Coal burner combined power plant having a fuel reformer

Abstract: A coal burner combined power plant, which includes a gas turbine (6) for burning coal in a furnace (1,12,14,15) under pressure and using produced gas, and a steam turbine (11) combined with an exhaust gas boiler (9) using exhaust gas from said gas turbine (6), and is structured so that another fuel is burned at an inlet of the gas turbine (6) for allowing the temperature at the inlet of said gas turbine to rise, characterized in that a fuel reformer (19) for reforming another fuel is located within said furnace (1,12,14,15).

Description: BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a combined power plant as defined in the preamble portion of claim 1 for utilities and industries. 2. Description of the Related Art Three examples of conventional coal burner combined power plants will be described hereunder. (First example) Fig. 12 is a diagram showing a systematic structure of a first example. A similar combined power plant disclosing the features of the preamble portion of claim 1 is described in "VGB Kraftwerkstechnik 73 (1993) 8, page 675. Coal serving as fuel is supplied to a pressure fluidized bed boiler 1 and then burned in the pressure fluidized bed boiler 1 by air which has been pressurized (about 10 to 30 kg/cm 2 ) by an air compressor 7 coupled to a gas turbine 6. The high-temperature combustion gas (about 850°C) is allowed to pass a cyclone 3 and ceramic filter 4, which serve as a dust removing unit. Since the combustion gas has a relatively low temperature as a temperature of a gas turbine inlet, natural gas is used as topping gas so as to be mixed with gas which has been burned by a burner 5. As a result, the temperature of the gas turbine inlet rises so that the efficiency of the plant is further enhanced. The gas turbine 6 drives the air compressor 7, thereby producing power at a power generator 8. The heat generated at the pressure fluidized bed boiler 1 is absorbed by a steam heat transfer tube 2. The steam system is heated by an exhaust gas boiler 9 using exhaust gas from the gas turbine, and a compound power generation cycle of the power generator 8 is constituted by the steam turbine 11 driven by the generated steam. The exhaust gas from the exhaust gas boiler 9 is discharged from a tunnel 10. (Second Example) Fig. 13 is a diagram showing a systematic structure of a second embodiment. A similar combined power plant as described in the preamble portion of claim 1 is disclosed in "VGB Kraftwerkstechnik 73 (1993) 8, page 675. Coal serving as fuel is partially burned into a gasified coal gas rich in carbon monoxide and hydrogen in a coal gasification furnace 12, and heat-exchanged in the heat transfer tube 2 to the steam system. Thereafter, the coal gas is allowed to pass a desulfurization/denitration unit 13 before being introduced to the gas turbine burner 5. For the purposes of compensating a heating value of gas produced in the coal gasification furnace 12 and of stabilizing the ignition of the gas turbine burner 5, natural gas as stabilizing fuel necessary for bringing flexibility of fuel as the power plant is mixed with gasified coal gas immediately before the gas turbine burner 5. The high-temperature gas which has been burned in the gas turbine burner 5 allows the gas turbine 6 to be driven so that the air compressor 7 is driven to generate power at the power generator 8. Further, downstream of the gas turbine 6, the exhaust gas boiler 9 exchanges heat with the steam system, and steam produced by heat supply due to the heat transfer section 2 within the coal gasification furnace allows the steam turbine 11 to be driven, thereby generating power at the power generator 8. The exhaust gas from the exhaust gas boiler 9 is discharged from the tunnel 10. (Third Example) Fig. 14 is a diagram showing a systematic structure of a third example. Coal serving as fuel is made to throw in a coal portion gasification furnace 14, and combustion/gasification is partially conducted in accordance with the invert ratio of coal. Unburnt char is made to throw in a full-quantity oxidation furnace 15. The full-quantity oxidation furnace 15 completely burns unburnt char as main fuel. The heat produced by the oxidation furnace 15 is absorbed by the steam system through the heat transfer section 2 disposed within the fluidized bed. After the gas produced from the oxidation furnace 15 is introduced into the coal portion gasification furnace 14, that gas is introduced together with gasified coal gas into the desulfurization furnace 16 where the gas is subjected to desulfurization in reducing atmosphere using a lime stone. Subsequently, after desulfurized fuel gas has passed the cyclone 3, it exchanges heat with the steam system at a gas cooler 17. Thereafter, the gas is again dust-removed through the ceramic filter 4 before being introduced into the gas turbine burner 5. Gas at the inlet of the gas turbine burner 5 is of low calorie gas, and provides excellent combustion as well as diversity and flexibility of fuel as a power plant. For this reason, natural gas is used as auxiliary/compound fuel immediately before the gas turbine burner 5. As a result, the gas turbine burner 5 enables excellent combustion. After gas has been burned by the gas turbine burner 5, the gas turbine 6 allows the air compressor 7 to be driven, and the power generator 8 generates power. A part of air compressed by the air compressor 7 is again boosted by an air booster 18 before being introduced into the gas portion gasification furnace 14 and the oxidation furnace 15. Because exhaust gas from the gas turbine has a high temperature such as about 560°C, heat of exhaust gas is collected by the steam system through the exhaust gas boiler 9. The steam system obtains heat values from the heat transfer tube 2 within the oxidation furnace 15, the gas cooler 17 and the exhaust gas boiler 9, and constitutes the compound power generation cycle of the power generator 8 coupled to the steam turbine 11. The conventional power plants suffer from no significant problems. However, from the viewpoints of effective utilization of energy resource and environment countermeasure as well as an improvement in profitability of a power plant, the present plant efficiency (42 to 49%) need be more improved. The general structure of a catalytic autothermal steam reformer arranged to supply reformed fuel and steam to a combustor zone of a gas turbine is described in EP-A-0 351 094. SUMMARY OF THE INVENTION An object of the present invention is to provide a combined power plant with improved efficiency. In order to solve this object there is provided a combined a power plant comprising a furnace for burning coal under pressure to produce a gas; a gas turbine driven by said gas; a burner for burning another fuel, said another fuel being natural gas, methanol or the like, said burner being connected with the inlet of said gas turbine for allowing the temperature at said inlet to rise, whereby said gas from said furnace being introduced to said gas turbine directly or via said burner; an exhaust gas boiler heated by exhaust gas from said gas turbine; and a steam turbine connected to said exhaust gas boiler; characterized in that a catalytic fuel reformer for reacting fuel and steam such that carbonoxides and hydrogen are produced is located within said furnace or within a gas cooler connected to said furnace. According to the present invention, a furnace for burning coal under pressure may be of a pressure fluidized bed boiler. In this case, the fuel reformer may be disposed within the pressure fluidized bed boiler. The location place for the reformer is selected in accordance with fuel to be reformed. Also, according to the present invention, a furnace for burning coal under pressure may be of a coal gasification furnace for partially burning coal. In this case, the fuel reformer may be disposed within the coal gasification furnace. In those structures, fuel which has been reformed by the fuel reformer is burned by the gas turbine burner disposed at the inlet of the gas turbine. Still further, according to the present invention, a furnace for burning coal under pressure may be of a coal gasification furnace having an oxidation furnace for completely burning unburnt char. In this case, the fuel reformer may be located within the oxidation furnace. In this structure, reformed fuel may be introduced into the coal gasification furnace or into the gas turbine burner. Yet still further, according to the present invention, a furnace for burning coal under pressure may be of a coal gasification furnace having a desulfurization furnace and a gas cooler. In this case, the fuel reformer may be located inside of any one of the desulfurization furnace and the gas cooler. In this case, reformed gas is burned by the gas turbine burner. According to the present invention, fuel to be reformed by the fuel reformer may be of natural gas, methanol or the like. In the coal burner combined power plant in accordance with the present invention, since the fuel reformer is located as described above, heat energy which has been collected by the steam system in the conventional power plant is exchanged into chemical energy by reforming fuel in the fuel reformer. After reforming, fuel gas is directly burned to provide actuating fluid, and power is generated by the gas turbine using the actuating fluid. Also, according to the present invention, since fuel reformation makes the heat value of fuel rise, fuel consumption can be reduced. For example, in the case where natural gas is reformed under the condition where a reformation temperature is 800°C, a reformation pressure is 30 ata, and the mole ratio (hereinafter referred to as "S/C") of steam S to carbon within natural gas is 2.5, a higher heating value rises about 1.167 times. If a description will be given in more detail, a reaction formula for steam reformation of natural gas is stated below. CnHm + nH 2 O ⇒ nCO + (m/2 + n)H 2 - Q (endoergic) Methane mainly occupying natural gas is: CH 4 + H 2 O ⇒ CO + 3H 2 - 49.3 (kcal/mol) The ideal heating value before and after reforming increases from CH 4 = 212.8 (kcal/mol) to CO (67.7 kcal/mol) + 3H 2 (3 x 68.3 68.3 kcal/mol) = 272.6 (kcal/mol), that is, 1.28 times. However, in fact, the gas composition after reforming is different depending on the reforming conditions (temperature, pressure, S/C) as shown in Fig. 9, and the increase rate of the higher heating value becomes slightly low as shown in Fig. 10. In steam used in reforming, for the purpose of preventing the precipitation of carbon within catalyst (nickel catalyst with a carrier of alumina), S/C of 2.5 or more is required. However, because throw-in of a large amount of steam leads to an increase of moisture loss, the range of S/C = 2 to 4 is selected. Subsequently, a description will be given of a case where methanol is fuel-reformed. In this case, a chemical reaction formula is stated below. CH 3 OH ⇒ CO + 2H 2 - 21.7 (kcal/mol) CO + H 2 O ⇒ CO 2 + H 2 - 9.83 (kcal/mol) Copper based catalyst is used for reformation catalyst, and reformation is conducted under the conditions where temperature is about 200 to 300°C, and pressure is 10kg/cm 2 or less, that is, low pressure. Also, for the purpose of preventing the precipitation of carbon within catalyst, S/C is set to about 2 to 3 for conducting reaction. Next, an operation when the fuel reformation is assembled into a compound cycle will be described. As shown in Figs. 11(a) and 11(b), a part of heat energy, which has thrown in a steam Rankine cycle within the cycle in the prior art of Fig. 11(a), is converted into chemical energy by using a fuel reforming action. The chemical energy is moved to the compound cycle (of the Brayton cycle + the Rankine cycle) as shown in Fig. 11(b) so that it can be directly burned into gas turbine operating fluid. As a result, the quantity of entropy production is reduced, thereby improving the efficiency of a plant. Further, in the present invention, since the fuel reformer is disposed within a furnace containing a high-temperature combustion gas therein, methanol which allows temperature necessary for reforming to be 300°C as well as natural gas or the like which requires reformation at a high temperature (about 550 to 850°C) can be used as fuel. The fact is well known that the efficiency of a power plant is more improved as a difference in temperature between the heat supply side (a high-temperature side) and the heat receiving side (a low-temperature side) is made small. In the present invention, after the temperature of the high-temperature combustion gas is lowered once by using the high-temperature heat of combustion gas for reformation of fuel, combustion gas is assembled into the power generation cycle. As a result, not only the efficiency of power generation is improved for that reason, but also the efficiency is also improved by reforming fuel. Hence, the efficiency of a power plant is remarkably improved. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a structural diagram showing a power generating system in accordance with a first embodiment of the present invention; Fig. 2 is a structural diagram showing a power generating system in accordance with a second embodiment of the present invention; Fig. 3 is a structural diagram showing a power generating system in accordance with a third embodiment of the present invention; Fig. 4 is a structural diagram showing a power generating system in accordance with a fourth embodiment of the present invention; Fig. 5 is a structural diagram showing a power generating system in accordance with a fifth embodiment of the present invention; Fig. 6 is a structural diagram showing a power generating system in accordance with a sixth embodiment of the present invention; Fig. 7 is a perspective view showing one example of the structure of a fuel reformer used in the power plant of the present invention; Fig. 8 is an explanatory diagram showing a temperature control method in the fuel reformer used in the power plant of the present invention; Fig. 9 is a graph representing a mole ratio of gas composition after fuel reformation due to the fuel reformer in the power plant of the present invention; Fig. 10 is a graph representing an increment ratio of a higher heating value after fuel reformation due to the fuel reformer in the power plant of the present invention; Figs. 11(a) and 11(b) are diagrams showing a change of an energy flow due to fuel reformation in the power plant of the present invention; Fig. 12 is a systematic structural diagram showing a conventional power plant where coal is burned under a pressure fluidized bed; Fig. 13 is a systematic structural diagram showing another conventional power plant for gasifying coal; and Fig. 14 is a systematic structural diagram showing a topping power generation cycle where coal portion gasification and a fluidized bed combustion are combined. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, a description will be given in detail of a coal burner combined power plant in accordance with the embodiments of the present invention with reference to the accompanying drawings. In the embodiments as will be described below, the parts identical to those of the conventional power plants shown in Figs. 12 to 14 are designated by the same symbols and their description is omitted because of duplication. (First Embodiment) Fig. 1 shows a first embodiment of the present invention. In this embodiment, a fuel reformer 19 is disposed within a pressure fluidized bed boiler 1 in the conventional plant shown in Fig. 12. In other words, a steam heat transfer tube 2 as well as a fuel reformer 19 is disposed within the fluidized bed in a furnace where the fluidized bed is burned under pressure. After natural gas is reformed under the conditions where a reformation temperature is 800°C, a reformation pressure is 30 ata and S/C is 2.5, so as to be converted into gas having a higher heating value, the gas is burned by a gas turbine burner 5 before being mixed with combustion gas which has been produced at point A due to fluidized bed combustion. Fig. 7 shows one example of the structure of the fuel reformer 19. The fuel reformer is of a double-tube structure. After gas is made to flow in an inner cylinder thereof and preheated, the gas is reformed by catalyst which is filled in an outer cylinder thereof. Because the inlet temperature of the catalyst layer must be about 450 to 500°C (depending upon the catalyst characteristics), temperature control using a bypass spray which is controlled by a temperature control bypass valve 21 as shown in Fig. 8 is required. The temperature of gas produced from the fluidized bed combustion is relatively low, that is, about 850°C. However, after being dust-removed through a cyclone 3 and a ceramic filter 4, that gas is mixed with high-temperature gas, which has been burned in the burner 5 into high-temperature gas of 1,300 °C or higher. The high-temperature gas is introduced into a gas turbine 6 and drives a compressor 7 to thereby generate power at a power generator 8. The efficiency of the gas turbine is remarkably improved by making the inlet temperature of the gas turbine higher. With making the inlet temperature of the gas turbine higher, the temperature of exhaust gas from the gas turbine rises similarly and the quantity of heat collection at the exhaust gas boiler 9 is also increased. The exhaust gas from the exhaust gas boiler 9 is discharged from a tunnel 10. A steam system receives heat supply from the exhaust gas boiler 9 as well as a heat transfer tube 2 disposed within a layer of fluidized bed combustion under pressure. The steam system then allows the steam turbine 11 to generate power at the power generator 8. With this system, the efficiency of the plant is improved by about 4% as a relative value. In the power plant in accordance with this embodiment, because the fuel reformer 19 is disposed within the fluidized layer of the pressure fluidized bed boiler 1, in the heat transfer within the fluidized layer, the heat transfer coefficient is largely high (3 to 5 times as high as convective heat transfer). Therefore, a difference between the temperature of the fluidized layer and the temperature of the surface of the heat transfer tube can be remarkably reduced, compared with a case of the heat transfer due to fire radiation or gas convection at a fire furnace or a gas turbine combustion chamber. Further, because temperature and the heat transfer coefficient are uniform within the fluidized layer, damage to the heat transfer tube due to local temperature rising is difficult to cause. Therefore, there is an advantage in that gas within the heat transfer tube can be heated to high temperature. (Second Embodiment) Fig. 2 shows a second embodiment of the present invention. In this embodiment, a fuel reformer 19 is disposed within the coal gasification furnace 12 in the conventional plant shown in Fig. 13. In Fig. 2, using gasified coat gas from the gasification furnace 12 which partially burns coal, the fuel reformer 19 is disposed in a part of the coal gasification furnace 12, where a steam system heat transfer tube 2 has been disposed in the conventional plant. With this structure, natural gas is reformed under the reformation condition where the reformation temperature is 800°C, the reformation pressure is 30 ata and S/C is 2.5. The gas is then mixed with gasified coal gas which has passed a desulfurization/dust-removing unit 13 before being burned by the burner 5 immediately before the gas turbine 6. Subsequently, that gas allows the gas turbine 6 to drive the compressor 7, to thereby generate power at the power generator 8. Because the exhaust gas from the gas turbine has high temperature, it is combined with a heat collecting boiler 9 to constitute a compound cycle which makes the steam turbine 11 generate power at the power generator 8. The exhaust gas at the outlet of the heat collecting boiler 9 is discharged through the tunnel 10. As a result, the efficiency of a plant is improved 4% as a relative value. (Third Embodiment) Fig. 3 shows a third embodiment of the present invention. In this embodiment, a fuel reformer is disposed within the oxidation furnace 15 in the conventional plant shown in Fig. 14. Using heat produced from the oxidation furnace 15 which completely burns as main fuel unburnt char which is obtained by partially burning in the gasification furnace 14, natural gas is reformed by the fuel reformer 19 under the reformation conditions where the reformation temperature is 800°C, the reformation pressure is 30 ata and S/C is 2.5. Reformed gas contains a large quantity of steam as described above, and throws in the gasification furnace. Gasified coal gas and reformed gas are mixed together in the gasification furnace 14 and then reduced under reducing atmosphere in the desulfurization furnace 16. Subsequently, after the gas exchanges heat with the steam system in the gas cooler 17 through the cyclone 3, the gas passes the ceramic filter 4 before being burned in the gas turbine burner 5. The gas allows the gas turbine 6 to drive the compressor 7, thereby generating power at the power generator 8. The air compressed by the compressor 7 is further boosted by the air booster 18 before being introduced into the gasification furnace 14 and the oxidation furnace 15. Downstream of the gas turbine 6 is an exhaust gas boiler 9 for collecting heat using high-temperature exhaust gas from the gas turbine. The exhaust gas exchanges heat with the steam system and is then discharged from the tunnel 10. The steam system receives heat supply from the gas cooler 17 and the exhaust gas boiler 9 allows the steam turbine 11 to generate power at the power generator 8. Thus, the plant system of the high efficiency as a whole is constituted and improved 4% as a relative value. (Fourth Embodiment) Fig. 4 shows a fourth embodiment of the present invention. As similar in the third embodiment, in this embodiment, a fuel reformer 19 is disposed within the oxidation furnace 15. In the fourth embodiment, reformed gas resulting from reforming natural gas under the conditions where reformation temperature is 800°C, reformation pressure is 30 ata and S/C is 2.5 is mixed with gasified coal gas at a point A immediately before not the gasification furnace 14 but the gas turbine burner 5. Because reformed gas at the outlet of the steam generator 20 is at 450°C and is mixed with gasified coal gas immediately before the burner 5, the capacity of the gas cooler 17, the cyclone 3, the ceramic filter 4, which constitute a dust collector, can be reduced. As a result, the mechanical equipment costs as the entire plants can be reduced to about 60% of that in the third embodiment. However, since steam for preventing the precipitation of carbon newly throws in the gasification furnace 14, the efficiency of the plants is improved about 3% as a relative value, which is slightly lower than that in the third embodiment. (Fifth Embodiment) Fig. 5 shows a fifth embodiment of the present invention. In this embodiment, a fuel reformer 19 is disposed within the gas cooler 17 in the conventional plant shown in Fig. 14. This embodiment is identical to the fourth embodiment except that the reformation of natural gas under the conditions where reformation temperature is 800°C, reformation pressure is 30 ata and S/C is 2.5 is conducted using gasified coal gas which has passed the cyclone 3 from the outlet of the desulfurization furnace 16. (Sixth Embodiment) Fig. 6 shows a sixth embodiment of the present invention. In this embodiment, a fuel reformer is disposed within the pressure fluidized bed boiler 1 as in the first embodiment so that methanol is reformed. The reformation of methanol is enabled at a low heating value, that is, about 21.7 kcal with respect to one mole of methanol. In this embodiment, using the heat produced by the pressure fluidized bed boiler 1, the methanol reformer 19 is disposed within the fluidized bed for reforming the fuel of methanol. After being burned in the gas turbine burner 5, reformed methanol gas is mixed with combustion gas which has passed the dust removing unit at the point A immediately before the gas turbine. Because the temperature of the exhaust gas from the gas turbine is 400 to 500°C, this is, high temperature, the exhaust gas is heat-recovered by an exhaust heat recovery feedwater heater, that is, the exhaust gas boiler 8 after having passed the denitration unit 22 so that a power generator 8 coupled to the steam turbine 11 generates power. As in the fuel reformer 19 shown in Fig. 7, the fuel reformer 19 for reforming methanol is of a double-tube structure, in which copper based catalyst is filled in between the inner and outer cylinders thereof. Methanol and steam are made to enter from the inner cylinder, and reheated for the purpose of restraining the precipitation of carbon within catalyst as much as possible. Subsequently, the tube bottom is reversed so that methanol is introduced to the outer cylinder, thus reforming methanol. According to this embodiment, the efficiency of the plant is improved about 3% as a relative value. In Fig. 6, reference numeral 23 denotes a condenser, and 24 is a water supply pump. As was described above, in the combined power plant of the present invention, a fuel reformation process is assembled into the conventional coal burner combined cycle with a result that the efficiency of the plant is remarkably improved. This is a very important matter from the viewpoints of effective utilization of energy resource and environmental countermeasures, and simultaneously economics of the power plants is remarkably improved.

Claims: A combined power plant comprising: a furnace (1,12,14,15) for burning coal under pressure to produce a gas; a gas turbine (6) driven by said gas; a burner (5) for burning another fuel, said another fuel being natural gas, methanol or the like, said burner (5) being connected with the inlet of said gas turbine (6) for allowing the temperature at said inlet to rise, whereby said gas from said furnace (1,12,14,15) being introduced to said gas turbine (6) directly or via said burner (5); an exhaust gas boiler (9) heated by exhaust gas from said gas turbine (6); and a steam turbine (11) connected to said exhaust gas boiler (9); characterized in that a catalytic fuel reformer (19) for reacting fuel and steam such that carbonoxides and hydrogen are produced is located within said furnace (1,12,14,15) or within a gas cooler (17) connected to said furnace (14,15). A combined power plant as claimed in claim 1, wherein said furnace is of a pressure fluidized bed boiler (1) within which said fuel reformer (19) is disposed so that reformed fuel is lead to a gas turbine burner (5). A combined power plant as claimed in claim 1, wherein said furnace is of a coal gasification furnace (12) for partially burning coal, within which said fuel reformer (19) is disposed so that reformed fuel is lead to a gas turbine burner (5). A combined power plant as claimed in claim 1, wherein said furnace is of a coal gasification furnace (14) having an oxidation furnace (15) for completely burning unburnt char as main fuel, and said fuel reformer (19) is disposed within said oxidation furnace (15) so that reformed fuel is lead to said coal gasification furnace (14). A combined power plant as claimed in claim 1, wherein said furnace is of a coal gasification furnace (14) having an oxidation furnace (15) for completely burning unburnt char as main fuel, and said fuel reformer (19) is disposed within said oxidation furnace (15) so that reformed fuel is lead to said burner (5). A combined power plant as claimed in claim 1, wherein said furnace is of a coal gasification furnace (14) having a desulfurization furnace (16) and a gas cooler (17), and said fuel reformer (19) is disposed within at least one of said desulfurization furnace (16) and said gas cooler (17) so that reformed fuel is lead to said burner (5). A combined power plant as claimed in any one of claims 1 to 6, wherein said another fuel is of natural gas. A combined power plant as claimed in any one of claims 1 to 6, wherein said another fuel is of methanol.

Inventors: HYAKUTAKE YOSHINORI, KANEKO SHOZO, KOBAYASHI YOSHINORI, SATO SUSUMU, UCHIDA SATOSHI, WAKABAYASHI YOSHIYUKI, YAMAUCHI YASUHIRO, HYAKUTAKE, YOSHINORI,, KANEKO, SHOZO,, KOBAYASHI, YOSHINORI,, SATO, SUSUMU,, UCHIDA, SATOSHI,, WAKABAYASHI, YOSHIYUKI,, YAMAUCHI, YASUHIRO,, HYAKUTAKE, YOSHINORI, C/O MITSUBISHI JUKOGYO K. K., KANEKO, SHOZO, C/O MITSUBISHI JUKOGYO K. K., KOBAYASHI, YOSHINORI, C/O MITSUBISHI JUKOGYO K. K., SATO, SUSUMU, C/O MITSUBISHI JUKOGYO K. K., UCHIDA, SATOSHI, C/O MITSUBISHI JUKOGYO K. K., WAKABAYASHI, YOSHIYUKI, C/O MITSUBISHI JUKOGYO KK., YAMAUCHI, YASUHIRO, C/O MITSUBISHI JUKOGYO K. K.
Applicants: MITSUBISHI HEAVY IND LTD, MITSUBISHI JUKOGYO KABUSHIKI KAISHA
Application year: 1995
Main classification: F01K23
IPC codes: F02C6, F01K23, F02C3, F02C7