Operation method for power generation system using fuel cell

Abstract: Anode gas is fed to an anode chamber (3) of a molten carbonate fuel cell (I) and cathode gas is fed to a cathode chamber (2) of the fuel cell (I). CO₂ is separated from gases discharged from the cathode chamber (2) of the fuel cell (I) by a CO₂ separator (27) or by another fuel cell (II) which serves as the CO₂ separator. The separated CO₂ is entirely or partially is introducted to the cathode chamber (2) with gases discharged from the anode chamber (3) such that a CO₂ concentration in the cathode chamber (2) is raised and the power generation is performed at a low CO₂ utilization factor mode.

Description: The present invention relates to a method of operating a power generation system using a fuel cell including molten carbonate, and particularly relates to an operation method for such a system to achieve a high efficiency power generation. A known molten carbonate-type fuel cell generally includes a plurality of fuel cell elements. Each fuel cell element includes an electrolyte plate (tile), a cathode (oxide electrode) and an anode (fuel electrode). The electrolyte plate includes a porous substance soaked with molten carbonate, and the cathode electrode and the anode electrode sandwich the electrolyte plate. A cathode chamber is formed in the cathode electrode and an anode chamber is formed in the anode electrode. Oxidizing gas is fed to the cathode chamber whereas fuel gas is fed to the anode chamber to cause power generation due to an electric potential difference between the cathode electrode and the anode electrode. A plurality of fuel cell elements are stacked one after another with separators being interposed between each two fuel cell elements. From US 4,080,487 a fuel cell power plant is known, comprising a plurality of stacks of molten carbonate fuel cells, the CO₂ produced at the anodes of the cells is combined with the process air of the cathode side of the stacks. The CO₂ rich mixture is fed from stack to stack in series through the cathode sides thereof with heat being removed from the cathode side exhaust streams between consecutive stacks. In this process it is intended to increase the partial pressure of CO₂ within the stacks. Amoung power generation systems using the fuel cell of the above-mentioned type, a typical natural gas reforming type power generation system is illustrated in Figure 11. An electrolyte plate 1 is sandwiched by a cathode and an anode. A cathode chamber 2 is provided over the cathode and an anode chamber 3 is provided over the anode to form a fuel cell I. Part of air A is pressurized by a compressor 4, cooled by a cooling device 5, pressurized again by another compressor 6 and preheated by an air preheater 7 before introduced to the cathode chamber 2 through an air feed line 8. Remaining part of the air A is introduced to a combustion chamber of a reformer 10 by a branch line 9. Gases discharged from the cathode chamber are introduced to a turbine 12 through a cathode exhaust gas line 11 and then expelled to atmosphere via the air preheater 7. On the other hand, natural gas (CH₄) NG flows through a natural gas preheater 13 and 14, a desulfurizer 15 and the reformer 10. The natural gas NG is reformed to fuel gas FG in the reformer 10 and the fuel gas FG is fed to the anode chamber 3 of the fuel cell I. Gases discharged from the anode chamber 3 are led to a heat exchanger 17, the natural gas preheater 14, a heating device 18, the natural gas preheater 13 and a condenser 19. The gases are cooled in the the condenser 19 and introduced to a gas-liquid separator 20. In the gas-liquid separator 20, H₂O is separated from the gases (anode exhaust gas), and then the gases are pressurized by a blower 21, introduced to the combustion chamber of the reformer 10 through a line 22 extending to the heat exchanger 17 and fed into the anode chamber 2 from the reformer 10. The separated H₂O is compressed by a pump 23 and led to a water heater 24 to become steam. The steam flows through the steam generator 18 and merges with the natural gas NG at an entrance of the reformer 10. Numeral 26 designates a blower used for a cathode recirculation. When the molten carbonate fuel cell is operated for power generation, the natural gas (CH₄) is reformed and fed is the anode chamber 3. In this case, a following reaction takes place in the reformer 10: CH₄ + H₂O --> CO + 3H₂ In the cathode chamber 2 of the fuel cell I, on the other hand, a following reaction takes place: CO₂ + 1/2O₂ + 2e⁻ --> CO₃⁻⁻ In the latter reaction, a carbonate ion CO₃⁻⁻ is produced and this carbonate ion CO₃⁻⁻ reaches the anode via the electrolyte plate 1. In the anode, the fuel gas reformed by the reformer 10 is introduced and contacts the carbonate ion CO₃⁻⁻, thereby causing following reactions: CO₃⁻⁻ + H₂ --> CO₂ + H₂O + 2e⁻ CO₃⁻⁻ + CO --> 2CO₂ + 2e⁻ Therefore, 5CO₂ and 3H₂O are discharged as the anode exhaust gas. In this manner, upon the power generation in the molten carbonate fuel cell, CO₂ is absorbed in the cathode whereas the same amount of CO₂ is produced in the anode. This can be said, at least apparently, that CO₂ is separated from the cathode gas and the separated CO₂ is transferred to the anode. In the reaction at the cathode 2, if the CO₂ concentration at the cathode is high, the reaction is accelerated and the fuel cell voltage becomes higher so that the power generation efficiency will be raised. However, in the conventional molten carbonate type fuel cell system, CO₂ among the anode exhaust gas discharged from the anode chamber 3 is introduced to the cathode chamber 2 to feed necessary CO₂ to the cathode chamber 2 and CO₂ recirculatedly fed to the cathode chamber 2 is diluted by the air. Therefore, the CO₂ concentration at the entrance of the cathode chamber 2 is very low, for example 7% which is considerably lower than a standard concentration of 30%. Consequently, the cell voltage is lower. A primary object of the present invention is to provide an operation method for a power generation system using a molten carbonate fuel cell for improving a power generation efficiency by raising a concentration of CO₂ fed to a cathode chamber of the fuel cell to lower a utilization factor of CO₂ and to maintain a CO₂ partial pressure at a proper level. Another object of the present invention is to provide a power generation system using a fuel cell operation method for lowering the CO₂ concentration of a cathode exhaust gas discharged to atmosphere. These objects are reached with a method as claimed in claim 1, 2 or 3. According to one aspect of the present invention, there is provided a power generation system operation method using at least two molten carbonate fuel cell including an electrolyte plate sandwiched by a cathode and an anode chamber. In such a case, gases containing a large amount of CO₂ are forced to go to a cathode chamber of a downstream fuel cell from a cathode chamber of an upstream fuel cell. CO₂ among an anode exhaust gas discharged from the anode chamber of the downstream fuel cell is entirely or partially fed to the cathode chamber of the upstream fuel cell with CO₂ among an anode exhaust gas discharged from the upstream fuel cell. In addition, part of the cathode exhaust gas discharged from the cathode chamber(s) of one or both of the upstream and the downstream fuel cells is recirculated to its or their own cathode chamber entrance(s) to lower the CO₂ utilization factor at the cathode. In the case where at least two molten carbonate fuel cells are used, cathode chambers of two fuel cells are connected to each other in series, an upstream fuel cell is operated in a low CO₂ utilization factor mode and excessive CO₂ is fed to a cathode chamber entrance of a downstream fuel cell from a cathode chamber exit of the upstream fuel cell, CO₂ is used for the reaction at the cathode and the CO₂ separation is carried out during the power generation. As CO₂ among the anode exhaust gas discharged from the anode chamber of the downstream fuel cell is recirculated to the cathode chamber of the upstream fuel cell, the CO₂ concentration in the cathode chamber is raised so that the CO₂ utilization factor is lowered. At the same time, the CO₂ partial pressure can be maintained at a proper level so that the reaction in the cathode is promoted and the power generation efficiency is raised. In the foregoing method, if CO₂ is recirculated from the cathode chamber exit to the cathode chamber entrance of one or both of the upstream and the downstream fuel cells, the CO₂ utilization factor at the cathode drops and desired operation conditions for an entire system can be selected. Other objects and advantages of the present invention will be apparent from the dependent claims and from the following detailed description taken in connection with the accompanying drawings. Figure 1 shows a relation between a CO₂ concentration at a cathode chamber entrance, a CO₂ utilization factor and a generated voltage; Figure 2 shows a schematic diagram of a power generation system to carry out a method of first embodiment of the present invention; Figure 3 shows a system diagram modified from Figure 3; Figure 4 shows a system diagram when an amount of CO₂ contained in fuel gas is relatively small as compared with the system of Figure 4; Figure 5 is a schematic system diagram wherein a cathode recirculation technique is used in the embodiment of Figure 2; Figures 6, 7 and 8 respectively illustrate a system diagram wherein the cathode recirculation technique is used in the embodiment of Figure 2; Figure 9 schematically illustrates a system diagram of another embodiment of the present invention; Figure 10 also schematically illustrates a system diagram of another embodiment of the present invention; and Figure 11 illustrates a schematic view of a conventional natural gas reforming molten carbonate fuel cell system. Now, preferred embodiments of the present invention will be explained with reference to the accompanying drawings. In the following description, however, a reformer, a catalyst combustor and so on which are incorporated in a molten carbonate fuel cell power generation system are omitted for an illustrative purpose. Generally, gases discharged from an anode chamber of a molten carbonate fuel cell contain a large amount of CO₂, H₂ as larg amount of as CO₂, a relatively small amount of H₂ and CO. In order to feed CO₂ contained in the gases discharged from the anode chamber, H₂ and CO are combusted by a catalyst combustor or combustible components are removed by a gas separation before fed to a cathode chamber of the fuel cell. There are some devices for this purpose. For example, the reformer 10 of Figure 10 functions as such a device. However, the present invention does not intend to disclose this type of device. Thus, the explanation of these devices are omitted in the following description. In addition, a heat exchanger, a moisture removal device and so on for optimizing the system operation will not be explained. In the present invention, the fuel cell I, as shown in Figures 2 to 10, is operated in a low CO₂ utilization mode with the CO₂ concentration at the cathode chamber entrance being raised, so that a high voltage is generated and the power generation efficiency is improved. As the CO₂ utilization factor is lowered, the retaining amount of CO₂ which promotes the reaction at the cathode is increased, so that the CO₂ partial pressure from the cathode chamber entrance through the cathode chamber exit is maintained at a high level. Consequently, a high voltage is generated and the power generation efficiency is raised. The relation between the CO₂ concentration, the CO₂ utilization factor and the generated voltage is shown in Figure 1. As seen from Figure 1, the generated voltages rises as the CO₂ concentration a at the cathode chamber entrance becomes higher. On the other hand, the generated voltage drops as the CO₂ utilization factor b becomes higher and the voltage rises as the utilization factor b drops. Here, the CO₂ concentration represents a ratio of CO₂ to entire gases. The CO₂ concentration varies with design factors. Therefore, generally it is difficult to show the CO₂ concentration quantitatively and an absolute amount of CO₂ is used instead of CO₂ concentration in the following description. Figure 2 shows a first embodiment of a method according to the present invention. An electrolyte plate 1 soaked with carbonate is sandwiched by a cathode and an anode at respective faces of the electrolyte plate 1, thereby forming a first fuel cell I. Oxidizing gas is fed to a cathode chamber and fuel gas is fed to an anode chamber. In this embodiment, air A (oxidizing gas) is fed to an entrance of the cathode chamber 2 by an air feed line 8 and fuel gas FG (anode gas) is fed to an entrance' of the anode chamber 3 by a fuel gas feed line 16. A cathode exhaust gas line 11 is connected to an exit of the cathode chamber 2. Combustible components are removed from the anode exhaust gas containing CO₂ (not illustrated) and then the anode exhaust gas is fed to the cathode chamber 2 through an anode exhaust gas line 29. A CO₂ branch line 30 is connected to the CO₂ circulation line 28 so that part of CO₂ can be branched for another purpose. The air whose CO₂ has been separated by the CO₂ separator 27 is expelled to atmosphere through a line 31. A second molten carbonate fuel cell II is provided. A cathode exit of the upstream or first fuel cell I is directly connected with an entrance of the downstream fuel cell II. The upstream fuel cell I is operated in a low CO₂ utilization mode and a necessary amount of CO₂ is fed to the downstream fuel cell II. In this case, a capacity ratio between the fuel cells I and II can be arbitrarily determined as required, but in this particular embodiment the fuel cells I and II have the same capacity. Specifically, the fuel cell II is located downstream of the fuel cell I such that the fuel cell II serves as a CO₂ separator, air is introduced to the cathode chamber entrance of the fuel cell I by an air feed line 8, anode exhaust gas discharged from the anode chamber 3 is introduced to the cathode chamber of the fuel cell I by an anode exhaust gas line 29 and a cathode exhaust gas line 11 of the cathode chamber 2 is connected to a cathode chamber entrance of the downstream fuel cell II so as to connect the cathode chambers of the fuel cells I and II with each other directly. Therefore, an excessive amount of CO₂ discharged from the cathode chamber 2 of the upstream fuel cell I is fed to the cathode chamber 2 of the downstream fuel cell II, and CO₂ which is used in the cathode reaction at the down stream fuel cell II and then separated is recovered from the anode chamber 3. The recovered CO₂ is entirely or partially introduced to the cathode chamber entrance of the upstream fuel cell I by a CO₂ recirculation line 28. Fuel gas feed lines 16 and 16a are respectively connected with the anode chambers 3 of the fuel cells I and II and the same amount of fuel gas is introduced to the anode chambers of the two fuel cells. In the upstream fuel cell I, a large amount of CO₂ (amount larger than used in the cathode reaction) is transferred to the cathode chamber 2 so that the CO₂ concentration at the cathode chamber entrance is high. In addition, a surplus CO₂ is discharged from the cathode chamber 2 of the upstream fuel cell I and led to the cathode chamber 2 of the downstream fuel cell II. Accordingly, the downstream fuel cell II is operated in the low CO₂ utilization mode. In the downstream fuel cell II, the power generation takes place using CO₂ discharged from the upstream cathode chamber 2 and the CO₂ separation is performed. Gases discharged from the anode chamber 3 of the downstream fuel cell II are returned to the cathode chamber 2 of the upstream fuel cell 1, i. e., the separated and recovered CO₂ at the downstream side is recirculated to the upstream side. Now, an example using specific numbers will be explained. In a case where LNG is used as raw material, an amount of CO₂ fed to the anode chamber 3 contained in the fuel gas is 25% of H₂. Thus, when a total amount of H₂ used in the reaction is 100V, CO₂ of 25V is divided to two and the same amount of CO₂ is respectively fed to the anode chambers 3 of the fuel cells I and II. CO₂ of 62.5V (sum of 12.5V fed to the anode chamber 3 and 50V used in the cell reaction) and CO₂ of 62.5V discharged and recirculated from the anode chamber 3 of the downstream fuel cell II, like the upstream fuel cell I, are led to the cathode chamber entrance of the upstream fuel cell I. In a word, CO₂ of 125V is fed to the cathode chamber entrance of the upstream fuel cell I. Among CO₂ gases thus fed, used is the 50V, and the remainder (CO₂ of 75V) is fed to the cathode chamber 2 of the downstream fuel cell II. In the fuel cell II, CO₂ of 50V is used and the remainder (CO₂ of 25V) is expelled to atmosphere. Therefore, in the upstream fuel cell I, the CO₂ concentration at the cathode chamber entrance is high and the CO₂ utilization factor is as low as 40%. Accordingly, the upstream fuel cell I serves as a CO₂ accumulator which can retain a large amount of CO₂. In addition, the CO₂ partial pressure from the cathode chamber entrance through the cathode chamber exit is maintained at a high level. Thus, the voltage to be generated can be set to a high value. On the other hand, in the downstream fuel cell II which serves as the CO₂ separator, the CO₂ utilization factor is as high as 66.7% and the CO₂ recovering efficiency is raised. In the system of Figure 2, the cathode exhaust gas discharged from the cathode chamber 2 of the upstream fuel cell I may be expelled to atmosphere without being introduced to the cathode chamber 2 of the downstream fuel cell II. In addition, CO₂ discharged from the anode chamber 3 of the downstream fuel cell II may be fed to the cathode chamber 2 of itself without being recirculated to the upstream side. In short, the fuel cells I and II may be independent from each other. In such a case, the amounts of CO₂ at the cathode chamber entrances of the two fuel cells I and II are respectively 62.5V and the amounts of CO₂ used are respectively 50V. Therefore, the CO₂ utilization factors of the fuel cells I and II are respectively 80%. This means that the CO₂ utilization factors are high respectively, amounts of retaining CO₂ are low respectively and the CO₂ partial pressures drop at the exits of the cathode chambers respectively. Thus, a high voltage cannot be expected. According to the present invention, on the other hand, the fuel cells I and II are connected with each other and the CO₂ concentration at the cathode chamber entrance of the upstream fuel cell I is high so as to discharge the surplus CO₂, i. e., the upstream fuel cell I is operated in the low CO₂ utilization factor mode. Therefore, the fuel cells I and II are operated at the high CO₂ concentration and at the low CO₂ utilization factor mode respectively as compared with the case of the two fuel cells being operated separately. In addition, the CO₂ partial pressure can be maintained at a higher level. Consequently, the generated voltage becomes higher. Figure 3 shows a modified version of Figure 2. In a system similar to the system of Figure 2, the capacity of the upstream fuel cell I is set to be different from the capacity of the downstream fuel cell II. Specifically, the fuel cell I having a larger capacity is located upstream and the fuel cell II having a smaller capacity is located downstream. The downstream fuel cell II serves as a CO₂ separator. Due to the capacity difference between the two fuel cells, amounts of CO₂ fed to the anode chambers 3 are set to 15V and 10V respectively, as illustrated in Figure 3. An amount of CO₂ used in the fuel cell I is set to 60V and that used in the fuel cell II is set to 40V such that CO₂ of 50V in total is discharged from the anode chamber 3. Among CO₂ of 50V, CO₂ of 35V is recirculated to the cathode chamber 2 of the upstream fuel cell I. CO₂ of 50V is discharged from the cathode chamber 2 of the upstream fuel cell I and introduced to the cathode chamber 2 of the downstream fuel cell II. In this embodiment, an amount of CO₂ led to the cathode chamber 2 of the upstream fuel cell I is a sum of 75V transferred from the anode chamber 3 and 35V recirculated, i. e., 110V. On the other hand, an amount of CO₂ used is 60V, and therefore the remaining 50V CO₂ is discharged. Consequently, the CO₂ concentration at the cathode chamber entrance is high and the CO₂ utilization factor is low (54.5%) This means that the fuel cell I is operated in the low CO₂ utilization mode, an amount of the retaining CO₂ in the cathode chamber 2 is large and the generated voltage is high. In the downstream fuel cell II, the power generation and the CO₂ separation are performed, but the CO₂ recovery is a primary object, so that the CO₂ utilization factor is high (80%) and accordingly the generated voltage is not high as the system of Figure 2. However, an amount of CO₂ expelled to atmosphere is very small (10V) and therefore this contributes to a prevention of a greenhouse effect of the earth. In addition, part of CO₂ discharged from the anode chamber 3 is recirculated to the upstream side and the remainder is branched out. The branched out CO₂ is used for purposes other than power generation: for example, for a methanol production as mixed with hydrogen gas. Figure 4 is an example showing that in the same system as Figure 3, the fuel gas which does not possess a sufficient amount of CO₂ is also satisfactory for the operation. Specifically, if the amount of CO₂ among the fuel gas is small, CO₂ discharged from the anode chamber 3 of the downstream fuel cell II is entirely recirculated to the cathode chamber 2 of the upstream fuel cell I to raise the CO₂ concentration at the cathode chamber entrance of the fuel cell I is raised to a required level. In addition, the CO₂ utilization factor is adjusted to be low and the amount of retaining CO₂ is increased. Therefore, an economical operation is possible and the power generation efficiency is improved. With taking advantages of this example, by-product gases produced in a chlorine plant which do not include CO₂ can be used. Figures 5 and 6 respectively illustrate other embodiments of the present invention. CO₂ discharged from the cathode chamber 2 of the upstream fuel cell I is recirculated by 50% such that the CO₂ gas composition at the cathode entrance and the CO₂ utilization factor are respectively changed. In Figure 5 which is similar to Figure 2, 50% of CO₂ discharged from the cathode chamber 2 of the upstream fuel cell I is recirculated. In other words, half of CO₂ discharged from the cathode chamber 2 (CO₂ of 75V) is recirculated to the cathode chamber entrance by a recirculation line 32 in a manner such that CO₂ transferred from the anode chamber 3 of the fuel cell I and CO₂ recirculated from the anode chamber 3 of the downstream fuel cell II, which sums 125V, merge with the above-mentioned CO₂ of 75V. Thus, the CO₂ utilization becomes 200V. Among 200V CO₂ transferred to the cathode chamber 2, 50V is used for the reaction and the remaining CO₂ of 150V is discharged from the cathode chamber exit. Among 150V CO₂, 75V is recirculated and another 75V is fed to the cathode chamber 2 of the downstream fuel cell II. In this manner, the amount of CO₂ at the cathode chamber entrance is increased to 200V while an amount used is constant, so that the utilization factor of CO₂ is 25%, which is lower than 40% of Figure 2. Figure 6 shows a system similar to Figure 3. As illustrated, 50% of CO₂ (50V) discharged from the cathode chamber 2 of the upstream fuel cell I is recirculated to the cathode entrance by the recirculation line 32. Thereupon, a total amount of CO₂ at the cathode entrance becomes 160V since CO₂ transferred from the anode chamber 3 of the fuel cell I and CO₂ recirculated from the anode chamber 3 of the downstream fuel cell II sum 110V and the above-mentioned 50V is added to 110V. The amount of CO₂ fed to the cathode entrance is 160V whereas the amount of CO₂ used is 60V (constant), so that the CO₂ utilization factor is 37.5%. This value is smaller than 54.5% of Figure 3. Figure 7 illustrates still another embodiment of the present invention. Figure 7 also shows a system similar to Figure 3. 50% of CO₂ (10V) discharged from the cathode chamber 2 of the downstream fuel cell II is recirculated to the cathode chamber entrance by a recirculation line 33. This 10V CO₂ merges with 50V CO₂ transmitted from the upstream fuel cell I at the cathode chamber entrance of the downstream fuel cell II. Therefore, the total becomes 60V. The amount of CO₂ fed to the cathode chamber entrance is 60V whereas the amount of CO₂ used is 40V (constant), so that the CO₂ utilization factor is 66.7%. This value is smaller than 80% of a case of no recirculation. Figure 8 depicts yet another embodiment of the present invention. This embodiment combines the cathode recirculation of the upstream fuel cell I of Figure 6 with the cathode recirculation of the downstream fuel cell II of Figure 7 (The cathode exhaust gas of the fuel cell II is recirculated to the cathode chamber entrance). Parts of CO₂ respectively discharged from the cathode chambers 2 of the fuel cells I and II are recirculated to their own cathode chamber entrances so as to lower the CO₂ utilization factor at the respective cathode chambers 2. Figure 9 also illustrates another embodiment of the present invention. In the embodiments of Figures 2 to 8, the fuel gas FG is directly fed to the upstream anode chamber 3 and the downstream anode chamber 3. On the other hand, in this particular embodiment (Figure 9), the fuel gas FG is fed only to the anode chamber 3 of the upstream fuel cell I. The anode exhaust gas from the anode chamber 3 of the upstream fuel cell I, which contains unreacted combustible gases, are introduced to the anode chamber 3 of the downstream fuel cell II via the anode exhaust gas feed line 40. The anode exhaust gas from the downstream fuel cell II is then introduced to the cathode chamber entrance of the upstream fuel cell I through the CO₂ recirculation line 28 after it is merged with the air of the air feed line 8. In this embodiment, the fuel gas is fed to the anode chamber 3 of the upstream fuel cell I only, but the anode exhaust gas from the downstream fuel cell II which contains CO₂ is fed to the cathode chamber 2 of the upstream fuel cell I. As a result, the same advantages as the embodiments of Figures 2 to 8 can be also obtained in this embodiment. Figure 10 shows still another embodiment. This comes from a modification of the embodiments of Figures 2 to 4. There are provided anode exhaust gas recirculation lines 41 and 42. These lines are used to recirculate the anode exhaust gas to the anode chambers 3 of the upstream and downstream fuel cells I and II respectively. Blowers 43 and 44 are also provided on the respective lines 41 and 42. The present invention is not limited to the above-described embodiments but may have other modes. For instance, in Figure 2, CO₂ discharged from the cathode chamber 2 of the second fuel cell II may be further separated and recovered by another fuel cell and the recovered CO₂ may be recirculated to the cathode chamber entrance of the most upstream or first fuel cell I. In other words, there may be provided three or more fuel cells. In summary, the present invention has following advantages: Since CO₂ is separated and recovered from gases containing CO₂ discharged from the cathode of the molten carbonate fuel cell by the CO₂ separator and the recovered CO₂ is entirely or partially recirculated to the cathode chamber entrance while CO₂ discharged from the anode chamber is also transferred to the cathode chamber, with the amount of CO₂ used being maintained to be constant and therefore the surplus CO₂ being discharged from the cathode chamber so as to achieve the operation of low CO₂ utilization factor mode, the CO₂ concentration at the cathode chamber entrance becomes high and the surplus CO₂ is discharged to lower the CO₂ utilization factor. As a result, a large amount of CO₂ which promotes the fuel cell reaction is retained in the cathode chamber and the CO₂ partial pressure from the cathode chamber entrance through the cathode chamber exit is maintained at a high level, thereby improving the power generation efficiency. Furthermore, when the second fuel cell is provided as a CO₂ separator instead of the above-mentioned CO₂ separator and the cathode chambers of the two fuel cells are directly connected with each other, with the upstream or first fuel cell being operated in the low CO₂ utilization mode and with the downstream or second fuel cell performing the power generation using CO₂ from the cathode chamber of the first fuel cell, CO₂ is recovered from the anode chamber exit and recirculated to the first fuel cell, the first fuel cell generates voltage as high as the foregoing case or the power generation efficiency can be improved. In addition, the second or downstream fuel cell performs the power generation while the CO₂ separation is proceeding, and the CO₂ utilization factor is raised. Thus, the amount of CO₂ recirculated to the upstream side can be increased and the amount of CO₂ can be decreased. This contributes to the prevention of the greenhouse effect of the earth. Moreover, the amount of CO₂, the CO₂ utilization factor and the CO₂ concentration at the cathode chamber(s) of the fuel cell(s) can be set to the most desirable values by recirculating part (50%, for example) of CO₂ discharged from the cathode chamber of the first fuel cell and/or the second fuel cell to its or their own cathode chamber entrance.

Claims: A method of operating a power generation system using at least two fuel cells (I, II) connected to each other in series, one fuel cell (I) being located upstream of a next fuel cell (II), the fuel cell (I; II) including an electrolyte plate (1) sandwiched by a cathode electrode and an anode electrode with a cathode chamber (2) being provided on the cathode electrode and an anode chamber (3) being provided on the anode electrode and with oxidizing gas being fed to the cathode chamber (2) and fuel gas being fed to the anode chamber (3) for power generation, said method comprises the steps of: (A) introducing air to the cathode chamber (2) of the most upstream fuel cell (I); (B) introducing the fuel gas (FG) to the anode chamber of each fuel cell (I; II); (C) recirculating CO₂ of the anode exhaust gas discharged from the anode chamber (3) of each fuel cell (I), except the most downstream fuel cell (II), to the cathode chamber (2) of the same fuel cell (I); (D) introducing CO₂ of the anode exhaust gas discharged from the most downstream fuel cell (II), to the cathode chamber (2) of the most upstream fuel cell (I); and (E) introducing part or all of the cathode exhaust gas discharged from each fuel cell (I), to the cathode chamber of the fuel cell (II) downstream thereof (I), whereby the power generation of high efficiency is achieved in all the fuel cells (I, II) at a low CO₂ utilization factor, using CO₂ of high concentration fed to the cathode chambers (2) of the fuel cells (I, II). A method of operating a power generation system using at least two fuel cells (I, II) connected to each other in series, one fuel cell (I) being located upstream of a next fuel cell (II), the fuel cell (I; II) including an electrolyte plate (1) sandwiched by a cathode electrode and an anode electrode with a cathode chamber (2) being provided on the cathode electrode and an anode chamber (3) being provided on the anode electrode and with oxidizing gas being fed to the cathode chamber (2) and fuel gas being fed to the anode chamber (3) for power generation, said method comprises the steps of: (A) introducing air to the cathode chamber (2) of the most upstream fuel cell (I); (B) introducing the fuel gas (FG) to the anode chamber of each fuel cell (I; II); (C) recirculating CO₂ of the anode exhaust gas discharged from the anode chamber (3) of each fuel cell (I), except the most downstream fuel cell (II), to the cathode chamber (2) of the same fuel cell (I); (D) introducing CO₂ of the anode exhaust gas discharged from the most downstream fuel cell (II), to the cathode chamber (2) of the most upstream fuel cell (I); and (E) introducing part of the cathode exhaust gas discharged from each fuel cell (I), to the cathode chamber (2) of a next fuel cell (II) downstream thereof (I) and introducing the remaining cathode exhaust gas to an entrance of the cathode chamber (2) of the same fuel cell (I), whereby the power generation of high efficiency is achieved in all the fuel cells at a low CO₂ utilization factor, using CO₂ of high concentration fed to the cathode chambers of the fuel cells (I; II). A method of operating a power generation system using at least two fuel cells (I, II) connected to each other in series, one fuel cell (I) being located upstream of a next fuel cell (II), the fuel cell (I; II) including an electrolyte plate (1) sandwiched by a cathode electrode and an anode electrode with a cathode chamber (2) being provided on the cathode electrode and an anode chamber (3) being provided on the anode electrode and with oxidizing gas being fed to the cathode chamber (2) and fuel gas (FG) being fed to the anode chamber (3) for power generation, said method comprises the steps of: (A) introducing air to the cathode chamber (2) of the most upstream fuel cell (I); (B) introducing the fuel gas (FG) to the anode chamber of each fuel cell (I; II); (C) recirculating CO₂ of the anode exhaust gas discharged from the anode chamber (3) of each fuel cell (I), except the most downstream fuel cell (II), to the cathode chamber (2) of the same fuel cell (I); (D) introducing CO₂ of the anode exhaust gas discharged from the most downstream fuel cell (II), to the cathode chamber (2) of the most upstream fuel cell (I); (E) introducing part or all of the cathode exhaust gas discharged from each fuel cell (I), to the cathode chamber (2) of a next fuel cell (II) downstream thereof; and (F) introducing the remaining cathode exhaust gas discharged from the most downstream fuel cell (II), to an entrance of the cathode chamber (2) of the most downstream fuel cell (II), whereby the power generation of high efficiency is achieved in all the fuel cells at a low CO₂ utilization factor, using CO₂ of high concentration fed to the cathode chambers of the fuel cells (I; II). The method according to any one of claims 1 to 3, characterized in that the fuel gas (FG) fed to the anode chamber (3) contains H₂ and CO₂, and CO₂ is about 25% with respect to H₂. The method according to any one of claims 1 to 4, characterized in that there are provided two fuel cells (I, II), a capacity of the upstream fuel cell (I) is about 1 to 1.5 times that of the downstream fuel cell (II), and the fuel gas (FG) is fed to the anode chambers (3) of the fuel cells (I, II) in accordance with the capacities of the fuel cells (I, II). The method of claim 5, characterized in that the cathode exhaust gas discharged from the cathode chamber (2) of the downstream fuel cell (II) is expelled to atmosphere. The method of claim 6, characterized in that the cathode exhaust gas discharged from the cathode chamber (2) of the upstream fuel cell (I) is partially fed to an entrance of the cathode chamber (2) of the same fuel cell (I). The method of claim 6, characterized in that the cathode exhaust gas discharged from the cathode chamber (2) of the upstream fuel cell (I) is divided approximately equally, and about one half of the cathode exhaust gas is fed to the cathode chamber (2) of the upstream fuel cell (I) and another about one half is fed to the downstream fuel cell (II).

Inventors: NAKAZAWA KENZO, NAKAZAWA, KENZO
Applicants: ISHIKAWAJIMA HARIMA HEAVY IND, ISHIKAWAJIMA-HARIMA HEAVY INDUSTRIES CO., LTD.
Application year: 1991
Main classification: H01M8
IPC codes: H01M8