the cell is increased to prevent the carbon deposition reaction from occurring.

FIG. 3 shows another embodiment of the present invention. As in the embodiment shown in FIG. 2, a plurality of reformers 30 and 54 and a plurality of fuel cells I and II are alternately installed. A configuration in which the reforming chamber 30a of the upstream reformer 30, the anode 3 of the upstream fuel cell I, the reforming chamber 54a of the downstream reformer 54, and the anode 3 of the downstream fuel cell II are connected in series. , The cathode gas outlet line 59 of the cathode 2 of the upstream fuel cell I is connected to the upstream reformer
30 and the combustion chamber 3 of the reformer 30.
0b and the cathode 2 inlet side of the downstream fuel cell II are connected by an exhaust gas line 60, and the other configuration is the same as that of the embodiment shown in FIG. The code is attached.

According to the embodiment shown in FIG. 3, in addition to the advantages obtained in the embodiment shown in FIG.
Since the reforming rate may be lower than that in the case of 54, the sensible heat of the cathode gas of the upstream fuel cell I is used as the heat source of the upstream reformer 30 so that the exhaust gas Is supplied to the cathode 2 of the fuel cell II on the downstream side, so that the sensible heat of the cathode gas of the fuel cell I on the upstream side is used as a heat source required for reforming in the upstream reformer 30. By this, it is possible to reduce the heating fuel for reforming, and at the same time, the cathode gas having the cooling effect of the fuel cell is cooled using the upstream reformer 30 as an intermediate cooler, Since it is supplied to the cathode 2 of the fuel cell II,
After omitting the cooler 40 in each of the above-described embodiments, the same operation and effect as those in the above-described embodiments can be obtained.Furthermore, in this embodiment, since the amount of heat required for the reforming of the downstream reformer 54 is small, In addition, a heating source can be used for generating steam, and the amount of generated steam increases, so that the amount of recovered steam can be increased.

Note that the present invention is not limited to only the above-described embodiment. For example, two fuel cells I and II are shown as a plurality of fuel cells, and two reformers are shown as a plurality of reformers. Although the reactors 30 and 54 are shown, three or more of them may be installed and connected in series. In the embodiment of FIG. 2, the inlet side of the combustion chamber 30b of the upstream reformer 30 is used. It may be possible to supply another heat source, and the exhaust gas line 44 may be connected to the outlet side of the combustion chamber 54b of the downstream reformer 54, as long as it does not deviate from the gist of the present invention. Of course, various changes can be made.

[Effects of the Invention] As described above, according to the molten carbonate fuel cell power generator of the present invention, a plurality of fuel cells and a plurality of reformers are installed, and the reforming of the upstream reformer is performed. Chamber, the anode of the upstream fuel cell, the reforming chamber of the downstream reformer, and the anode of the downstream fuel cell are connected in series in this order, and the fuel gas reformed in the upstream reformer is sequentially turned on at each anode. After utilization, the fuel is introduced into the fuel of the downstream reformer, so that the fuel utilization as a whole can be increased without increasing the fuel utilization at each fuel cell anode. In addition, the efficiency of the power generation end can be increased, and the amount of anode gas passing through each battery cell is greater in a series arrangement than in a case where fuel cells are arranged in parallel. Anode gas with low uniformity of flow distribution By further supplying only a part of the anode gas from the anode of the downstream fuel cell and a part of the cathode gas from the cathode to the combustion chamber of the reformer through the catalytic combustor, Sensible heat reforming. or,
When the fuel cells are arranged in series and the cooler is placed between the upstream and downstream cathodes, the total amount of gas when passing through each battery cell is reduced compared to the case where the fuel cells are arranged in parallel. Since the amount of gas can be reduced, the concentration of CO ₂ in the gas increases with the decrease in the amount of gas, so that the cell voltage can be increased.In addition, the power of the cathode gas blower for recycling can be reduced, and the fuel cell can be used. If the same amount of cathode gas as the total amount of cathode gas in the parallel arrangement is made to flow in the series arrangement of the fuel cells, the amount of cathode gas passing through each battery cell can be increased,
As a result, the battery inlet temperature can be increased, the temperature difference between the inlet and outlet can be reduced, and the operating temperature of the battery can be increased.Accordingly, the battery voltage can be increased, the efficiency can be improved, and the temperature required for reforming can be improved. S / C (steam /
If the (carbon) ratio is reduced, a carbon deposition reaction may occur at the fuel cell anode inlet, but the carbon deposition reaction is less likely to occur due to the higher operating temperature of the cell, and the S / C ratio can be reduced. The fuel concentration at the anode can be increased and the steam consumption can be reduced, thereby increasing the efficiency of the system. In addition, as described above, the source gas flows in the order of the reforming chamber of the upstream reformer, the anode of the upstream fuel cell, the reforming chamber of the downstream reformer, and the anode of the downstream fuel cell. As a result, the reforming rate of the upstream reformer may be low, so that anything can be used as a heat source for reforming, and hydrogen is consumed by the anode reaction of the upstream fuel cell and generated by the reaction, and steam is generated by the downstream reaction. Since it is supplied to the reformer for reforming, the reforming rate can be increased in the downstream reformer, and the amount of steam for reforming can be reduced at the same time. Can be smaller. Further, as a heat source of the upstream reformer, the sensible heat of the cathode gas of the upstream fuel cell may be used,
By using the sensible heat of the exhaust gas discharged from the combustion chamber of the downstream reformer, the heating fuel in the reformer can be reduced, and The exhaust gas from the combustion chamber of the reformer is configured to be supplied to the cathode of the downstream combustion cell, so that the cathode gas is cooled by the reformer. The same effect can be obtained by omitting the cooler provided between the cathodes.

[Brief description of the drawings]

FIG. 1 is a system diagram showing an outline of an embodiment of a molten carbonate fuel cell power generator according to the present invention, FIG. 2 is a system diagram showing an outline of another embodiment of the present invention, and FIG. FIG. 4 is a schematic diagram showing still another embodiment of the fuel cell system, FIG. 4 is a diagram showing a non-uniform state of fuel flow distribution in each cell of the fuel cell, and FIG. 5 is a fuel flow in a single cell. FIG. 6 is a schematic diagram showing an example of a system configuration of a conventional natural gas reforming molten carbonate fuel cell power generation system. I, II: molten carbonate fuel cell (fuel cell), 2: cathode, 3: anode, 30: upstream reformer (reformer), 30a: reforming chamber, 30b ... combustion chamber, 31 ... fuel gas supply line, 35 ... anode gas outlet line, 37 ... air supply line, 41 ... cathode gas outlet line, 42 ...
Outlet branch line, 43: Cathode gas blower for recycling, 44: Exhaust gas line, 45: Steam superheater, 46: Steam generator (steam generator), 47: Steam generator for reforming (steam generation) ), 53 ... steam line, 54 ... downstream reformer, 54a ... reforming chamber, 54b ... combustion chamber, 55 ... anode gas outlet line, 57 ... fuel gas supply line, 58 ...
... line, 60 ... exhaust gas line, 61 ... catalytic combustor.

──────────────────────────────────────────────────続 き Continuing on the front page (72) Inventor Hiromasa Morimoto 3-1-1, Toyosu, Koto-ku, Tokyo Ishikawa Shima-Harima Heavy Industries Co., Ltd. Tokyo Second Plant (72) Inventor Satoshi Hajima 3-Toyosu, Koto-ku, Tokyo No. 1-115, Ishikawa Shima-Harima Heavy Industries Co., Ltd., Tokyo No. 2 Factory (72) Inventor Hiroshi Agematsu 3-1-1, Toyosu, Koto-ku, Tokyo Ishikawa Shima-Harima Heavy Industries Co., Ltd., Tokyo No. 2 Factory (72) Inventor Satoshi Hikita 2-10-21 Hiyoshi, Kohoku-ku, Yokohama-shi, Kanagawa (72) Inventor Kenichi Shinozaki 4-1-2, Hirano, Chuo-ku, Osaka-shi, Osaka Inside Osaka Gas Co., Ltd. (72) Shigeru Nakagawa, inventor 507-1 Shinhocho, Tokai City, Aichi Prefecture Toho Gas Co., Ltd. (56) References JP-A-59-149663 (JP, A) JP-A-63-126173 (JP, A) JP-A-2-170368 ( P, A) JP flat 1-105475 (JP, A) (58 ) investigated the field (Int.Cl. ^6, DB name) H01M 8/00 - 8/24

Claims (3)

(57) [Claims] 1. A plurality of molten carbonate fuel cells and a plurality of reformers are installed, a reforming chamber of an upstream reformer, an anode of an upstream fuel cell, and a downstream reformer. Are connected in series so that gas flows in the order of the reforming chamber and the anode of the downstream fuel cell, and only the respective outlets of the anode and cathode of the downstream fuel cell are connected to the combustion chamber of the downstream reformer. Connected via a combustor, and each of the upstream and downstream reformers so that the combustion heat of the combustion chamber of the downstream reformer is used as a heating source of the combustion chamber of the upstream reformer. Wherein the combustion chambers are connected by a line. 2. A plurality of molten carbonate fuel cells and a plurality of reformers are installed, a reforming chamber of an upstream reformer, an anode of an upstream fuel cell, and a downstream reformer. Are connected in series so that gas flows in the order of the reforming chamber and the anode of the downstream fuel cell, and the cathode gas discharged from the cathode of the upstream fuel cell is introduced into the combustion chamber of the upstream reformer. A cathode gas outlet line is connected so that the exhaust gas discharged from the combustion chamber of the upstream reformer is supplied to the cathode of the downstream fuel cell, and an exhaust gas line is provided.
A molten carbonate fuel cell power generator having a configuration in which only the outlets of the anode and cathode of the downstream fuel cell are connected to the combustion chamber of the downstream reformer via a catalytic combustor. . 3. A plurality of molten carbonate fuel cells and a plurality of reformers are installed, a reforming chamber of an upstream reformer, an anode of an upstream combustion cell, and a downstream reformer. The cathode gas outlet is connected in series so that the gas flows in the order of the reforming chamber and the anode of the downstream combustion cell, and the cathode gas of the upstream combustion cell is introduced into the combustion chamber of the upstream reformer. Along with connecting the lines, an exhaust gas line is provided so as to supply exhaust gas discharged from the combustion chamber of the upstream reformer to the cathode of the downstream combustion cell, and each of the anode and cathode of the downstream combustion cell is provided. Only the outlet side is connected to the combustion chamber of the downstream reformer via the catalytic combustor, and further, the exhaust gas line is connected to the steam generator so that the heat of the combustion chamber of the downstream reformer is used as a heat source for generating steam. Through steam, and part of the generated steam is reformed as raw material Molten carbonate fuel cell power plant characterized by having a disposing composed constituting steam line to supply the upstream to the reformer inlet side as.