Method of and apparatus for utilizing and recovering carbondioxide in combustion exhaust gas

Abstract: A method of recovering carbon dioxide gas from the combustion exhaust gas of fossil fuel, using a combustion equipment(II), characterized in that fuel gas (AG) is supplied to an anode chamber (3) of a molten carbonate fuel cell (FC) and oxidizing gas is supplied to a cathode chamber (2) of the fuel cell (FC), the combustion exhaust gas (G) from the combustion equipment (II) is suuplied to the cathode chamber (2) as part of the oxidizaing gas, CO₂ in the combustion exhaust gas (G) is allowed to react with O₂ in the oxidizing gas at the cathode (C) to produce carbonate ion, which is allowed to pass through an electrolyte (1) of the fuel cell (FC) and to reach the anode (A) , which the carbonate ion is allowed to react with hydrogen in the fuel gas (AG) to produce CO₂ and H₂O, the anode exhaust gas (8) containing CO₂ and H₂O generated at the anode (A) is discharged from the anode chamber (3) , H₂O is separated from the anode exhaust gas (8) and high-concentration CO₂ gas is recovered.

Description: The present invention relates to methods and apparatuses to utilize and recover CO₂ contained in combustion exhaust gas of fossil fuel such as coal in an attempt to remove carbon dioxide gas (CO₂) contained in the combustion exhaust gas before it is discharged to atmosphere. Combustion exhaust gas from a combustion equipment using fossil fuel contains a large volume of CO₂. In particular, exhaust gas generated from thermal power plants using coal, LNG and petroleum or exhaust gas from gas turbine generators is enormous, and CO₂ contained in the exhaust gas which is simultaneously generated from the thermal power plants is also tremendous. Conventionally, a large volume of exhaust gas generated from the thermal power plants is discharged to atmosphere without recovering CO₂ contained the exhaust gas. Recently, various approaches have been proposed to recover CO₂. For instance, it was proposed to discharge the exhaust gas into the open sea or to convert it into useful substances for recycle. The table below shows the volume of CO₂ discharged from the thermal power plants with respect to installed capacity and generated energy. The values used in the table for installed capacity and generated energy are specified by the power construction project plan for 1995 prepared in accordance with actual results of 1985. Installed capacity (x 10⁴ KW) Generated energy (x 10⁸ KWH) CO₂ discharge rate Nm³/KWH x 10⁸ Nm³ Ratio Coal 2300 990 0.42 416 32.1 LNG 4300 1660 0.24 398 30.8 Petroleum 5100 1600 0.30 480 37.1 Total 11700 4250 1294 100 As shown in the table above, the coal-fired thermal power plant discharges 0.42 Nm³/KWH of CO₂, LNG-fired thermal power plant 0.24 Nm³/KWH and petroleum-fired thermal power plant 0.30 Nm³/KWH, thereby evidencing the discharge of a great volume of CO₂. As discussed above, since a large amount of CO₂ is expelled to atmosphere from the thermal power plants, long wave long radiation from the earth surface is absorbed by CO₂ expelled. This prevents the long wave long radiation from permeating through the atmosphere, thereby warming the earth surface and lower atmosphere and causing the green-house effect and an environmental pollution problem. As the measure to prevent this green-house effect, the recovery of CO₂ discharged from the thermal power plants is imperative and its effective recovery method has been investigated. However, as mentioned above, the CO₂ volume discharged from the thermal power plants is enormous. In general, the concentration of SOx and NOx contained in the flue gas is just small (150 to 200 ppm at most) whereas that of CO₂ is said to be some hundred thousand ppm. It is believed to be impossible to treat CO₂ with the current removal technique such as the flue gas desulfurization or denitrification process, and no economical technique has been developed to recover CO₂ from the condition diluted with a great volume of air. As for the technique to discharge CO₂ into the sea proposed as one of CO₂ disposal methods, CO₂ recovered in some manner must be discharged to the sea after liquefaction, which raises problems to consume extra electric power in recovering, liquefying and transporting CO₂ to the offing. An object of the present invention is to provide a method of and an apparatus for recovering CO₂ contained in combustion exhaust gas discharged from combustion equipment of fossil fuel to minimize the volume of CO₂ released to atmosphere. Another object of the present invention is to provide a method of and an apparatus for utilizing CO₂ contained in combustion exhaust gas for cell reactions of a molten carbonate fuel cell. Still another object is to provide a method of and an apparatus for recovering CO₂ from anode exhaust gas discharged from an anode of a fuel cell to utilize CO₂ contained in combustion exhaust gas for cell reactions. According to one aspect of the present invention, there is provided a method of recovering CO₂ contained in fossil fuel combustion exhaust gas, comprising: feeding oxidizing gas to a cathode chamber of a molten carbonate fuel cell as well as feeding fuel gas to an anode chamber of the same fuel cell; feeding combustion exhaust gas to the cathode as part of the oxidizing gas; allowing CO₂ in the combustion exhaust gas to react with O₂ in the oxidizing gas at the cathode to generate carbonate ion, allowing the carbonate ion to pass through an electrolyte of the molten carbonate fuel cell and reach the anode, whereby the carbonate ion is allowed to react with hydrogen of the fuel gas at the anode to form CO₂ and H₂O; releasing from the anode chamber the anode exhaust gas containing CO₂ and H₂O generated at the anode; and recovering high-concentration CO₂ gas by separating H₂O from the anode exhaust gas. The present invention also provides a method of utilizing carbon dioxide gas of combustion exhaust gas discharged from a fossil fuel combustion equipment, comprising: feeding oxidizing gas to a cathode chamber and feeding fuel gas to an anode chamber of a molten carbonate fuel cell; feeding combustion exhaust gas to a cathode as part of the oxidizing gas; allowing CO₂ of the Combustion exhaust gas to react with O₂ of the oxidizing gas a the cathode to generate carbonate ion, allowing the carbonate ion to pass through an electrolyte of the molten carbonate fuel cell and reach the anode, whereby the carbonate ion is allowed to react with hydrogen of the fuel gas at the anode to form CO₂ and H₂O; and releasing the anode exhaust gas containing CO₂ and H₂O generated at the anode from the anode chamber and releasing cathode exhaust gas containing dilute CO₂ from the cathode chamber to atmosphere. The present invention further provides a method of utilizing and recovering carbon dioxide gas of fossil fuel combustion exhaust gas, comprising: mixing the fossil fuel combustion exhaust gas with air and feeding them as oxidizing gas to a cathode chamber of a molten carbonate fuel cell; feeding fuel gas to an anode chamber of the molten carbonate fuel cell; allowing CO₂ of the combustion exhaust gas in react with O₂ of the oxidizing gas at the cathode to generate carbonate ion, which ion is allowed to pass through an electrolyte of the molten carbonate fuel cell and reach the anode, at which the carbonate ion is allowed to react with hydrogen in the fuel gas to form CO₂ and H₂O; releasing from the anode chamber the anode exhaust gas containing CO₂ and H₂O generated at the anode; and separating H₂O from the anode exhaust gas expelled from the combustion chamber of the reformer to recover high-concentration CO₂ gas. The present invention also provides apparatuses for carrying out the above-described methods. Figure 1 is a system diagram showing one embodiment of the present invention; Figure 2 is a system diagram showing another embodiment of the present invention; Figure 3 is a schematic diagram of still another embodiment according to the present invention; Figure 4 is an illustration concretely showing part of Figure 3; Figure 5 is a schematic diagram showing yet another embodiment according to the present invention; Figure 6 illustrates part of Figure 5; Figure 7 is a schematic view of another embodiment according to the present invention; Figure 8 illustrates an outline of another embodiment according to the present invention; Figure 9 plots Mol ratio of exhaust gas to air and operating range of CO₂ recovery ratio; and Figure 10 is a view showing O₂ rate at a combustion chamber exit of a reformer and CO₂ reduction rate in the operating range of Figure 9. Referring now to the accompanying drawings, embodiments of the present invention will be described in depth. In Figure 1, an electrolyte tile (electrolyte plate) 1 including a molten carbonate soaked in a porous substance as an electrolyte is held between a cathode (oxygen electrode) C and an anode (fuel electrode) A, and a cathode chamber 2 is formed at the cathode C to introduce oxidizing gas, which contains CO₂, O₂ and N₂, and anode chamber 3 is formed at the anode A to introduce fuel gas, which contains H, CO and H₂O. A fuel cell element is formed by the electrolyte tile 1, cathode C, anode A, cathode chamber 2 and anode chamber 3. A molten carbonate fuel cell FC is formed by stacking the cell elements in multi-layers. The molten carbonate fuel cell system I is incorporated into a combustion equipment II which uses fossil fuel, that is, a combustion exhaust gas line 5 of the combustion equipment II is connected to an oxidizing gas feed line 4, which is connected to the supply side of the cathode chamber 2 of the molten carbonate fuel cell FC, so that the fossil fuel combustion exhaust gas G is fed to the cathode chamber 2 as part of the oxidizing gas CG. A reforming chamber 6a of a reformer 6 is connected to the anode chamber 3 by a fuel gas line 7 to feed into the anode chamber 3 the fuel gas AG which is reformed at the reformer 6. On the other hand, the exhaust side of the anode chamber 3 is connected to a combustion chamber 6b of the reformer 6 by an anode exhaust gas line 8. Methane CH₄ and steam H₂O are fed as fuel to the reforming chamber 6a of the reformer 6 through a supply line 15 and fed to the anode chamber 3 after the reforming at the reforming chamber 6a. CO₂ and H₂O produced upon reactions at the anode chamber 3 and unreacted H₂ are released into the anode exhaust gas line 8 as anode exhaust gas. Numeral 9 designates a gas-liquid separator, which is connected with the reformer 6 via a line 10 so that water contained in the anode exhaust gas (CO₂, H₂O) released from the combustion chamber 6b of the reformer 6 is separated. The gas-liquid separator 9 is also connected to a condenser 11 via a line 12, which condenses CO₂ after water is separated at the gas-liquid separator 9, so that CO₂ is condensed and separated from nitrogen N₂ and CO₂ is recovered as liquid. Numeral 13 denotes a line to feed either air or pure oxygen to the anode exhaust gas line 8 and numeral 14 denotes a cathode exhaust gas line connected to the exhaust side of the cathode chamber 2. Along with CO₂ and O₂ introduced as oxidizing gas CG to the oxidizing gas supply line 4 extending to the cathode chamber 2, the fossil fuel combustion exhaust gas G, which has been disposed to atmosphere, is introduced through the combustion exhaust gas line 5 whereby CO₂ contained in the combustion exhaust gas G is used as part of the oxidizing gas fed to the cathode chamber 2. CO₂ contained in the combustion exhaust gas G fed to the cathode chamber 2 of the fuel cell FC is allowed to react as follows at the cathode C together with the oxidizing gas: CO₂ + 1/2O₂ + 2e⁻ --> CO₃⁻⁻ (1) and converted into the carbonate ion CO₃⁻⁻. This carbonate ion CO₃⁻⁻ electrophoretically migrates in the tile 1 from the cathode C and reaches the anode A. On the other hand, fuel gas reformed in the reformer 6 is fed to the anode chamber 3 from the fuel gas supply line 7. Therefore, allowing the fuel gas AG fed to the anode chamber 3 to make contact with the carbonate ion CO₃⁻⁻ causes a following reaction to take place at the anode A: CO₃ + H₂ --> CO₂ + H₂O + 2e⁻⁻ (2) and CO₂ and H₂ are discharged from the anode A to the anode chamber 3, which releases CO₂ and H₂O as anode exhaust gas containing unreacted H₂. This anode exhaust gas is mixed with the air or pure oxygen supplied through a line 13. The air or pure oxygen has a quantity sufficient to combust the H₂. The anode exhaust gas is combusted with air or oxygen at the combustion chamber 6b. The line 13 is connected to the line 8 in the course to the combustion chamber 6b of the reformer 6. The anode exhaust gas is used as heat source of the reformer 6. From the combustion chamber 6b, CO₂ and H₂O are discharged and guided into the gas-liquid separator 9 by the line 10. In the separator 9, H₂O is separated to remove CO₂ for recovery. In this event, when CO₂ is recovered in the form of liquid, CO₂ is guided to the condenser 11 through the line 12 and condensed. The recovered CO₂ is allowed to react for effective recycle. For example, the recovered CO₂ is allowed to react with magnesium or calcium to produce magnesium oxide (MgO) or calcium oxide (CaO). MgO is used for catalyst, absorbent, magnesia cement and pharmaceuticals, while CaO is used for lining of furnaces and crucibles, construction materials and soil conditioner. The recovered CO₂ may be allowed to react with sodium carbonate (Na₂CO₃) and water to form sodium bicarbonate (2NaHCO₃). The sodium bicarbonate is used as fire extinguisher, pharmaceuticals, cleaning agent and baking powder. In addition, the recovered CO₂ may be allowed to react with calcium oxide (CaO) to form calcium carbonate (CaCO₃). The calcium carbonate can be used as industrial material, dental materials and pharmaceuticals. In the recovery process of the combustion exhaust gas CG, allowing the carbonate ion CO₃⁻⁻ generated by reactions on the cathode C side to reach the anode A via the tile 1 and discharging CO₂ and H₂O to the anode chamber 3 through the reaction at the anode A causes the cathode C to deliver electrons to the surroundings, thereby raising the electric potential higher than the surroundings. In contrast, the anode A receives electrons from the surroundings, thereby lowering the electric potential power than the surroundings. The electric power can be obtained by the potential difference between the cathode C and anode A. Figure 2 shows another embodiment of the present invention, which exhibits a case where the exhaust gas is utilized as heat source of the reformer 6 when the exhaust gas heat is wasted. That is, when the heat for the reformer 6 is produced from any other sources than the anode exhaust gas, high-temperature combustion exhaust gas is fed to the combustion chamber 6b from the line 16 of fossil fuel and air are fed to the combustion chamber 6b from the line 16 to combust them therein and are discharged from the exhaust line 17. The anode exit gas line 8 is connected to the gas-liquid separator 9 so that the anode exhaust gas from the anode chamber 2 is directly guided to the gas-liquid separator 9 without entering the combustion chamber 6b of the reformer 6. Also in this embodiment, CO₂ is condensed and recovered after separating H₂O in the anode exhaust gas. As described above, according to the present invention, CO₂ Contained in the fossil fuel combustion exhaust gas is used as part of oxidizing gas to be supplied to the cathode of the fuel cell without disposing to atmosphere as it is, and is conveyed to the anode side as carbonate ion by the reactions at the cathode side and them removed as CO₂ and H₂O through reactions at the anode, and CO₂ is recovered by separating H₂O or by further Concentrating CO₂. This can prevent green-house effect caused by discharging CO₂ of the combustion exhaust gas to atmosphere while producing electric power as well as saving oxidizing gas supplied to the cathode. Figure 3 and 4 in combination show one embodiment of the present invention. A coal-gasified molten carbonate fuel cell power generator IV is combined into the coal-fired thermal power plant III and the exhaust gas generated from the thermal power plant III is supplied as part of oxidizing gas to the cathode chamber of the molten carbonate fuel cell FC of the power generator IV without discharging it to atmosphere, and CO₂ in the exhaust gas is utilized for CO₂ required for reactions at the cathode. CO₂ is separated and recovered from the exhaust gas containing CO₂, thereby reducing the CO₂ content in the exhaust gas released from the cathode chamber of the fuel cell. The coal-gasified used carbonate fuel cell power generator IV includes five subsystems, namely gasification, gas purification, fuel cell, bottoming cycle and power conversion adjusting. The molten carbonate fuel cell FC in the fuel cell system is as described in Figure 1 and the exhaust gas from the thermal power plant III is directly introduced to the entrance of the cathode chamber 2 by the exhaust gas utilization line 20. Part of fuel gas and anode exhaust gas flowing through the circulation line 22 are branched to the anode chamber 3 by the fuel gas line 21. The air supply line 23 is connected to the exhaust gas utilization line 20 and the anode exhaust gas line 24 is connected to the exhaust gas line 20 via a catalyst combustor 25 so that air is fed to the cathode chamber 2 from the air supply line 23 as the oxidizing gas in addition to the exhaust gas, and other part of the anode exhaust gas discharged from the anode chamber 3 can be fed to the cathode chamber 2 from the line 24 via the catalyst combustor 25. The branch line 26 is connected to the catalyst combustor 25 to feed air required from combusting unreacted H₂ or CO contained in the anode exhaust gas in the catalyst combustor 25. The cathode exhaust gas released from the cathode chamber 2 is discharged to atmosphere from the discharge line 27, whereas part of the anode exhaust gas is removed via a line 28 to recover CO₂. To the cathode chamber 2 of the fuel cell FC, the exhaust gas utilization line 20 is connected to guide the exhaust gas discharged from the thermal power plant III so that a great volume of exhaust gas from the thermal power plant is fed to the cathode chamber 2 of the fuel cell FC as part of the oxidizing gas. Therefore, CO₂ required for reactions in the cathode chamber 2 is gained from the exhaust gas fed from the exhaust gas utilization line 9, and the exhaust gas with dilute CO₂ is released from the exit of the cathode chamber 2 via an exhaust line 27. Now, let the discharge rate of CO₂ contained in the exhaust gas released from a 1,000,000-KW coal-fired thermal power plant be 0.42 Nm³/KWH as discussed before. In implementing the present invention, a 500,000-KW coal-fired thermal power plant III is combined with a coal-gasified molten carbonate fuel cell power generator IV which consumes coal equivalent to 500,000 KW coal-fired thermal power generation which corresponds to the coal for 1,000,000 KW coal-fired thermal power generation, and the exhaust gas released from the plant III is supplied to the cathode chamber 2. This will feed the exhaust gas containing 0.42 Nm³/KWH of CO₂ to the cathode chamber 2 of the coal-gasified molten carbonate fuel cell FC from the thermal power plant III as part of oxidizing gas. This great volume of CO₂ is utilized in the reactions of equation (1) at the cathode chamber 2 together with CO₂ supplied to the cathode chamber 2 from the air supply line 23 and is converted to the carbonate ion CO₃⁻⁻. This carbonate ion CO₃⁻⁻ electrophoretically migrates in the electrolyte plate 1 and is carried to the anode 3. On the anode side, the reaction of equation (2) take place and CO₂ and H₂O are released from the anode chamber 3, part of which is fed to the cathode 2 and used for reactions. Because the molten carbonate fuel cell FC has a high power generating efficiency, 650,000 KW output is obtained, thereby creating a facility of 1,150,000-KW power output by adding the power output of 500,000 KW of the thermal power plant III. This system not only provides a power output exceeding that of the existing 1,000,000 KW thermal power plant but also utilizes CO₂ in the reactions at the cathode, which can be removed in the form of condensed CO₂ as the anode exhaust gas. Therefore, CO₂ released to atmosphere from this combined system of thermal power generator and molten carbonate fuel cell generator is only those which cannot be separated and recovered at the cathode, and whose volume is reduced to just 0.1 Nm³/KWH. With this system, the volume of CO₂ released to atmosphere becomes minute. Figures 5 and 6 show another embodiment of the present invention. Combined to the LNG as thermal power plant V, a natural gas reforming molten carbonate fuel cell power generator IV is installed and the exhaust gas CO₂ released from the thermal power plant V is used for power generation in the molten carbonate fuel cell FC to Separate CO₂, thereby raising a total power output of the LNG thermal power plant V and molten carbonate fuel cell generator IV while reducing the CO₂ content of the exhaust gas released from the cathode of the fuel cell. The fuel cell FC used in the natural gas reforming molten carbonate fuel cell generator VI is same as that in Figure 1. The anode chamber 3 is designed to receive fuel gas reformed in the reformer 30a of the reformer 30 from the fuel gas supply line 31. The cathode chamber 2 is designed to receive the exhaust gas released from the thermal power plant V guided from the exhaust gas utilization line 32. The air is also fed to the cathode chamber 2 from the air supply line 33, and gas containing CO₂ released from the combustion chamber 30b of the reformer 30 is supplied to the cathode chamber 2 from the line 34 through the exhaust gas utilization line 32. To the combustion chamber 30b of the reformer 30, the anode exhaust gas is supplied via an anode exhaust gas line 35 as well as part of air fed from the branch line 36 and part of the anode exhaust gas is removed from the exhaust gas line 37. In this embodiment, the CO₂ discharge rate from the LNG thermal power plant V is 0.24 Nm³/KWH as described above, but by supplying the exhaust gas containing such a large volume of CO₂ to the cathode chamber 2 of the natural gas reforming molten carbonate fuel cell FC from the exhaust gas utilization line 32 is part of oxidizing gas, CO₂ is separated from the exhaust gas discharged from the thermal power plant V through utilizing CO₂ of the exhaust gas for the reactions in the cathode, thereby controlling CO₂ in the exhaust gas released from the cathode 2 via an exhaust line 38 to be as small as 0.1 Nm³/KHW. When the thermal power plant V is combined with the natural gas reforming molten carbonate fuel cell equipment VI as shown in Figure 5 to form a plant corresponding to an existing 1,000,000 KW LNG thermal plant and the installed capacity of the thermal power plant V is made to be 500,00 KW, because of high power generating efficiency of the natural gas reforming molten carbonate fuel cell FC, 680,000 KW power generating output is obtained, and as a whole, the output of 1,180,000 KW can be obtained. Figure 7 shows another embodiment of the present invention. In place of combining the thermal power plant and molten carbonate fuel cell equipment described in the previous embodiments and utilizing CO₂ in the exhaust gas from the thermal power plant for power generation by the molten carbonate fuel cell to separate and recover CO₂, thereby discharging gas with dilute CO₂ to atmosphere, the gas turbine generator VII is installed in combination with the molten carbonate fuel cell power generator VIII, and the gas turbine generator is operated to generate power at the time of peak load. At this moment, the exhaust gas to be released to atmosphere is utilized for part of oxidizing gas to the molten carbonate fuel cell FC and at the same time the gas with little CO₂ is released to atmosphere. That is, for example, a simple open cycle gas turbine generator VII and a natural gas reforming molten carbonate fuel cell equipment VIII are combined and the exhaust gas utilization line 41 of the turbine 40 of the gas turbine generator VII is connected to the cathode chamber 2 entry of the molten carbonate fuel cell FC to allow the air from the air supply line 42 and the combustion gas of combustion section 43b of the reformer 43 from the combustion gas via a line 44 to join in the line 41. The gas turbine generator VII combusts the fuel supplied to the combustor 46 from the fuel supply line 45 with the air introduced from the compressor 47 and drives the turbine 40 by the high temperature high pressure combustion gas released from the combustor 46 to generate electric power with the generator 48 directly connected to the turbine 40. The natural gas reforming molten carbonate fuel cell power generating equipment VIII is designed to place an electrolyte plate 1 between the cathode C and anode A and supply the oxidizing gas to the cathode chamber 2 and the fuel gas to the anode chamber 3, respectively. Natural gas (CH₄) and steam (H₂O) are supplied to the anode chamber 3 of this fuel cell FC after they are reformed to the fuel gas at the reforming section 43a of the reformer 43. The air compressed by the compressor 50 which is rotated by the power turbine 49 is supplied to the cathode chamber 2. The cathode exhaust gas released from the cathode chamber 2 passes through the cathode exhaust gas line 52 and is fed back to the air supply line 42 via a blower 59. The cathode exhaust gas released from the cathode chamber 2 passes through the cathode exhaust gas line 52 and after heat is removed by the air at the air preheater 51, it is guided to the power turbine 49 to drive the turbine 49, thereby generating electric power by the generator 53. The anode exhaust gas released from the anode chamber 3 is guided to the combustion chamber 43b of the reformer 43 through the anode exhaust gas line 54. Unreacted combustible gases contained in the anode exhaust gas are combusted with air supplied to the combustion chamber 43b via the line 55, and the gases containing CO₂ expelled from the combustion chamber 43b of the reformer 43 are fed to the cathode chamber 2. In addition, part of the anode exhaust gas is removed through the line 56. The cathode exhaust gas from the power turbine 49 is expelled to atmosphere through the exhaust line 57. By providing the exhaust gas utilization line 41 between the turbine 40 and the cathode chamber 2 in a manner such that the exhaust gas from the turbine 40 of the gas turbine generator VII is guided to the cathode chamber 2 inlet of the fuel cell FC, the gas turbine generator VII and molten carbonate fuel cell power generating equipment IX are combined to obtain power output from both equipment simultaneously. Numeral 58 designates a cathode recycle line. In this embodiment, let the power output of the gas turbine generator VII be 15 MW and that of the molten carbonate fuel cell FC 26.2 MW and that of the generator 49 directly connected to the power turbine 49 be 4.5 MW. Therefore, when only the fuel cell power generation apparatus VIII is operated, the output is the sum of the above two, that is, 26.2 + 4.5 = 30.7 MW. Operating the gas turbine generator VII which is only operated during the peak load condition increases the power of the generator 53 which generates power by operation of the power turbine 49 and thus increases the output further by 9.1 MW. The total output becomes: 15 + 26.2 + 4.5 + 9.1 = 54.8 MW. This means that the combined system is a power generation system of 50 KW class. In addition, because the gas turbine generator VII does not need any condenser as with the case of turbine power generator, the construction cost is low. Therefore, compared with the case where the molten carbonate fuel cell generating equipment VIII is only operated, operating together with the gas turbine generator can reduce the unit price per 1 KW of electric power remarkably. Thus, for an example, if the construction cost of a 30-MW-class natural gas reforming fuel cell power generating system VIII is 7.5 billion yen and that of the gas turbine generator VIII is 1.2 billion yen, the cost when only the fuel cell power generating system VIII is operated is: 7.5 billion yen - 30 MW = 250,000 yen/KW, whereas the cost becomes lower when the output is brought to the 50 MW class by operating the gas turbine generator V, namely (7.5 billion yen - 1.2 billion yen) - 50 MW = 174,000 yen/KW. During the operation under the peak load condition, because the exhaust gas of the gas turbine 40 is supplied to the cathode chamber 2 of the fuel cell FC as part of the oxidizing gas without discharging to atmosphere, CO₂ contained in the exhaust gas is utilized as CO₂ required for the reactions at the cathode. Therefore, CO₂ discharged to atmosphere from the cathode chamber 2 is minute and same as in case of the foregoing embodiments, i. e., the CO₂ discharge rate can be made to be 0.1 Nm³/KWH. In all above-described embodiments, since as CO₂ + H₂O (anode exhaust gas) discharged from the anode chamber 3 of the fuel cell FC and part of unreacted H₂ and CO are drawn out of the circulation line by the branched line 56, CO₂ H₂O, unreacted H₂ and CO are separated in the subsequent process to recover CO₂. CO₂ recovered will be effectively used: for example, CO₂ is allowed to react with magnesium and calcium to produce magnesium oxide (MgO) and calcium oxide (CaO). MgO is used to manufacture catalyst, absorbent, magnesia cement and pharmaceuticals, while CaO is used for lining for furnaces and crucibles, construction materials and soil conditions. CO₂ recovered as above may be used at a vegetable plant or solidified to a harmless substance and disposed to the environment. In the foregoing embodiments, as examples, combination of the thermal power plant III or V and fuel cell power generation system IV or VI, and combination of the gas turbine generator VII and fuel cell power generator VIII are illustrated, but needless to say, the present invention should not limited to those combination of thermal power plants and fuel cell power generation systems For example, the fuel cell power generator may be combined with a facility which generates air containing a great volume of CO₂, such as iron works or paper-manufacturing plant as well as thermal power plants, in an attempt to separate CO₂ as well as to generate power. Figure 8 shows a system to utilize and recover CO₂ according to the present invention. The system includes a molten carbonate fuel cell power generating system X and a CO₂ separator XI. The treated gas containing CO₂ released from the natural gas thermal power plant IX is supplied to the cathode chamber 2 of the molten carbonate fuel cell FC together with fresh air and natural gas (reformed material gas), after the reforming, is supplied to the anode. The CO₂ separator XI separates CO₂ from the gas containing CO₂. More specifically, the molten carbonate fuel cell power generating system has a stacked fuel cell elements. Each cell element includes an electrolyte plate 1 soaked with molten carbonate sandwiched between a cathode (oxygen electrode) C and an anode (fuel electrode) A. The cathode chamber 2 and anode chamber 3 are formed on the cathode C and anode A respectively to make one cell element. To the cathode chamber 2 of the fuel cell FC which is formed by stacking these cell elements in multiple layers, fresh air compressed by the compressor 62 is supplied through the oxidizing gas supply line 63 after allowing it to pass the filter 61 together with the exhaust gas passing the exhaust gas utilization line 60 from the thermal power plant IX. At the same time, the cathode exhaust gas released from the cathode chamber 2 is discharged to atmosphere after it is guided to the turbine 65 from the cathode exhaust gas line 64 and part of the cathode exhaust gas is allowed to pass through the branch line 67 to be guided to the combustion chamber 67b of the reformer 68. The exhaust gas released from the combustion chamber 68b of the reformer 68 is pressurized by the blower 69 and supplied to the cathode chamber 2 from the line 70. On the other hand, natural gas NG is preheated at the natural gas preheater 71, then is allowed to pass the natural gas supply line 72 and is guided to the reformer chamber 68a of the reformer 68, in which it is reformed to fuel gas FG and is finally supplied to the anode chamber 3 from the fuel gas supply line 73. The anode exhaust gas released from the anode chamber 3 is guided to the gas-liquid separator 77 via a heat exchanger 74, evaporator 75 and condenser 76. In the separator 77, water (H₂O) contained in the anode gas is separated, and gas containing CO₂ is introduced to the CO₂ separator XI from the leading line 78 to separate and recover CO₂. H₂O separated at the gas-liquid separator 77 is then pressurized by the pump 79 and introduced into a liquid storing container 80. After that, it is evaporated to steam by the evaporator 75 and led to the midst of the natural gas supply line 72 to be mixed with natural gas. The CO₂ separator XI separates CO₂ of the gas after it is separated from the water at the gas-liquid separator 77, removes and recovers the separated CO₂ from the recovery line 81 and sends it to the CO₂ treating device 82. Also, the CO₂ separator XI returns the remaining gas, after recovery of CO₂, to the fuel cell power generation system X through the line 83 and guides it into the combustion chamber 68b of the reformer 68 via the heat exchanger 74 from the blower 84. There are two types of CO₂ separator XI: one that recovers CO₂ in the form of gas and the other that cools CO₂ with cryogenic fluid and recovers it in the form of liquid. To recover CO₂ from the exhaust gas released from the thermal power plant IX, the exhaust gas is introduced into the oxidizing gas supply line 63 from the exhaust gas utilization line 60, compressed together with air by the compressor 62 and supplied to the cathode chamber 2. On the other hand, natural gas gasified by the CO₂ separator XI is guided to the natural gas supply line 72 and reformed at the reformer 68, then as the fuel gas FG, it undergoes cell reactions at the anode chamber 3 to condense and remove CO₂ from the anode chamber 3. As the reactions take place on both cathode and anode sides, power is generated and CO₂ moves from the cathode to the anode. The gas flow rate in the cathode chamber 3 is a fraction of that of the cathode chamber 2, and therefore, CO₂ moved to the anode chamber 3 is condensed resulting in concentration of several times. Consequently, in the fuel cell FC, CO₂ condensation takes place as well as power generation. The anode gas with CO₂ condensed at the anode chamber 3 is sent to the gas-liquid separator 77 via the heat exchanger 74, evaporator 75 and condenser 76. In the separator 77, H₂O is separated and removed, then it is guided to the CO₂ separator XI by the leading line. In the CO₂ separator XI, CO₂ is separated from the gas and removed through the recovery line 81 to be recovered. The recovered CO₂ is sent to the CO₂ treating device 82. In this event, if CO₂ is recovered in the form of gas, CO₂ is separated and recovered without any further processing, while if CO₂ is recovered in the form of liquid, CO₂ is cooled to liquid with the cryogenic liquid. After CO₂ is recovered by the CO₂ separator XI, the remaining gases are guided to the combustion chamber 68b of the reformer 68 through the heat exchanger 74 in the fuel cell power generation system by the line 83 and recycled to the cathode chamber 2. With respect to recovery of CO₂, if the exhaust gas containing 9% CO₂ relative to the total gas flow rate is processed, for example, the CO₂ concentration of 7% of the gas entering the cathode chamber 2 is condensed to 42% at the exit of the anode chamber 3, the CO₂ concentration of the gas guided to the CO₂ separate XI from the CO₂ leading line 78 is condensed to 82%, the CO₂ concentration of the gas guided to the line 83 from the CO₂ separator XI is 74%, the gas recovered by the CO₂ separator XI is 100% and the CO₂ concentration of the gas discharged to the atmosphere via the turbine 65 can be reduced to 3%. In order to obtain this result, a certain range should be assigned to the Mol ratio of exhaust gas to fresh air supplied to the cathode chamber 2 and CO₂ recovery ratio of the CO₂ separator XI. For this purpose, followings are recommended: (1) Keep the Mol ratio of the exhaust gas to air supplied to 1 - 0.65; and (2) Keep the CO₂ volume recovered from the recovery line 81 in the CO₂ separator XI to be 0.2 - 0.4 relative to the CO₂ volume introduced to the CO₂ separator XI from the leading line 78. These operating ranges are specified in order to: (i) secure the proper content of CO₂ and O₂ at the cathode chamber 2 inlet of the fuel cell FC and the proper O₂ content at the exit of the combustion chamber 68b of the reformer 68; and (ii) bring the CO₂ reduction ratio of the gas released from the equipment below 1, that is, the ratio of CO₂ released to the atmosphere after passing the turbine 65 to the CO₂ content in the exhaust gas should be reduced under 1. According to the above operating conditions, if the Mol ratio of the exhaust gas to air is set to 1 - 0.65 as indicated by the line A of Figure 9 and the CO₂ recovery ratio of the CO₂ separator XI is set to 0.2 - 0.4 as indicated by the line B, the O₂ content and CO₂ reduction ratio at the combustion chamber exit of the reformer 68 satisfy the conditions (i) and (ii) as indicated by the lines C and D of Figure 10, respectively. In the above description, if the CO₂ recovery ratio is set to about 0.2 - 0.4 as shown in Figure 9, the CO₂ partial pressure, as CO₂ is liquefied and separated, increases and the power required can be reduced. The embodiments deal with the cases of recovering CO₂ in the combustion exhaust gas released from the natural-gas-fired thermal power plants by utilizing the recovered CO₂ for power generation, but the same principle can be applied to the gases released from plants other than thermal power plants, and the above-described molten carbonate fuel cell power generation system only represents one example. Also, another molten carbonate fuel cell may be provided in the downstream line 66 of the turbine 65.

Claims: A method for recovering carbon dioxide gas from combustion exhaust gas (G) of fossil fuel, using a fossil fuel combustion equipment (II), a molten carbonate fuel cell (FC) and a reformer (6), the fuel cell (FC) having anode (A), anode chamber (3), cathode (C), cathode chamber (2) and electrolyte (1) and the reformer (6) having a reforming chamber (6a) and a combustion chamber (6b), the method comprising the steps of supplying anode gas to the anode chamber (3) of the fuel cell (FC) and oxidizing gas supplied to the cathode chamber (2); feeding gases (G) produced upon combustion (called "combustion exhaust gas") to the cathode chamber (2) as part of the oxidizing gas; allowing CO₂ of the combustion exhaust gas (G) to react with O₂ of the oxidising gas at the cathode to produce carbonate ion; allowing the carbonate ion to pass through the electrolyte (1) of the fuel cell (FC) and reach the anode (A); allowing the carbonate ion to react with hydrogen of the fuel gas at the anode (A) to produce CO₂ and H₂O; and discharging gases (8) produced at the anode (A) (called "anode exhaust gas") from the anode chamber (3), which gases containing CO₂, H₂O, unreacted H₂ and CO; and the method being further characterized by separating H₂O from the anode exhaust gas (8) expelled from the combustion chamber (6b) of the reformer (6) and recovering high-concentration CO₂ gas. The method of claim 1, characterized in that the method further includes the step of: feeding the anode exhaust gas (8) to the combustion chamber (6b) of the reformer (6) as combustible gas to be burned in the combustion chamber (6b) of the reformer (6). The method of claim 1 or 2, characterized in that the method further includes the step of: discharging the cathode exhaust gas (G) from which CO₂ has been removed, to atmosphere from the cathode chamber (2). The method according to one of Claims 1 to 3, characterized in that the fuel gas (AG) supplied to the anode chamber (3) of the molten carbonate fuel cell (FC) includes H₂, CO and H₂O. The method according to one of Claims 1 to 4, characterized in that the oxidizing gas supplied to the cathode chamber (2) of the molten carbonate fuel cell (FC) includes CO₂, O₂ and N₂. The method of Claim 1 or 2 and 4, characterized in that the fuel gas (AG) is produced by reducing natural gas with steam in the reforming chamber (6a) of the reformer (6). The method of Claim 6, characterized in that the anode exhaust gas (8) is mixed with air and guided to the combusiton chamber (6b) of the reformer (6), and unreacted combusitible gases contained in the anode exhaust gas (8) are combusted in the combustion chamber (6b) to be used as heat source for reforming reactions. The method according to one of Claims 1 to 7, characterized in that the combustion exhaust gas (G) is directly supplied to the cathode chamber (2) from the fossil fuel combustion equipment (II). The method of Claim 7 or 8, characterized in that H₂O is separated by condensing the anode exhaust gas (8) discharged from the combustion chamber (6b) of the reformer (6) and high-concentration CO₂ gas produced upon removal of H₂O is condensed to recover CO₂. The method according to one of Claims 1 to 9, characterized in that a majority of CO₂ contained in the oxidizing gas supplied to the cathode chamber (2) is removed and released from the cathode chamber (2). The method according to one of Claims 6 to 10, characterized in that combustible gases are supplied into the combustion chamber (6b) of the reformer (6) and burned therein to maintain reforming reaction temperature of the reforming chamber (6a). The method according to one of Claims 2 to 11, characterized in that the anode exhaust gas (8) is condensed to separate H₂O and the high concentration CO₂ gas from which H₂O has been removed is further condensed to recover CO₂. The method according to one of Claims 3 to 12, characterized in that combustion exhaust gas (G) discharged from a thermal power plant (III) is directly introduced into the cathode chamber (2) and the combustion exhaust gas (G) is mixed with air so that CO₂ of the combustion exhaust gas is diluted before expelled to atmosphere. The method according to one of Claims 3 to 13, characterized in that part of the anode exhaust gas (8) from the anode chamber (3) is recirculated into the anode chamber (3) and another part of the anode exhaust gas (8) is introduced into the catalyst combustor (25) such that unreacted combustible gases contained in the anode exhaust gas (8) is burned with air fed into the catalyst combustor (25) and gases upon the combustion are guided to the cathode chamber (2). The method of claim 3, characterized in that the method further includes the steps of: reforming gas such as natural gas with steam to fuel gas (AG) and feeding the fuel gas (AG) into the anode chamber (3) of the fuel cell (FC). The method of Claim 15, characterized in that the combustion exhaust gas (G) includes gases discharged from a thermal power plant (V), the combustion exhaust gas (G) is mixed with air and gases discharged from the combustion chamber (30b) of the reformer (30) before introduced into the cathode chamber (2) so that CO₂ of the combustion exhaust gas (G) is diluted before expelled to atmosphere. The method of claim 1, characterized in that the fossil fuel combustion equipment is a turbine generator (VI) and the method further includes the steps of: supplying air into the compressor (47) of the turbine generator (VI) to compress the air; feeding natural gas into the compressed air to combust the natural gas and feeding the combusted gas to the turbine to drive the generator; and mixing with air the combustion exhaust gas (G) discharged from the turbine (40) and feeding the combustion exhaust gas (G) as oxidizing gas into the cathode chamber (2). The method of Claim 17, characterized in that the natural gas and steam are fed into the reforming part (43a) of the reformer (43) to produce combustion gas containing H₂, CO and H₂ and the combustion gas is introduced into the anode chamber (3). The method of Claim 18, characterized in that part of the anode exhaust gas (8) from the anode chamber (3) is fed into the combustor (43b) of the reformer (43) such that unreacted combustible gases contained in the anode exhaust gas (8) are burned with air introduced into the combustor (43b) to maintain reforming reactions at the reforming part (43a). The method of Claim 19, characterized in that gases discharged from the combustor (43b) of the reformer (43) are fed into the cathode chamber (2) as the oxidizing gas. The method of Claim 20, characterized in that the cathode exhaust gas is fed to a power turbine (49) of an auxiliary generator (53) to drive the auxiliary generator (53), and air fed into a compressor (50) of the auxiliary generator (53) is compressed and introduced into the cathode chamber (2). The method of claim 1, 2 or 3, characterized in that the oxidizing gas contains the mixture of fossil fuel combustion gas and air. The method of Claim 22, characterized in that the combustion exhaust gas and air are pressurized and then supplied into the cathode chamber (2). The method of Claim 22 or 23, characterized in that the natural gas is reduced with steam at the reforming chamber (68a) of the reformer (68) to produce the fuel gas and the fuel gas is supplied to the anode chamber (3). The method according to one of Claims 22 to 24, characterized in that the anode exhaust gas from the anode chamber (3) is condensed to remove H₂O, the high concentration CO₂ gas from which H₂O has been removed is further condensed to recover CO₂. The method of Claim 25, characterized in that the anode exhaust gas after the CO₂ recovery is fed into the combustion chamber (68b) of the reformer (68), part of the cathode exhaust gas is fed into the combustion chamber (68b) of the reformer (68), unreacted combustible gases contained in the anode exhaust gas are burned with unreacted O₂ contained in the cathode exhaust gas at the combustion chamber (68b) to be used as heat source of reforming reactions at the reforming chamber (68a). The method of Claim 26, characterized in that exhaust gas from the combustion chamber (68b) of the reformer (68) is fed into the cathode chamber (2) as the oxidizing gas. An apparatus for recovering carbon dioxide gas from combustion exhaust gas of fossil fuel, using a fossil fuel combustion equipment (II), the apparatus comprising a molten carbonate fuel cell (FC), including a plurality of cell elements piled up, soaked with molten carbonate, an anode (A), anode chamber (3), cathode (C) and cathode chamber (2) with the electrolyte tile (1) being sandwiched by the anode (A) and cathode (C); means (7) for supplying fuel gas to the anode chamber (3) of the fuel cell (FC); means (4) for supplying oxidizing gas supplied to the cathode chamber (2) of the fuel cell (FC); and means (5) for feeding gases produced upon combustion at the combustion equipment (II) (called combustion exhaust gas") to the cathode chamber (2); characterized in that the apparatus further comprises means (9, 11) for separating H₂O from the anode exhaust gas and recovering CO₂. The apparatus of Claim 28, characterized in that the fuel gas supply means (7) includes a reformer (6), the reformer (6) has a reforming chamber (6a) for reforming natural gas with steam and has a combustion chamber (6b) for maintaining reforming reaction temperature of the reforming chamber (6a). The apparatus of Claim 29, characterized in that an exit of the anode chamber (3) is connected with the combustion chamber (6b) of the reformer (6) by an anode exhaust gas line (8) , an air feed line (13) is connected to the anode exhaust gas line (8) and unreacted combustible gases contained in the anode exhaust gas are combusted in the combustion chamber (6b). The apparatus of Claim 30, characterized in that the H₂O separating and CO₂ recovering means (9, 11) draws the anode exhaust gas from the combustion chamber (6b) of the reformer (6) and includes a condenser (9) for condensing H₂O contained in the anode exhaust gas and a carbon dioxide recovering device (11) for recovering carbon dioxide gas discharged from the condenser (9) in the form of liquid. The apparatus of claim 28, characterized in that the apparatus further includes: a reformer (6, 30) having a reforming chamber (6a, 30a) for reforming natural gas with steam and a combustion chamber (6b, 30b) for maintaining reforming reactions at the reforming chamber (6a, 30a); means (7, 31) for supplying fuel gas reformed by the reforming chamber (6a, 30a) of the reformer (6, 30) into the anode chamber (3) of the fuel cell (FC); and means (4) for supplying oxidizing gas supplied to the cathode chamber (2) of the fuel cell (FC). The apparatus according to one of Claims 28 to 32, characterized in that the oxidizing gas supply means includes a line (4) for introducing oxidizing gas such as air into the cathode chamber (2), and a combustion exhaust gas line (5) extending from the fossil fuel combustion equipment (II) is connected with the oxidizing gas introducing line (4). The apparatus of Claim 32 or 33, characterized in that excessive fossil fuel to the combustion equipment (II) is guided into the combustion chamber (6b) of the reformer (6) to be burned therein. The apparatus according to claim 28 or 32, characterized in that the apparatus further includes: a carbon dioxide gas utilization line (20) for connecting an exhaust gas exit of the combustion equipment (III) with the cathode chamber (2) of the fuel cell (FC); and means (23) or feeding air into the utilization line (20). The apparatus of Claim 35, characterized in that a discharge line (28) for the anode exhaust gas is connected to the exit of the anode chamber (3) and there is provided a recirculation line (22) for mixing part of the anode exhaust gas with the fuel gas of the fuel gas supply means (21) to recirculate them into the anode chamber (3). The method of Claim 36, characterized in that a combustor (25) for introducing the anode exhaust gas is connected with the recirculation line (24) and the air feed line (26) is connected with the combustor (25) such that unreacted combustible gases of the anode exhaust gas are burned at the combustor (25), and an exit of the combustor is connected to the utilization line (20). The apparatus of claim 32 or 35, characterized in that the apparatus further includes: carbon dioxide gas utilization line (32) for connecting an exhaust gas exit of the combustion equipment (V) with the cathode chamber (2) of the fuel cell (FC); and means (34, 36) for feeding air into the utilization line. The apparatus according to one of claims 35 to 38, characterized in that the combustion equipment (V) includes a thermal power plant. The apparatus according to one of claims 35 to 39, characterized in that a discharge line for expelling to atmosphere the cathode exhaust gas from whose CO₂ has been diluted is connected to the cathode chamber (2). The apparatus of Claim 40, characterized in that an exit of the anode chamber (3) is connected with the combustion chamber (30b) of the reformer (30) by an anode exhaust gas like (35), the air feed line (36) is connected with the combustion chamber (30b) and a line (35) for guiding unreacted combustible gases of the anode exhaust gas is connected to the combustion chamber (30b) such that the unreacted combustible gases of the anode exhaust gas are burned at the combustion chamber (30b), and an exit of the combustion chamber (30b) is connected to the utilization line (32). The apparatus of claim 28, characterized in that the fossil fuel combustion equipment is a gas turbine generator (VI), and the apparatus further includes: a reformer (43) having a reforming chamber (43a) for reforming natural gas with steam and a combustion chamber (43b) for maintaining reforming reactions at the reforming chamber (43a); a carbon dioxide gas utilization line (41) connecting the turbine (40) with the cathode chamber (2) for supplying the combustion exhaust gas into the cathode chamber (2); and means (50, 42) for feeding pressurized air into the carbon dioxide gas utilization line (41). The apparatus of Claim 42, characterized in that a discharge like for expelling to atmosphere the cathode exhaust gas whose CO₂ has been diluted is connected to the cathode chamber (2), a power turbine (49) of an auxiliary turbine generator (53) which is driven by the cathode exhaust gas is connected to the discharge line (52) and a discharge end of a compressor (50) of the power generator (53) is connected to the carbon dioxide gas utilization line(41) by the pressurized air line (42). The apparatus of Claim 42 or 43, characterized in that a discharge line (54) for the anode exhaust gas is connected to the exit of the anode chamber (3), a line (54) for introducing part of the anode exhaust gas into the combustion chamber (43b) of the reformer (43) is connected to the exit of the anode chamber (3) such that unreacted combustible gases of the anode exhaust gas are burned at the combustion chamber (43b), and an exit of the combustion chamber (43b) is connected to the utilization line (41). The apparatus according to claim 38, characterized in that the apparatus further includes: means (XI, 82) for drawing the anode exhaust gas and separating H₂O from the anode exhaust gas and recovering CO₂. The apparatus of Claim 45, characterized in that a cathode gas discharge line (64) for expelling the cathode exhaust gas is connected to the cathode chamber (2), a turbine (65) of an auxiliary turbine generator is connected to the cathode gas discharge line (64) and a compressor (62) of the auxiliary generator is connected to the utilization line (60, 63). The apparatus according to one of Claims 32 to 34 and 45, 46, characterized in that the H₂O separating and CO₂ recovering means (76, 77, XI) draws the anode exhaust gas from the anode chamber (3) and includes a condenser (76, 77) for condensing H₂O contained in the anode exhaust gas and a carbon dioxide (XI) recovering device for recovering carbon dioxide gas discharged from the condenser (76, 77) in the form of liquid. The apparatus of Claim 47, characterized in that a line (83) for supplying into the combustion chamber (68b) of the reformer (68) the anode exhaust gas (8) whose CO₂ is removed by the carbon dioxide gas recovering device (XI) is connected to the carbon dioxide gas recovering device (XI) and unreacted combustible gases contained in the anode exhaust gas (8) are burned in the combustion chamber (68b). The apparatus of Claim 48, characterized in that a line (70) for supplying gases discharged from the combustion chamber (68b) of the reformer (68) into the cathode chamber (2) via the utilization line (63) is connected to the combustion chamber (68b) of the reformer (68).

Inventors: HATORI SATOSHI, HIRATA TETSUYA, IKEDA HIDETO, MIYAUCHI TOSHIO, NAKAZAWA KENZO, UEMATSU HIROYOSHI, HATORI, SATOSHI, HIRATA, TETSUYA, IKEDA, HIDETO, MIYAUCHI, TOSHIO, NAKAZAWA, KENZO, UEMATSU, HIROYOSHI
Applicants: ISHIKAWAJIMA HARIMA HEAVY IND, MIYAUCHI TOSHIO, ISHIKAWAJIMA-HARIMA HEAVY INDUSTRIES CO., LTD., MIYAUCHI, TOSHIO
Application year: 1990
Main classification: H01M8
IPC codes: C01B31, H01M8