AU742742B2 - Method of manufacturing hydrogen/carbon-monoxide mixture gas, system thereof, and fuel/electric-power co-production plant - Google Patents
Method of manufacturing hydrogen/carbon-monoxide mixture gas, system thereof, and fuel/electric-power co-production plant Download PDFInfo
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- AU742742B2 AU742742B2 AU69696/00A AU6969600A AU742742B2 AU 742742 B2 AU742742 B2 AU 742742B2 AU 69696/00 A AU69696/00 A AU 69696/00A AU 6969600 A AU6969600 A AU 6969600A AU 742742 B2 AU742742 B2 AU 742742B2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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AUSTRALIA
PATENTS ACT 1990 COMPLETE SPECIFICATION NAME OF APPLICANT(S): Hitachi, Ltd. AND Babcock-Hitachi Kabushiki Kaisha ADDRESS FOR SERVICE: DAVIES COLLISON CAVE Patent Attorneys 1 Little Collins Street, Melbourne, 3000.
INVENTION TITLE: Method of manufacturing hydrogen/carbon-monoxide mixture gas, system thereof, and fuel/electric-power co-production plant The following statement is a full description of this invention, including the best method of performing it known to me/us:- 1A The present invention relates to a method of manufacturing hydrogen/carbon-monoxide mixture gas by gasifying carbon group fuel such as coal, heavy mass oil and coal bed gas using oxygen, steam and so on, and a system of manufacturing hydrogen and carbon monoxide mixing gas, and a fuel producing and electric power generating combined plane comprising the system of manufacturing m f15 hydrogen/carbon-monoxide mixture gas.
In a coalfield mining coal, coal bed gas containing methane as the main component may be produced. The main object of collecting the coal bed gas may be to secure safety of the mining activity, and most part of the collected coal bed gas may be disposed without using though a part of the collected coal bed gas is used as fuel. Therefore, effective use of the coal bed gas is required from the viewpoint of energy saving. In addition, it is calculated in the framework treaty on climatic change that the greenhouse effect of methane is 21 times as large as that of carbon dioxide, and accordingly the effective use of the coal bed gas is also important from the viewpoint of prevention of global warming.
In regard to the conventional technology using the coal bed gas containing methane as the main component, Japanese Patent Application Laid-Open No.9-67582 discloses a method that a hydrogen/carbon-monoxide mixture gas is manufactured using coal and methane as the raw materials by supplying coal and methane to a gasifier furnace. In the conventional technology, the coal and the methane to be 10 used as the raw materials are pressurized to be supplied to the gasifier furnace operated under about 30 atmospheric *pressures. Further, steam reforming reaction of methane may be produced in the furnace in order to increase the ratio of hydrogen to carbon monoxide. The hydrogen-carbon monoxide 15 mixed gas obtained as described above may be used in an electric power generation system using a gas turbine or a fuel cell, in a fuel manufacturing system for manufacturing fuel such as methanol, methyl ether, an FT synthesized oil, or in a fuel/electric-power co-production plant for producing fuel and generating electric power at a time.
Although the method described above is effective, for obtaining highly pure methane, it may be difficult to pressurizing the methane because the coal bed gas collected as one of the minin activities contains air (oxygen) and it also may be difficult to obtain a high temperature for progressing the steam reforming reaction. This is because the gas temperature becomes approximately 600 °C when the P:\OPERMCU2355533 sp.doc-OI/l Iml -3coal bed gas is pressurized up to 30 atmospheric pressures using the compressor, and on the other hand the ignition temperature of methane is 630 20 °C and accordingly there may be possibility that the methane and the oxygen contained in the coal bed gas may rapidly react with each other.
Further, nitrogen in the air is inactive to the reaction, and it may become difficult to maintain the high temperature when the air is mixed into the coal bed gas 10 because the thermal energy to increase the temperature of the nitrogen is required. The temperature is approximately 330 °C when the coal bed gas is pressurized up to S" atmospheric pressures, and accordingly the methane and the oxygen do not rapidly react with each other under this 15 pressure. However, the size of the gasifier furnace in the case of gasification under 10 atmospheric pressures becomes three times as large as the size in the case of gasificatin, :under 30 atmospheric pressures, and accordingly there may arise a problem of increasing the cost.
SUMMARY OF THE INVENTION An object of embodiments of the present invention is to provide a method and a system which are capable of manufacturing hydrogen/carbon-monoxide mixture gas having a high hydrogen ratio from coal and coal bed gas without steam reforming reaction. A further object of embodiments of the present invention is to provide a fuel/electric-power coproduction plant which comprises a system for synthesizing a fuel from a hydrogen/carbon-monoxide mixture gas and an electric power generation system for generating electric power using the synthesized fuel.
P:A)PERORJC2355533 spe.do-3 /lOA)I -4- In accordance with the present invention, there is provided a method of manufacturing hydrogen/carbon-monoxide mixture gas from a carbon group fuel and a coal bed gas containing methane as a main component, the method comprising the steps of: forming hydrogen and carbon monoxide by partially oxidizing said carbon group fuel and said coal bed gas; and making reaction between part of said carbon monoxide and 10 steam to form hydrogen in order to increase a hydrogen ratio of said hydrogen/carbon-monoxide mixture gas.
Preferably, the method further comprising the steps of: supplying said carbon group fuel and said coal bed gas and an oxidation agent into an upstream zone of a gasification apparatus to partially oxidize said carbon group fuel and said coal bed gas, gas flowing in one direction said gasification apparatus; and making shift reaction of the carbon monoxide formed by said partial oxidation by supplying steam into a downstream zone of said gasification apparatus.
In accordance with the present invention, there is also provided a method of manufacturing hydrogen/carbon-monoxide mixture gas from a carbon group fuel and a coal bed gas containing methane as a main component, the method comprising the steps of: partially oxidizing said carbon group fuel in two zones of an upstream zone and a downstream zone of a gasification apparatus, gas flowing in one direction in said gasification apparatus; partially oxidizing said coal bed gas, and burning part P: OPERRJCU355533 spe.doc.05/I 1/01 of said carbon group fuel in said upper zone; and making shift reaction of said formed carbon monoxide in said downstream zone to increase a hydrogen ratio of said hydrogen/carbon-monoxide mixture gas.
By burning part of the carbon group fuel in the upper S: zone in the gasification apparatus, temperature in the .furnace of the upstream zone is increased and accordingly an ash component formed in association with gasification of the o. 10 carbon group fuel is melted to suppress the ash component from attaching to the furnace wall.
**Preferably, steam for preventing temperature rise of a furnace wall of said gasification apparatus is supplied to said upper zone of said gasification apparatus.
Preferably, the gasification reaction in each of sa~j., upstream zone and said downstream zone is performed by forming a swirl flow of supplied raw materials, and a magnitude of the swirl flow in said downstream zone is larger than a magnitude of the swirl flow in said upstream zone.
In accordance with the present invention, there is also provided a method of manufacturing hydrogen/carbon-monoxide mixture gas from raw materials of a carbon group fuel and a coal bed gas containing methane as a main component using a gasification apparatus of a pressurized gas type, the method comprising the steps of: partially oxidizing said coal bed gas to reduce an amount of oxygen contained in said coal bed gas in prior to supplying said coal bed gas to said gasification apparatus; I- after that P:PWERRJ02355533 p.doc-~/111Ol -6partially oxidizing said coal bed gas and said carbon group fuel by supplying said coal bed gas reduced in the amount of oxygen and said carbon group fuel and an oxidation agent to said gasification apparatus; and making shift reaction of part of the carbon monoxide formed by said partial oxidation by supplying steam into a downstream zone of said gasification apparatus.
Preferably, the partial oxidation reaction of Chemical Formula occurs by the carbon group fuel and the partial oxidation reaction of Chemical Formula occurs by the coal bed gas.
Preferably, the shift reaction of the carbon monoxide shown by Chemical Formula occurs. The symbol CH in Chemical Formula expresses coal, and the symbol CH 4 in the Chemical Formula expresses methane in the coal bed, gas.
Preferably, in the case where the method of manufacturing hydrogen/carbon-monoxide mixture gas in accordance with the present invention is performed using the gasification apparatus in which gas flows in one direction, the method of partially oxidizing the coal bed gas only in the upstream zone or the method of partially oxidizing the coal bed gas in both of the upstream zone and the downstream zone is included.
2CH 02 2CO H 2 (1) 2CH 4 02 2CO 4H 2 (2) It can be understood from Chemical Formula that the hydrogen/carbon monoxide ratio of the gas obtained by the gasification of coal is about 0.5, and it can be understood from Chemical Formula that the hydrogen/carbon monoxide ratio of the gas obtained by the gasification of coal bed gas is about 2. Therefore, the hydrogen/carbon monoxide ratio can be adjusted by mixing these gases.
Further, by causing the shift reaction of Chemical Formula the hydrogen/carbon monoxide ratio can be further increased.
CO H 2 0 C0 2
H
2 (3) In a case where the method of manufacturing hydrogen/carbon-monoxide mixture gas in accordance with the present invention is performed using a gasification apparatus of a pressurized gas type, it is preferable that the coal bed gas is partially oxidized by the oxygen contained in the coal bed gas in prior to supplying the coal bed gas to the gasification apparatus to remove the oxygen from the coal bed gas. In this case, the coal bed gas flows out of a coal bed gas tank of a coal bed gas supply system, and is reduced in oxygen concentration by partially oxidized in a partial oxidation unit, and is cooled by a heat exchanger before being pressurized because temperature of the coal bed gas is increased by the partial oxidation reaction. The oxygen concentration of the coal bed gas becomes nearly zero by the partial oxidation reaction, and accordingly the coal bed gas does not rapidly react with oxygen even if it is compressed up to a high pressure. Thus, the coal bed gas can be pressurized up to nearly 30 atmospheric pressures to be supplied to the gasification apparatus.
The amount of oxygen in the coal bed gas is preferably short of completely burning the methane, and the oxygen is preferably consumed in progressing the partial oxidation reaction of methane of Chemical Formula In the stage S: before supplying the coal bed gas to the gasification apparatus, it is preferable that the reaction temperature in the partial oxidation reaction of methane by the oxygen in ooo :the coal bed gas is increased above 1000 °C in order to 10 improve the reaction between methane and oxygen. Therefore, it is preferable to make use of catalytic burning reaction.
By removing or reducing the oxygen in the coal bed gas in prior to supplying the coal bed gas to the 15 gasification apparatus, the coal bed gas does not rapidly react with oxygen even if the coal and the coal bed gas are reacted with each other under a high pressure condition, and the hydrogen/carbon-monoxide mixture gas can be efficiently manufactured, and the system can be made small in size. Further, a mixture gas having an optimum hydrogen/carbon monoxide ratio can be manufactured corresponding to a synthesized fuel. Furthermore, it may be possible to effectively use the coal bed gas which has been disposed, and to attain energy saving, and to contribute to prevention of the global warming.
P:XOPERUC%2355533 Spe.dc-3 I/OOI -9- In accordance with the present invention, there is also provided a system of manufacturing hydrogen/carbon-monoxide mixture gas from raw materials of a carbon group fuel and a coal bed gas containing methane as a main component qsing a gasification apparatus, which comprises: said gasification apparatus in which gas flows in one direction; a supply system for supplying said carbon group fuel and *e..9said coal bed gas and an oxidation agent to an upstream zone 9*° 10 of said gasification apparatus so that said carbon group fuel *.9.9and said coal bed gas are partially oxidized in said upstream zone; and a supply system for supplying steam to a downstream zone of said gasification apparatus so that part of said carbon monoxide formed in said upstream zone is shifted to hydrogen 9 in said downstream zone.
9 In accordance with the present invention, there is also provided a system of manufacturing hydrogen/carbon-monoxide mixture gas from raw materials of a carbon group fuel and a coal bed gas containing methane as a main component using a gasification apparatus, which comprises: said gasification apparatus in which gas flows in one direction; a supply system for supplying said carbon group fuel and said coal bed gas and an oxidation agent to an upstream zone of said gasification apparatus so that said carbon group fuel is partially oxidized and burned, and said coal bed gas is partially oxidized in said upstream zone; and a supply system for supplying said carbon group fuel and the oxidation agent and steam to a downstream zone of said Sgasification apparatus so that said carbon group fuel is P.OPERWCX2355533 spe.doc-3 I/l0I partially oxidized and shift reaction of part of said carbon monoxide formed by partial oxidation of said carbon group fuel and said coal bed gas in said downstream zone.
In accordance with the present invention, there is also provided a system of manufacturing hydrogen/carbon-monoxide o• :i mixture gas from raw materials of a carbon group fuel and a coal bed gas containing methane as a main component using a gasification apparatus of a pressurized gas type, which S 10 comprises: said gasification apparatus in which gas flows in one direction; a supply system for supplying said carbon group fuel and said coal bed gas and an oxidation agent to an upstream zone of said gasification apparatus so that said carbon group fuel and said coal bed gas are partially oxidized in said upstream *.o zone; a supply system for supplying steam to a downstream zone of said gasification apparatus so that shift reaction of part of said carbon monoxide formed by partial oxidation of said carbon group fuel and said coal bed gas in said downstream zone; and a partial oxidation unit for partially oxidizing said coal bed gas with oxygen contained in said coal bed gas before supplying said coal bed gas to said upstream zone to reduce an amount of oxygen contained in said coal bed gas.
In accordance with the present invention, there is also provided a system of manufacturing hydrogen/carbon-monoxide mixture gas from raw materials of a carbon group fuel and a coal bed gas containing methane as a main component using a Sgasification apparatus of a pressurized gas type, which P:OPERJC22355533 spc.doc-3 1/1001 -11comprises: said gasification apparatus in which gas flows in one direction; a supply system for supplying said carbon group fuel and said coal bed gas and an oxidation agent to an upstream zone of said gasification apparatus so that said carbon group fuel is partially oxidized and burned, and said coal bed gas is partially oxidized in said upstream zone; a supply system for supplying said carbon group fuel and 10 the oxidation agent and steam to a downstream zone of said gasification apparatus so that shift reaction of part of said carbon monoxide formed by partial oxidation of said carbon group fuel and said coal bed.gas in said downstream zone; and a partial oxidation unit for partially oxidizing said coal bed gas with oxygen contained in said coal bed gas before supplying said coal bed gas to said upstream zone to 000 reduce an amount of oxygen contained in said coal bed In accordance with the present invention, there is also provided a fuel/electric-power co-production plant comprising: the above described system of manufacturing hydrogen/carbon-monoxide mixture gas; a gas purification apparatus for purifying a hydrogen/carbon-monoxide mixture gas manufacture by said system of manufacturing hydrogen/carbon-monoxide mixture gas; a fuel synthesis apparatus for synthesizing any one of methanol, dimethyl ether and an FT synthesized oil from said hydrogen/carbon-monoxide mixture gas purified by said gas purification apparatus; and RT e an electric power generation system for generating jelectric power using said fuel synthesized by said fuel P:\OPERURJC2355533 spe.doc-3 1/IOAI -12synthesis apparatus as a power source.
In accordance with the present invention, there is also provided a fuel/electric-power co-production plant comprising: the above described system of manufacturing f* ".hydrogen/carbon-monoxide mixture gas; gas purification apparatus for purifying a 10 hydrogen/carbon-monoxide mixture gas manufacture by said S. system of manufacturing hydrogen/carbon-monoxide mixture gas; a fuel synthesis apparatus for synthesizing any one of methanol, dimethyl ether and an FT synthesized oil from said hydrogen/carbon-monoxide mixture gas purified by said gas 15 purification apparatus; and an electric power generation system for generating electric power using said fuel synthesized by said f.,L synthesis apparatus and not-reacted gases as a power source.
Preferably, the mixture gas having a hydrogen/carbon monoxide ratio suitable for a fuel such as methanol, dimethyl ether, an FT synthesized oil or the like can be efficiently manufactured.
Preferably, since the coal bed gas is supplied to the gasification apparatus after reducing the oxygen in the coal bed gas through the partial oxidation, the coal bed gas can be compressed up to a high pressure, and accordingly the system can be made small in size and low in cost.
P:OPER\RJC\2355533 spe.doc-31/OA)l -12A- Preferably, the fuel/electric-power co-production plant comprising the system of manufacturing hydrogen/carbonmonoxide mixture gas can attain energy saving by effective use of the coal bed gas, and is also effective for preventing the global warming.
BRIEF DESCRIPTION OF THE DRAWINGS **0 FIG. 1 is a block diagram showing an embodiment of a 10 fuel/electric-power co-production plant comprising a system for manufacturing a hydrogen/carbon-monoxide mixture gas in accordance with the present invention.
FIG. 2 is a block diagram showing the coal bed gas 0 supply system of FIG. 1.
15 FIG. 3 is a cross-sectional view showing the partial oxidation unit of FIG. 2.
@00 FIG. 4 is a view showing the detailed construction ,of the gasification apparatus of FIG. 1.
FIG. 5 is a cross-sectional view showing the adjusting reaction portion of FIG. 4, and FIG. 5 is a cross-sectional view showing the gasification reaction portion of FIG. 4.
FIG. 6 is a diagram showing a control system of the adjustment apparatus of FIG. 1.
FIG. 7 is a block diagram showing another embodiment of a fuel/electric-power co-production plant comprising a system for manufacturing a hydrogen/carbon-monoxide mixture 13 gas in accordance with the present invention.
FIG. 8 shows another embodiment of a gasification apparatus, and FIG. 8 is a cross-sectional view showing the adjusting reaction portion, and FIG. 8 is a crosssectional view showing the gasification reaction portion.
FIG. 9 is a block diagram showing another embodiment of a coal bed gas supply system.
FIG. 10 is a cross-sectional view showing another embodiment of a partial oxidation unit.
DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of a fuel/electric-power co-production plant comprising a system of manufacturing hydrogen/carbonmonoxide mixture gas in accordance with the present 15 invention will be described below in detail, referring to the accompanied drawings. FIG. 1 is a block diagram showing S. an embodiment of a fuel/electric-power co-production plant 0. comprising a system for manufacturing a hydrogen/carbonmonoxide mixture gas in accordance with the present invention. In FIG. 1, a system of manufacturing hydrogen/carbon-monoxide mixture gas 10 is a system of manufacturing hydrogen/carbon-monoxide mixture gas by gasifying coal 1 of a carbon group fuel and coal bed gas 2 using oxygen 3 and by shift-reacting the produced carbon monoxide using steam 4. The system of manufacturing hydrogen/carbon-monoxide mixture gas 10 is constructed so that the coal 1 and the coal bed gas 2 are supplied to a 14 gasification apparatus 20 to produce a gas by progressing gasification reaction of the coal 1 and the coal bed gas 2 in the gasification apparatus 20, and a hydrogen/carbon monoxide ratio is adjusted by adjusting the proportions of supplying amounts of the coal 1, the coal bed gas 2, the oxygen 3 and the steam 4 using an adjustment apparatus The gasification apparatus 20 comprises a gasifying *reaction portion 21 to progress mainly gasification reaction between the coal 1 therein and the coal bed gas 2 S 10 and an adjusting reaction portion 22 to progress mainly adjusting reaction of the hydrogen/carbon monoxide ratio in the produced mixture gas 5, and is constructed so that the 0 hydrogen/carbon monoxide ratio is adjusted in the gasification apparatus 20 by adjusting the proportions of 15 supplying amounts of the coal 1, the coal bed gas 2, the oxygen 3 and the steam 4 using an adjustment apparatus That is, the pulverized coal 1 and the coal bed gas 2 are supplied to the gasification apparatus 20 from a coal supply system 11 and a coal bed gas supply system 12 as the raw materials, respectively, and are gasified by the oxygen 3 as an oxidation agent supplied from an oxygen supply system 13 to form the mixture gas containing hydrogen and carbon monoxide as the main components. Part of the formed carbon monoxide is converted to hydrogen by the steam 4 supplied from a steam supply system 14 to be sent out as a mixture gas 5 through a gas send-out hole in the upper portion. A zone having a temperature above 1500 OC is formed inside the gasification apparatus 20, and ash of the coal 1 is drained as a molten slag 6 from the bottom portion of the gasification apparatus In a case where the coal bed gas 2 contains a large amount of oxygen as the composition, the caol-bed gas supply system 12 may be constructed in such that the oxygen is reacted with the methane in the coal bed gas 2, and the partially oxidized coal bed gas 2A reduced in oxygen concentration is pressurized and supplied to the oeee 10 gasification apparatus 20. Here, the coal bed gas supply system 12 will be described in detail, referring to FIG. 2 and FIG. 3. The coal bed gas 2 stored in a coal bed gas tank 121 is supplied to an partial oxidation unit 122. In the partial oxidation unit 122, the methane in the coal bed gas 2 is partially oxidized by oxygen. Although the partial oxidation unit 122 used is a reaction unit capable of "attaining a high reaction rate by maintaining a high pressure without using any catalyst, it is possible to employ a reaction unit performing the reaction under a relatively low pressure with using a catalyst. The coal bed gas 2A partially oxidized by the partial oxidation unit 122 is cooled by a heat exchanger 123 and compressed by a compressor 124 to be supplied to the gasification apparatus The partial oxidation unit 122 of the present embodiment is constructed such that a fuel injection nozzle 122b for injecting the coal bed gas is arranged inside a vessel 122a, and the partial oxidation unit 122 is constructed so that the whole unit is heated by a temperature rising apparatus (not shown) burning fuel such as light oil or propane. Therefore, the position near the fuel injection nozzle 122b is maintained at a temperature above the ignition temperature of methane (630 20 It is necessary for safe operation to maintain the position near the fuel injection nozzle 122b above this temperature.
The coal bed gas 2 becomes the partially oxidized coal bed e:ee e 10 gas 2A by passing through the partial oxidation unit 122.
eeo* The gasification apparatus 20 will be described below in detail, referring to FIG. 4 and FIG. 5. FIG. 4 is a view showing the detailed construction of the gasification apparatus of FIG. 1. FIG. 5 is a cross-sectional view 15 showing the adjusting reaction portion of FIG. 4, and FIG.
is a cross-sectional view showing the gasification reaction portion of FIG. 4. Referring to FIG. 4 and FIG. the gasification apparatus 20 is a apparatus having a onechamber two-stage type furnace, and is constructed so that the formed mixture gas 5 flows from one side (the lower side) to the other side (the upper side). As injection portions of the coal 1, the coal bed gas 2, the oxygen 3 and the steam 4 at one position in the lower side and at the other position in the upper side, there are provided lower stage burners 23 arranged in the lower stage and upper stage burners 24 arranged in the upper stage. The coal 1, the coal bed gas 2, the oxygen 3 and the steam 4 17 are supplied to the gasification apparatus 20 through both of the lower stage burners 23 and the upper stage burners 24.
The gasification reaction portion 21, in which gasification reaction of the coal 1 and the coal bed gas 2 is mainly progressed, is formed in the lower stage of the gasification apparatus 20, and the adjusting reaction portion 22, in which adjusting reaction of the hydrogen/carbon monoxide ratio is mainly progressed, is 10 formed in the upper stage. By adjusting the proportions of the coal i, the coal bed gas 2, the oxygen 3 and the steam 4 supplied through the injection portions of the lower stage burners 23 and the upper stage burners 24, the hydrogen/carbon monoxide ratio of the produced hydrogen/carbon monoxide mixture gas 5 is adjusted. The slag (coal ash) 6 melted in the gasification reaction portion 21 is drained outside of the furnace through a slag tap 25. The slag 6 is crushed into small pieces by being rapidly cooled by water filled in a slag quenching zone 26.
FIG. 5 is a view showing an example of the arrangement of the upper stage burners 24. In this embodiment, the coal 1, the oxygen 3 and the steam 4 are supplied from the upper stage burners 24. Particles of the coal 1 of raw material are supplied so as to form a swirl flow having a swirl diameter D1 in order to secure a long staying time in the furnace. Therefore, the upper stage burners 24 are arranged so that the coal, the oxygen and 18 the steam are injected toward the tangential direction of the circumference of the horizontal section of the gasification apparatus 20, as illustrated in FIG. 5. In the embodiment of FIG. 5, the coal 1 and the oxygen 3 are supplied from the upper stage burners 24a, 24b, 24d and 24e, and the steam 4 is supplied from the upper stage burners 24c and 24f.
FIG. 5 is a view showing an example of the arrangement of the lower stage burners 23. In this 10 embodiment, the coal i, the coal bed gas 2, the oxygen 3 and the steam 4 are supplied from the lower stage burners 23. Similar to the raw material supply from the upper stage burners 24, the raw materials are supplied from the lower stage burners 23 so as to form a swirl flow. However, since 15 high temperature flames are formed in the lower stage zone, there is possibility to damage the furnace wall if the swirl diameter is large. Therefore, it is necessary that the swirl diameter D2 is made smaller than that in the upper stage. In the embodiment of FIG. 5, the coal 1 and the oxygen 3 are supplied from the lower stage burners 23a and 23d, and the coal bed gas 2 and the oxygen 3 are supplied from the lower stage burners 23b and 23e, and the steam 4 is supplied from the lower stage burners 23c and 23f.
Here, referring to FIG. 6, description will be made on the adjustment apparatus 30 which adjusts the hydrogen/carbon monoxide ratio in the formed mixture gas 19 by adjusting the ratio of mixing the coal 1 and the coal bed gas 2. FIG. 6 is a diagram showing a control system of the adjustment apparatus 30. A mixture gas composition detector 31 for measuring the hydrogen/carbon monoxide ratio in the formed mixture gas 5 is connected to a pipe from a sent-out hole of the gasification apparatus 20, and a gas chromatography may be used as the composition detector 31. Therein, since a period of measured data becomes 2 to 3 minutes in the shortest period when the gas 10 chromatography is used. Therefore, in order to perform the control further in detail, it may be possible that concentrations of carbon monoxide, carbon dioxide and methane are measured using an infrared absorption instrument which is capable of continuously analyzing, and 15 a hydrogen/carbon monoxide ratio is estimated by inputting the measured concentrations in an analytical model of the e "gasification apparatus In addition to the hydrogen/carbon monoxide ratio, temperature and pressure of the mixture gas 5 formed as described above are detected by a temperature detector 32 for detecting the formed mixture gas temperature and by a pressure detector 33 for detecting the formed mixture gas pressure, respectively, and the detected data is input to a raw material supply controller 34. Further, there are arranged a temperature detector 35 for detecting temperature of the adjusting reaction portion 22 in the upper stage of the gasification apparatus 20 and a temperature detector 36 for detecting temperature of the gasification reaction portion 21 in the lower stage of the gasification apparatus 20, and the data is also input to the raw material supply controller 34.
There are some cases that the temperature of the gasification reaction portion 21 in the lower stage can not be measured because of attaching of the slag to the temperature measurement portion. In such a case, it is preferable to provide the raw material supply controller 34 10 with a predicting estimation model for predicting the temperature of the lower stage gasification reaction portion. The raw material supply controller 34 is for e estimating a state of the gasification apparatus 20 and for calculating an optimum coal bed gas/coal ratio, an optimum oxygen/coal ratio and a steam/coal ratio. Signal lines for controlling a coal supply control valve 37, a coal bed gas supply control valve 38, an oxygen supply control valve 39 and a steam supply control valve 40 are connected to the raw material supply controller 34.
In the embodiment of FIG. 6, the coal supply system 11, the coal bed gas supply system 12, the oxygen supply system 13 and the steam supply system 14 are connected to each of the gasification reaction portion 21 and the adjusting reaction portion 22 of the gasification apparatus 20. However, in the case where the coal bed gas 2 is not supplied to the adjusting reaction portion in the upper stage, the coal supply system 12 in the upper portion is not necessary and accordingly the supply systems may be changed depending on the necessity. Further, the supply systems may be constructed in such that the coal supply system 11, the coal bed gas supply system 12, the oxygen supply system 13 and the steam supply system 14 are provided one for each, and each of the supply systems is branched to the gasification reaction portion 21 in the lower stage and to the adjusting reaction portion 22 in the upper stage.
10 The fuel/electric-power co-production plant shown in FIG. 1 comprises the system of manufacturing hydrogen/carbon-monoxide mixture gas 10, the gas purification apparatus 45, the fuel synthesis apparatus and the electric power generation system 55, as described 15 above, and the mixture gas 5 produced in the system of manufacturing hydrogen/carbon-monoxide mixture gas 10 is supplied to the gas purification apparatus 45. In the gas purification apparatus 45, dust-removing and desulfurization of the mixture gas 5 are performed. A cyclone, a filter or the like may be employed for the dustremoving. Sulfuric chemical compounds contained in the produced mixture gas 5 are hydrogen sulfide and carbonyl sulfide, and as desulfurization methods, there are wet desulfurization methods and dry desulfurization methods. As the wet desulfurization methods there are methods using physical absorption such as the selexsol method, the rectisol method and the like, and there are methods using chemical absorption such as the methyl-di-ethanol-amine method and the like. In the dry desulfurization methods, iron oxide particles are used. As described above, the mixture gas 5 is dust-removed and desulfurized in the gas purification apparatus 45 to become a refined gas 7.
The refined gas 7 is conducted to the fuel synthesis apparatus 50 or the electric power generation system The fuel synthesis apparatus 50 is composed of a fuel synthesis unit 51 and a fuel distillation unit 52, and as 10 synthesized fuels there are methanol, dimethyl ether, an FT synthesized oil and so on. In the fuel synthesis unit 51 in the case of synthesizing methanol as the fuel, a Cu/Zn oooo group catalyst is used, and the reaction conditions are 220 to 300 C and 50 to 100 atmospheric pressures. The 15 synthesizing reactors of the fuel synthesis unit 51 employed are of a quench type, a heat insulation external cooling type, a tube cooling type, a steam generation type, a liquid phase type, a fluid bed type and so on. The fuel distillation unit 52 is for distilling the fuel such as methanol and the like synthesized in the fuel synthesis unit 51.
In the fuel synthesis unit 51 in the case of synthesizing dimethyl ether as the fuel, since the produced dimethyl ether does not require high purity, the synthesized gas is passed through a slurry which is formed by dissolving, for example, a Cu/Zn group catalyst for synthesizing methanol and Y -Al20 3 catalyst for synthesizing dimethyl ether in an organic solvent, and it is possible to use the method that reaction from the refined gas 7 to dimethyl ether can be performed using one reacting vessel.
By constructing as described above, cost of the fuel synthesis apparatus 50 can be reduced.
The FT synthesized oil is hydrocarbons obtained from hydrogen and the carbon monoxide mixture gas through Fischer-Tropsh reaction. The hydrocarbons in the FT synthesized oil are not composed of a single kind of 10 hydrocarbon, but compositions having a certain distribution.
S The reaction conditions are 200 to 300 °C and about atmospheric pressures, and iron, cobalt or ruthenium is ae..
used as the catalyst.
The fuel 8 synthesized by the fuel synthesis 15 apparatus 50 such as methanol, dimethyl ether, the FT synthesized oil are stored in the fuel storage tank 60, and a...supplied to the electric power generation system 55 through the fuel reform apparatus 61. The fuel synthesizing reaction from the hydrogen/carbon monoxide mixture gas in the fuel synthesis apparatus 50 is an equilibrium reaction, and accordingly non-reacted hydrogen and non-reacted carbon monoxide always remain. Part of these non-reacted gases 9 are recycled from the fuel distillation unit 52 to the fuel synthesis unit 51, and the remainder is supplied to the electric generation system 55 so that the system synthesizes fuel and generates electric power at a time.
As the electric power generation system 55, a steam power electric power generating system which generates electric power using a steam turbine by recovering heat at burning the fuel 8 as steam; a gas turbine electric power generating system using a gas turbine; a combined cycle electric power generating system which generates electric power using a gas turbine and a steam turbine; an electric power generating system using a diesel electric power generator and a steam turbine; and a fuel cell system can be used.
10 Description will be made below on the operation of the fuel/electric-power co-production plant comprising the embodiment of the system of manufacturing hydrogen/carbon- OS b monoxide mixture gas constructed as described above.
Pulverized coal 1 from the coal supply system 11 is oo .o 15 supplied to the gasification apparatus 20 through the adjustment apparatus 30, and similarly oxygen 3 from the oxygen supply system 13 is supplied to the gasification b eS apparatus 20 through the adjustment apparatus 30, and steam 4 from the steam supply system 14 is supplied to the gasification apparatus 20 through the adjustment apparatus Further, the coal bed gas 2 from a coal bed gas tank 121 of the coal bed gas supply system 12 is changed to a partial oxidation coal bed gas 2A reduced in containing oxygen by being partially oxidized in the partial oxidation unit 122, and before being compressed, the partial oxidation coal bed gas 2A is cooled by a heat exchanger 123 because its temperature is increased by the partial oxidation, and then the cooled partial oxidation coal bed gas 2A is compressed by a compressor 124 to be supplied to the gasification apparatus The coal bed gas 2 used here is slightly reduced in containing methane and is reduced to nearly zero in oxygen by the partial oxidation reaction, as the composition shown in Table i, and then the coal bed gas 2 is pressurized to about 30 atmospheric pressures to be supplied to the .gasification unit 20. The coal bed gas does not rapidly 10 react even it is pressurized to the high pressure because it contains no oxygen. The coal bed gas 2 shown in Table is only one example, and the composition varies depending on the district of mining.
Table 1 ooooo *e coal bed gas partial oxidation coal bed gas (vol.%) methane 42.6 29.3 nitrogen 47.4 42.4 oxygen 7.9 0.0 carbon dioxide 2.1 7.2 hydrogen 0.0 17.6 carbon monoxide 0.0 As shown in Table 1, for example, the coal bed gas 2 contained methane of about 42.6 vol.% and oxygen of about 7.9 vol.%, but by reacting the coal bed gas at 600 0 C using a catalyst in the partial oxidation unit 122, the exit gas of the partial oxidation coal bed gas 2A contained oxygen nearly zero and the composition of the exit gas was methane of about 29.3 vol.%, carbon monoxide of 3.5 vol.%, hydrogen of about 17.6 vol.%.
Inside the gasification apparatus 20, in the gasification reaction portion 21 at one position in the lower side, the coal 1, the coal bed gas 2, oxygen 3 and steam 4 are supplied from a lower stage burner 23, and the gasification reaction of the above-mentioned chemical 10 formula occurs where the coal is expressed by CH and the gasification reaction of the above-mentioned chemical formula occurs where the coal bed gas is expressed by
CH
4 Because actually the supplied amount of oxygen is slightly more then an amount determined by the S 15 stoichometric ratio in order to maintain the temperature for the reaction, carbon dioxide is also produced. In the gasification reaction portion 21, the temperature needs to be maintained above 1500 °C in order to progress the gasification reaction and to melt the ash component in the coal to drain it from the furnace. The lower stage burners 23 produce a small diameter swirl flow of flame because the flame becomes high temperature so as to not damage the furnace wall.
It can be understood from Chemical Formula that the hydrogen/carbon monoxide ratio of the gas obtained by the gasification of coal is about 0.5, and it can be understood from Chemical Formula that the hydrogen/carbon monoxide ratio of the gas obtained by the gasification of coal bed gas is about 2. Therefore, the hydrogen/carbon monoxide ratio can be adjusted by mixing these gases. As shown by Chemical Formula partial oxidation reaction occurs between the methane in the coal bed gas and oxygen in the gasification reaction portion 21.
On the other hand, in the adjusting reaction portion 22 at the other position in the upper side, the coal 1, oxygen 3 and steam 4 are supplied from an upper stage burner 24, and the shift reaction of the above-mentioned chemical formula occurs to adjust the hydrogen/carbon monoxide ratio. The temperature of this portion needs to be maintained above 1300 °C in order to progress the abovementioned reaction without catalyst. Since the temperature 15 of the upper stage burner 24 is lower than that of the lower stage burner 23, the diameter of the swirl flow of the flame is made larger so that the staying time of the gas may be lengthened.
The mixture gas 5 produced in the gasification apparatus 20 is supplied to the gas purification apparatus from a send-out hole in the upper portion of the gasification apparatus 20. The composition of the mixture gas 5 is detected at a position between the send-out hole and the gas purification apparatus using a mixture gas composition detector 31, and the composition data is input to a raw material supply controller 34 and at the same time detected data signals of temperature detectors 32, 35, 36 and a pressure detector 33 are also input to the raw material supply controller 34. The raw material supply controller 34 estimate the state of the gasification apparatus 20, and calculates optimum coal bed gas/coal ratio, oxygen/coal ratio and steam/coal ratio, and then controls a coal supply control valve 37, a coal bed gas supply control valve 38, an oxygen supply control valve 39 and a steam supply control valve 40 to adjust their opening degrees.
10 By doing as described above, an optimum hydrogen/carbon monoxide ratio for synthesizing a fuel such as methanol, dimethyl ether, the FT synthesis oil or the like can be obtained by making the hydrogen/carbon monoxide ratio of the mixture gas 5 to an optimum state. The mixture 15 gas 5 is dust-removed and desulfurized in the gas purification apparatus 45 to be formed into a refined gas 7.
S. Part of the refined gas 7 is transferred to the fuel synthesis apparatus 50 to be synthesized to the fuel 8, stored in the fuel storage tank 60, reformed to a mixed gas of hydrogen and carbon monoxide in the fuel reform apparatus 61, and then supplied to the electric power generation system 55 depending on necessity. On the other hand, non-reacted gas 9 from the fuel distillation unit 52is returned to the fuel synthesis apparatus 51 or supplied to the electric power generation system 55 to be effectively used. Therein, it is possible that the refined gas 7 is directly supplied to the electric power generation system 55 from the fuel storage tank 60 not through the fuel reform apparatus 61.
The fuel such as methanol, dimethyl ether, the FT synthesis oil or the like is synthesized in the fuel synthesis apparatus 50. Methanol synthesis reaction is an exothermic reaction shown by Chemical Formula and Chemical Formula and the composition suitable for the synthesis is hydrogen/carbon monoxide ratio of 2 (mol/mol).
A Cu/Zn group catalyst is used in the methanol synthesis, and the reaction condition is 220 to 300 OC and 50 to 100 atmospheric pressures.
2 H2 CO CHOH (4) 3 H 2 CO -CH3OH H20 Dimethyl ether can be obtained by dehydration 15 reaction shown by Chemical Formula In the dimethyl ether synthesis process, the methanol synthesis reaction .i shown by Chemical Formula and shift reaction shown by Chemical Formula are also occur, and these reactions can be integrated into a reaction shown by Chemical Formula In this case, the composition suitable for the synthesis is hydrogen/carbon monoxide ratio of 1 (mol/mol).
By the reactions described above, methanol and dimethyl ether are synthesized.
2 CH 3 OH CH 3
OCH
3
H
2 0 (6)
H
2 0 CO H 2
CO
2 (7) 3 H, 3 CO CH 3
OCH
3
CO
2 (8) In the past, in the synthesis of dimethyl ether, two different reactors, a methanol synthesis unit and a dimethyl ether synthesis unit, have been used. However, since dimethyl ether produced in fuel manufacturing is not required to be of high purity, from the viewpoint of cost reduction it is preferable to employ a method of using one reactor for reactions from the synthesis gas to dimethyl ether. For example, there is a method in which the synthesis gas is passed through a slurry solving a Cu/Zn group catalyst for synthesizing methanol and y -Al 2 03 10 catalyst for synthesizing dimethyl ether into an organic solvent.
Another embodiment of a fuel/electric-power coproduction plant comprising a system of manufacturing hydrogen/carbon-monoxide mixture gas in accordance with the present invention will be described below in detail, referring to FIG. 7. FIG. 7 is a block diagram showing another embodiment of a fuel/electric-power co-production plant comprising a system for manufacturing a hydrogen/carbon-monoxide mixture gas in accordance with the present invention. Compared to the above-mentioned embodiment, this embodiment is characterized by that the total amount of the purified gas 7 purified in the gas purification apparatus 45 is supplied to the fuel synthesis apparatus 50. The other constructions essentially equal to those in the above-mentioned embodiment are identified by the same reference characters, and will be omitted to be explained in detail. According to the present embodiment, a large amount of piping can be reduced and the construction can be symplified.
Another embodiment of a gasification apparatus will be described below, referring to FIG. 8. Compared to the above-mentioned embodiment, the gasification apparatus of FIG. 8 characterized in the point that the coal bed gas 2 is supplied only to the adjusting reaction portion 22. That is, in FIG. 8 the coal bed gas 2 is supplied from the burners 64a, 64d in the upper stage. On the other hand, 10 coal 1 and oxygen 3 are supplied from the burners 63b, 63e in the lower stage. the other constructions are essentially equal to those in the above-mentioned embodiment. By constructing as described above, the construction of the burners 23, 24 can be simplified and at the same time the 15 piping can be also simplified.
S: Another embodiment of a coal bed gas supply system will be described below, referring to FIG. 9. FIG. 9 is a block diagram showing another embodiment of the coal bed gas supply system. In the coal bed gas supply system 72, Initially the collected coal bed gas 2 is supplied to the partial oxidation unit 721. In the partial oxidation unit 721, methane in the coal bed gas 2 is partially oxidized by oxygen. Although the partial oxidation unit 721 used is a reaction unit capable of attaining a high reaction rate by maintaining a high pressure without using any catalyst, it is possible to employ a reaction unit performing the reaction under a relatively low pressure with using a catalyst. The partially oxidized coal bed gas 2A is cooled by a heat exchanger 722 and compressed by a compressor 124 and stored in the coal bed gas tank 723. The partially oxidized coal bed gas 2A is compressed by the compressor 724 to be supplied to the gasification apparatus depending on necessity.
Another embodiment of a partial oxidation unit will be described below, referring to FIG. 10. FIG. 10 is a cross-sectional view showing another embodiment of the partial oxidation unit. In the vessel 721a of the partial oxidation unit 721, a fuel injection nozzle 721b for injecting the coal bed gas is arranged in the upstream side, and a combustion catalyst 721c is arranged in the downstream side. According to this partial oxidation unit 15 721, the reaction between methane and oxygen can be progressed at a temperature lower than that in the case without catalyst. As the catalyst platinum or the like is used, and by using the catalyst, methane initiates to be burned at a temperature of 370 to 380 °C and can be completely burned at a temperature of 400 to 450 °C.
Although the example of using coal as the carbon group fuel has been described above, of course it is possible that the system can be constructed so as to use the other carbon group fuel such as heavy mass oil. It is possible to cope with that case by modifying the burners of the injection portions to the gasification apparatus.
Throughout this specification and the claims which follow, unless the context requires otherwise, the word "comprise", and variations such as "comprises" and "comprising", will be understood to imply the inclusion of a stated integer or step or group of integers or steps but not the exclusion of any other integer or step or group of integers or steps.
The reference to any prior art in this specification is not, and should not be taken as, an acknowledgment or any form of suggestion that that prior art forms part of the common general knowledge in Australia.
S..oo.
S. o o
DOS.
S
Claims (4)
- 2. A method of manufacturing hydrogen/carbon-monoxide mixture gas according to claim i, the method further comprising the steps of: supplying said carbon group fuel and said coal bed 15 gas and an oxidation agent into an upstream zone of a gasification apparatus to partially oxidize said carbon group fuel and said coal bed gas, gas flowing in one direction in said gasification apparatus; and making shift reaction of the carbon monoxide formed by said partial oxidation by supplying steam into a downstream zone of said gasification apparatus.
- 3. A method of manufacturing hydrogen/carbon-monoxide mixture gas from a carbon group fuel and a coal bed gas containing methane as a main component, the method comprising the steps of: partially oxidizing said carbon group fuel in two zones of an upstream zone and a downstream zone of a gasification apparatus, gas flowing in one direction in said gasification apparatus; partially oxidizing said coal bed gas, and burning part of said carbon group fuel in said upper zone; and making shift reaction of said formed carbon monoxide in said downstream zone to increase a hydrogen ratio of said hydrogen/carbon-monoxide mixture gas.
- 4. A method of manufacturing hydrogen/carbon-monoxide mixture gas according to any one of claim 2 and claim 3,
- 99.9 10 wherein steam for preventing temperature rise of a furnace wall of said gasification apparatus is supplied to said upper zone of said gasification apparatus. A method of manufacturing hydrogen/carbon-monoxide i mixture gas according to any one of claim 2 and claim 3, 15 wherein the gasification reaction in each of said upstream zone and said downstream zone is performed by forming a swirl flow of supplied raw materials, and a magnitude of the swirl flow in said downstream zone is larger than a magnitude of the swirl flow in said upstream zone. 6. A method of manufacturing hydrogen/carbon-monoxide mixture gas from raw materials of a carbon group fuel and a coal bed gas containing methane as a main component using a gasification apparatus of a pressurized gas type, the method comprising the steps of: partially oxidizing said coal bed gas to reduce an amount of oxygen contained in said coal bed gas in prior to supplying said coal bed gas to said gasification apparatus; 36 after that partially oxidizing said coal bed gas and said carbon group fuel by supplying said coal bed gas reduced in the amount of oxygen and said carbon group fuel and an oxidation agent to said gasification apparatus; and making shift reaction of part of the carbon monoxide formed by said partial oxidation by supplying steam into a downstream zone of said gasification apparatus. 7. A system of manufacturing hydrogen/carbon-monoxide 10 mixture gas from raw materials of a carbon group fuel and a coal bed gas containing methane as a main component using a gasification apparatus, which comprises: said gasification apparatus in which gas flows in one direction; a supply system for supplying said carbon group fuel and said coal bed gas and an oxidation agent to an upstream *zone of said gasification apparatus so that said carbon group fuel and said coal bed gas are partially oxidized in said upstream zone; and a supply system for supplying steam to a downstream zone of said gasification apparatus so that part of said carbon monoxide formed in said upstream zone is shifted to hydrogen in said downstream zone. 8. A system of manufacturing hydrogen/carbon-monoxide mixture gas from raw materials of a carbon group fuel and a coal bed gas containing methane as a main component using a gasification apparatus, which comprises: said gasification apparatus in which gas flows in one direction; a supply system for supplying said carbon group fuel and said coal bed gas and an oxidation agent to an upstream zone of said gasification apparatus so that said carbon group fuel is partially oxidized and burned, and said coal bed gas is partially oxidized in said upstream zone; and a supply system for supplying said carbon group fuel and the oxidation agent and steam to a downstream zone of 10 said gasification apparatus so that said carbon group fuel is partially oxidized and shift reaction of part of said acarbon monoxide formed by partial oxidation of said carbon oeoo group fuel and said coal bed gas in said downstream zone. 9. A system of manufacturing hydrogen/carbon-monoxide ooo 15 mixture gas according to any one of claim 7 and claim 8, which comprises a system for supplying steam to said a.. upstream zone of said gasification apparatus. A system of manufacturing hydrogen/carbon-monoxide mixture gas according to any one of claim 7 and claim 8, which comprises a raw material supply system and an oxidation agent supply system and a steam supply system so that swirl flows of the raw material, the oxidation agent and steam are formed in both of said upstream zone and said downstream zone of said gasification apparatus, and a magnitude of the swirl flow in said downstream zone is larger than a magnitude of the swirl flow in said upstream zone. 38 11. A system of manufacturing hydrogen/carbon-monoxide mixture gas from raw materials of a carbon group fuel and a coal bed gas containing methane as a main component using a gasification apparatus of a pressurized gas type, which comprises: said gasification apparatus in which gas flows in one direction; a supply system for supplying said carbon group fuel and said coal bed gas and an oxidation agent to an upstream 10 zone of said gasification apparatus so that said carbon group fuel and said coal bed gas are partially oxidized in said upstream zone; a supply system for supplying steam to a downstream zone of said gasification apparatus so that shift reaction 15 of part of said carbon monoxide formed by partial oxidation of said carbon group fuel and said coal bed gas in said downstream zone; and a partial oxidation unit for partially oxidizing said coal bed gas with oxygen contained in said coal bed gas before supplying said coal bed gas to said upstream zone to reduce an amount of oxygen contained in said coal bed gas. 12. A system of manufacturing hydrogen/carbon-monoxide mixture gas from raw materials of a carbon group fuel and a coal bed gas containing methane as a main component using a gasification apparatus of a pressurized gas type, which comprises: said gasification apparatus in which gas flows in one direction; a supply system for supplying said carbon group fuel and said coal bed gas and an oxidation agent to an upstream zone of said gasification apparatus so that said carbon group fuel is partially oxidized and burned, and said coal bed gas is partially oxidized in said upstream zone; a supply system for supplying said carbon group fuel and the oxidation agent and steam to a downstream zone of said gasification apparatus so that shift reaction of part 10 of said carbon monoxide formed by partial oxidation of said carbon group fuel and said coal bed gas in said downstream zone; and a partial oxidation unit for partially oxidizing said coal bed gas with oxygen contained in said coal bed gas 15 before supplying said coal bed gas to said upstream zone to reduce an amount of oxygen contained in said coal bed gas. o 13. A fuel/electric-power co-production plant comprising: the system of manufacturing hydrogen/carbon-monoxide mixture gas according to any one of claims 7, 8, 11 and 12; a gas purification apparatus for purifying a hydrogen/carbon-monoxide mixture gas manufacture by said system of manufacturing hydrogen/carbon-monoxide mixture gas; a fuel synthesis apparatus for synthesizing any one of methanol, dimethyl ether and an FT synthesized oil from said hydrogen/carbon-monoxide mixture gas purified by said gas purification apparatus; and an electric power generation system for generating electric power using said fuel synthesized by said fuel synthesis apparatus as a power source. 14. A fuel/electric-power co-production plant comprising: the system of manufacturing hydrogen/carbon-monoxide mixture gas according to any one of claims 7, 8, 11 and 12; a gas purification apparatus for purifying a hydrogen/carbon-monoxide mixture gas manufacture by said system of manufacturing hydrogen/carbon-monoxide mixture 10 gas; a fuel synthesis apparatus for synthesizing any one of methanol, dimethyl ether and an FT synthesized oil from said hydrogen/carbon-monoxide mixture gas purified by said gas purification apparatus; and 15 an electric power generation system for generating electric power using said fuel synthesized by said fuel synthesis apparatus and not-reacted gases as a power source. A method of manufacturing hydrogen/carbon-monoxide mixture gas substantially as hereinbefore described with reference to the drawings and/or Examples. 16. A system for manufacturing hydrogen/carbon-monoxide gas substantially as hereinbefore described with reference to the drawings and/or Examples. 17. A fuel/electric-power co-production plant substantially as hereinbefore described with reference to the drawings and/or Examples. DATED this 5 th Day of November 2001 Hitachi, Ltd. AND Babcock-Hitachi Kabushiki Kaisha by DAVIES COLLISON CAVE Patent Attorneys for the applicant(s)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11-313756 | 1999-11-04 | ||
| JP31375699A JP2001139303A (en) | 1999-11-04 | 1999-11-04 | Method and device for producing hydrogen/carbon monoxide mixed gas, and fuel/power combination plant provided with the device |
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| Publication Number | Publication Date |
|---|---|
| AU6969600A AU6969600A (en) | 2001-05-17 |
| AU742742B2 true AU742742B2 (en) | 2002-01-10 |
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| Application Number | Title | Priority Date | Filing Date |
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| AU69696/00A Ceased AU742742B2 (en) | 1999-11-04 | 2000-11-02 | Method of manufacturing hydrogen/carbon-monoxide mixture gas, system thereof, and fuel/electric-power co-production plant |
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| Country | Link |
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| JP (1) | JP2001139303A (en) |
| CN (1) | CN1155683C (en) |
| AU (1) | AU742742B2 (en) |
| ID (1) | ID29057A (en) |
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| US20050144961A1 (en) * | 2003-12-24 | 2005-07-07 | General Electric Company | System and method for cogeneration of hydrogen and electricity |
| US7722690B2 (en) * | 2006-09-29 | 2010-05-25 | Kellogg Brown & Root Llc | Methods for producing synthesis gas |
| JP5389335B2 (en) * | 2007-03-22 | 2014-01-15 | 電源開発株式会社 | Gasifier |
| CN100582201C (en) * | 2007-06-22 | 2010-01-20 | 清华大学 | Combined system and process for producing electricity-substituted natural gas based on coal gasification and methanation |
| JP2009104884A (en) * | 2007-10-23 | 2009-05-14 | Showa Shell Sekiyu Kk | Solid oxide fuel cell system |
| AU2009218694B2 (en) * | 2008-02-28 | 2014-02-13 | Krones Ag | Method and device for converting carbonaceous raw materials |
| JP2009302010A (en) * | 2008-06-17 | 2009-12-24 | Showa Shell Sekiyu Kk | Fuel cell cogeneration system |
| JP5527743B2 (en) * | 2008-08-22 | 2014-06-25 | マイクロ・エナジー ホールディングス リミテッド | Gasification apparatus, fuel generation system, gasification method, and fuel generation method |
| AU2010246510B2 (en) * | 2009-12-01 | 2013-01-24 | Electric Power Development Co. Ltd. | Gasifier, thermal power plant using gasifier, operating procedure of gasifier, and operating procedure of thermal power plant using gasifier |
| JP2013253003A (en) * | 2012-06-08 | 2013-12-19 | Sumitomo Seika Chem Co Ltd | Method and apparatus for producing hydrogen |
| JP2012251169A (en) * | 2012-09-24 | 2012-12-20 | Electric Power Dev Co Ltd | Gasification furnace |
| WO2016158918A1 (en) * | 2015-03-30 | 2016-10-06 | 株式会社クボタ | Gasification furnace, method of operating gasification furnace and biomass gasification treatment method |
| JP6454583B2 (en) * | 2015-03-30 | 2019-01-16 | 株式会社クボタ | Gasification furnace and operation method of gasification furnace |
| JP6454582B2 (en) * | 2015-03-30 | 2019-01-16 | 株式会社クボタ | Gasification furnace, gasification furnace operating method, and biomass gasification processing method |
| JP6637797B2 (en) * | 2016-03-11 | 2020-01-29 | 三菱日立パワーシステムズ株式会社 | Carbon-containing raw material gasification system and method for setting oxidizing agent distribution ratio |
| JP6951140B2 (en) * | 2017-07-19 | 2021-10-20 | 日本特殊陶業株式会社 | Reforming method, reforming equipment and reforming structure |
| KR102086651B1 (en) * | 2018-07-09 | 2020-04-23 | 한국에너지기술연구원 | System of distributed energy production plant using cal |
| KR102086652B1 (en) * | 2018-07-09 | 2020-03-10 | 한국에너지기술연구원 | System of distributed energy production plant using cal |
| KR102200407B1 (en) * | 2019-05-20 | 2021-01-08 | 두산중공업 주식회사 | A system for guiding the operation of a coal gasification plant and a method therefor |
| CN110923010A (en) * | 2019-12-10 | 2020-03-27 | 中国科学院工程热物理研究所 | Coal staged gasification method and device based on chemical looping combustion |
| CN112831352B (en) * | 2021-01-09 | 2021-09-07 | 中国华能集团清洁能源技术研究院有限公司 | Efficient gasification furnace and working method thereof |
| CN114181741B (en) * | 2021-11-19 | 2022-09-20 | 新奥科技发展有限公司 | Coal hydro-gasification device |
| AU2022256206B2 (en) * | 2021-12-10 | 2024-02-22 | Ekona Power Inc. | Methods and systems for mixing fluids |
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| AU8559782A (en) * | 1981-07-20 | 1983-01-27 | Zimpro-Aec Ltd. | Production of synthesis gas |
| DE3902773A1 (en) * | 1989-01-31 | 1990-08-02 | Basf Ag | METHOD FOR PRODUCING SYNTHESIS GAS BY PARTIAL OXIDATION |
| EP0522744A2 (en) * | 1991-07-09 | 1993-01-13 | Imperial Chemical Industries Plc | Synthesis gas production |
-
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- 1999-11-04 JP JP31375699A patent/JP2001139303A/en active Pending
-
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- 2000-11-02 AU AU69696/00A patent/AU742742B2/en not_active Ceased
- 2000-11-03 CN CNB001366297A patent/CN1155683C/en not_active Expired - Fee Related
- 2000-11-06 ID IDP20000952A patent/ID29057A/en unknown
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|---|---|---|---|---|
| AU8559782A (en) * | 1981-07-20 | 1983-01-27 | Zimpro-Aec Ltd. | Production of synthesis gas |
| DE3902773A1 (en) * | 1989-01-31 | 1990-08-02 | Basf Ag | METHOD FOR PRODUCING SYNTHESIS GAS BY PARTIAL OXIDATION |
| EP0522744A2 (en) * | 1991-07-09 | 1993-01-13 | Imperial Chemical Industries Plc | Synthesis gas production |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2001139303A (en) | 2001-05-22 |
| ID29057A (en) | 2001-07-26 |
| AU6969600A (en) | 2001-05-17 |
| CN1298926A (en) | 2001-06-13 |
| CN1155683C (en) | 2004-06-30 |
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