CN1298926A - Process and system for prodn. of hydrogen/carbon mono oxide mixture, and fuel/electric power combination installation - Google Patents
Process and system for prodn. of hydrogen/carbon mono oxide mixture, and fuel/electric power combination installation Download PDFInfo
- Publication number
- CN1298926A CN1298926A CN 00136629 CN00136629A CN1298926A CN 1298926 A CN1298926 A CN 1298926A CN 00136629 CN00136629 CN 00136629 CN 00136629 A CN00136629 A CN 00136629A CN 1298926 A CN1298926 A CN 1298926A
- Authority
- CN
- China
- Prior art keywords
- coal bed
- hydrogen
- gas
- bed gas
- carbon monoxide
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
Landscapes
- Industrial Gases (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
本发明的目的是提供一种通过使煤和煤床气在高压条件下反应生产氢气和一氧化碳混合气的方法和生产氢气与一氧化碳混合气的系统及包括有生产氢气的混合气的系统的燃料/电力联合装置。本发明的特征是:通过将煤床气和煤供应给气化设备以将它们部分氧化来生产有高氢气比的氢气/一氧化碳混合气,在气化设备中用水蒸气使部分形成的一氧化碳发生转移反应。The object of the present invention is to provide a kind of method and the system of producing hydrogen and carbon monoxide mixed gas by making coal and coal bed gas react under high pressure condition to produce hydrogen and carbon monoxide mixed gas and comprise the fuel/fuel of the system of the mixed gas of producing hydrogen Power combination. The present invention is characterized in that a hydrogen/carbon monoxide mixture with a high hydrogen ratio is produced by supplying coal bed gas and coal to a gasification plant to partially oxidize them, where part of the formed carbon monoxide is diverted by water vapor reaction.
Description
The present invention relates to amethod for producing a hydrogen/carbon monoxide mixed gas by gasifying a carbon-based fuel such as coal, heavy oil and coal bed gas with oxygen, steam or the like, a system for producing a hydrogen and carbon monoxide mixed gas, and a combined apparatus for producing a fuel and generating electricity including the system for producing a hydrogen/carbon monoxide mixed gas.
In coal mining in a coal field, coal bed gas containing methane as a main component is produced. The main purpose of collecting the coal bed gas is to ensure the safety of the coal mining activity, and although a part of the collected coal bed gas is used as fuel, most of the collected coal bed gas is disposed of as waste without being utilized. Therefore, from the viewpoint of energy saving, the coal bed gas is to be effectively used. In addition, in a framework protocol concerning climate change, it is calculated: methane has 21 times the greenhouse effect of carbon dioxide, and therefore it is also important to effectively utilize coal bed gas from the viewpoint of preventing global warming.
In conventional technology using coal bed gas containing methane as a main component, japanese patent application laid-open No. 9-67582 discloses a method of producing a hydrogen/carbon monoxide mixed gas by feeding coal and methane into a gasification furnace using coal and methane as raw materials. In the conventional art, coal and methane as raw materials are pressurized to be supplied to a gasification furnace operating at about 30 atmospheres. In addition, in order to increase the ratio of hydrogen to carbon monoxide, a steam reforming reaction of methane is performed in the gasifier. The hydrogen-carbon monoxide mixed gas obtained as described above can be used in a power generation system by a gas turbine or a fuel cell, can be used in a fuel production system for producing a fuel such as methanol, methyl ether,FT synthesis oil, or can be used in a combined fuel/power plant for simultaneously producing a fuel and generating power.
Although the above method can efficiently obtain high purity methane, it is difficult to pressurize methane because the coal bed gas collected as one of mining activities contains air (oxygen) and it is also difficult to reach a certain high temperature for the steam reforming reaction because the gas temperature approaches 600 ℃ already when the coal bed gas is pressurized to 30 atmospheres by a compressor, and on the other hand, the ignition temperature of methane is 630 ± 20 ℃, so that the methane and oxygen contained in the coal bed gas may rapidly react.
In addition, nitrogen in air is reactive inert, and it is difficult to maintain a high temperature when air is mixed into the coal bed gas because heat energy is required to raise the temperature of nitrogen. The temperature approaches 330 c when the coal bed gas is pressurized to 10 atmospheres, so methane and oxygen do not react rapidly at this pressure. However, the size of the gasification furnace at 10 atm is 3 times that of the gasification furnace at 30 atm, which causes a problem of cost increase.
The present invention has been made to solve the above-mentioned problems, and it is an object of the present invention to provide a method and system capable of producing a hydrogen/carbon monoxide mixed gas having a high hydrogen ratio from coal and coal bed gas without performing a steam reforming reaction. In addition, it is another object of the present invention to provide a fuel/electric power combined plant including a system for synthesizing a fuel from a hydrogen/carbon monoxide mixture and an electric power generation system for generating electric power from the synthesized fuel.
In order to achieve the aboveobject, a method for producing a hydrogen/carbon monoxide mixture gas according to the present invention is characterized in that the method comprises the steps of: forming hydrogen and carbon monoxide by partially oxidizing the carbon-based fuel and the coal bed gas; in order to increase the hydrogen ratio of the hydrogen/carbon monoxide mixture, part of the carbon monoxide is reacted with steam to form hydrogen.
The partial oxidation of carbon based fuels and coal bed gas is carried out by supplying the feedstock and oxidant to a gasification plant furnace. The shift reaction of carbon monoxide is carried out by supplying steam to the gasification furnace to contact carbon monoxide. Thus, the gasification apparatus is preferably constructed such that the gas flows in one direction, the carbon-based fuel and coal bed gas and the oxidant are supplied to an upstream region of the gasification apparatus, and the water vapor is supplied to a downstream region.
In addition, the method for producing a hydrogen/carbon monoxide mixture according to the present invention is characterized in that the method comprises the steps of: partially oxidizing a carbon-based fuel in two regions, an upstream region and a downstream region of a gasification device, in which a gas flows in one direction; partially oxidizing the coal bed gas and combusting a portion of the carbon-based fuel in an upstream zone; the formed carbon monoxide is subjected to a shift reaction in a downstream zone to increase the ratio of hydrogen in the hydrogen/carbon monoxide mixture. By combusting a portion of the carbon-based fuel in an upstream region of the gasification facility, the furnace temperature in the upstream region is increased, and thus, ash formed in connection with gasification of the carbon-based fuel melts to prevent the ash from binding to the furnace walls.
When the method for producing a hydrogen/carbon monoxide mixed gas of the present invention is carried out by a gasification apparatus of a pressurized gas type, it is preferable to partially oxidize a coal bed gas with oxygen contained in the coal bed gas to remove oxygen in the coal bed gas or to reduce the oxygen content in the coal bed gas before supplying the coal bed gas to the gasification apparatus. In the case where the coal bed gas is mined from a coal field, when it is pressurized and supplied to a gasification apparatus of a pressurized gas type, the temperature of the coal bed gas rises when pressurized, and therefore there is a risk of ignition of the coal bed gas. Therefore, it is possible to prevent such a problem from occurring by removing oxygen from the coal bed gas in advance.
According to the method for producing a hydrogen/carbon monoxide mixture of the invention, the chemistry of the carbon-based fuel takes placeA partial oxidation reaction of reaction formula (1) and a partial oxidation reaction of chemical reaction formula (2) of the coal bed gas. A carbon monoxide shift reaction represented by the chemical reaction formula (3) also occurs. The symbol CH in chemical reaction formula (1) represents coal, and the symbol CH in chemical reaction formula (2)4Representing methane in the coal bed gas.
In the case of carrying out the method for producing a hydrogen/carbon monoxide mixed gas of the present invention with a gasification apparatus in which a gas flows in one direction, a method for partially oxidizing a coal bed gas only in an upstream zone or a method for partially oxidizing a coal bed gas in both an upstream zone and a downstream zone is included in an embodiment of the present invention.
From the chemical reactionformula (1), it can be known that: the ratio of hydrogen to carbon monoxide in the gas obtained by coal gasification is about 0.5, as can be seen from the chemical reaction formula (2): the hydrogen/carbon monoxide ratio of the gas obtained by gasifying coal bed gas is about 2. Thus, mixing these gases can adjust the hydrogen/carbon monoxide ratio.
In addition, the hydrogen/carbon monoxide ratio can be further increased by the shift reaction of chemical reaction formula (3).
When the method for producing a hydrogen/carbon monoxide mixed gas of the present invention is carried out by a gasification apparatus of a pressurized gas type, it is preferable to partially oxidize a coal bed gas with oxygen contained in the coal bed gas before supplying the coal bed gas to the gasification apparatus to remove oxygen from the coal bed gas. In this case, the bed gas flows out of the bed gas holder of the bed gas supply system, and its oxygen concentration is reduced by partial oxidation in the partial oxidation apparatus, and the bed gas is cooled by a heat exchanger before being pressurized because the temperature of the bed gas is increased by the partial oxidation reaction. The oxygen concentration in the coal bed gas by the partial oxidation reaction is almost zero, and therefore, the coal bed gas does not react with oxygen rapidly even when the coal bed gas is compressed to a high pressure. Therefore, the coal bed gas can be pressurized to about 30 atmospheres and then supplied to the gasification facility.
The oxygen content of the coal bed gas is insufficient to completely combust methane, and the oxygen is consumed in performing the partial oxidation reaction of the chemical reaction formula (2). In order to improve the reaction of methane and oxygen at a stage before the coal bed gas is supplied to the gasification apparatus, it is preferable to raise the reaction temperature of the partial oxidation reaction of methane with oxygen in the coal bed gas to more than 1000 ℃. Therefore, a catalytic combustion reaction is preferably used.
By removing or reducing oxygen in the coal bed gas before supplying the coal bed gas to the gasification apparatus, the coal bed gas does not react with oxygen rapidly even if the coal and the coal bed gas react with each other under high pressure, and the hydrogen/carbon monoxide mixed gas can be produced efficiently, and the size of the system can be made small. In addition, a mixture having an optimum hydrogen/carbon monoxide ratio corresponding to the synthetic fuel can be produced. In addition, it is possible to effectively utilize the coal bed gas that has been wasted for the purpose of energy saving and to contribute to prevention of global warming.
The present invention is characterized in that a system for producing a hydrogen/carbon monoxide mixed gas using a gasification apparatus with a carbon-based fuel and a coal bed gas containing methane as a main component as raw materials, the system comprising: a gasification device in which gas flows in one direction; a supply system for supplying a carbon-based fuel and a coal bed gas and an oxidant to an upstream region of a gasification facility to partially oxidize the carbon-based fuel and the coal bed gas in the upstream region; a supply system for supplying steam to the downstream region of the gasification plant to shift part of the carbon monoxide formed in the upstream region into hydrogen in the downstream region.
The invention features a system for producing a hydrogen/carbon monoxide mixture. It includes: a gasification device in which gas flows in one direction; a supply system for supplying a carbon-based fuel and a coal bed gas and an oxidant to an upstream region of the gasification facility to partially oxidize and combust the carbon-based fuel in the upstream region and partially oxidize the coal bed gas in the upstream region; a supply system for supplying a carbon-based fuel and an oxidant and steam to a downstream region of a gasification device to partially oxidize the carbon-based fuel in the downstream region and to effect a shift reaction of carbon monoxide formed in part by the partial oxidation of the carbon-based fuel and the coal bed gas.
In addition, the invention features a system for producing a hydrogen/carbon monoxide mixture, comprising: a gasification device in which gas flows in one direction; a supply system for supplying a carbon-based fuel and a coal bed gas and an oxidant to an upstream region of a gasification facility to partially oxidize the carbon-based fuel and the coal bed gas in the upstream region; a supply system for supplying steam to a downstream region of the gasification facility to shift react a portion of the carbon monoxide formed from the partial oxidation of the carbon-based fuel and the coal bed gas in the downstream region; a partial oxidation device for partially oxidizing the coal bed gas with oxygen contained in the coal bed gas before supplying the coal bed gas to the upstream region to reduce the oxygen content in the coal bed gas.
The invention features a combined fuel/power plant, including: the system for producing the hydrogen/carbon monoxide mixed gas; a gas purification apparatus for purifying a hydrogen/carbon monoxide mixed gas produced by the system for producing a hydrogen/carbon monoxide mixed gas; a fuel synthesis device for synthesizing any one of methanol, dimethyl ether and FT synthetic oil from the hydrogen/carbon monoxide mixed gas purified by the gas purification device; the fuel synthesized by the fuel synthesis equipment is used as an energy source to generate electricity.
Additionally, the invention features acombined fuel/power plant including: the system for producing the hydrogen/carbon monoxide mixed gas; a gas purification apparatus for purifying a hydrogen/carbon monoxide mixed gas produced by the system for producing a hydrogen/carbon monoxide mixed gas; a fuel synthesis device for synthesizing any one of methanol, dimethyl ether and FT synthetic oil from the hydrogen/carbon monoxide mixed gas purified by the gas purification device; a power generation system for generating power by using a fuel synthesized by a fuel synthesis apparatus and an unreacted gas as an energy source. As described above, according to the method for producing a hydrogen/carbon monoxide mixed gas and the system for producing a hydrogen/carbon monoxide mixed gas of the present invention, a mixed gas having a hydrogen/carbon monoxide ratio suitable for fuels such as methanol, dimethyl ether, FT synthesis oil, and the like can be efficiently produced.
In addition, since the coal bed gas is supplied to the gasification apparatus after the oxygen content in the coal bed gas is reduced by partial oxidation, the coal bed gas can be compressed to a high pressure, and accordingly, the size of the system can be reduced, thereby reducing the cost.
Further, the fuel/electric power combined plant including the system for producing a hydrogen/carbon monoxide mixture gas according to the present invention can achieve energy saving by effectively utilizing the coal bed gas, and can also effectively prevent global warming.
FIG. 1 is a block diagram illustrating one embodiment of a combined fuel/power plant including a system for producing a hydrogen/carbon monoxide mixture according to the present invention.
FIG. 2 is a block diagram illustrating the coal bed gas supply system of FIG. 1.
Fig. 3 is a cross-sectional view illustrating a partial oxidation apparatus of fig. 2.
Fig. 4 is a view showing a detailed structure of the gasification apparatus of fig. 1.
Fig. 5(a) is a cross-sectional view illustrating the conditioning reaction part of fig. 4, and fig. 5(b) is a cross-sectional view illustrating the gasification reaction part of fig. 4.
Fig. 6 is a schematic diagram illustrating a control system of the adjusting apparatus of fig. 1.
FIG. 7 is a block diagram illustrating another embodiment of a combined fuel/power plant including a system for producing a hydrogen/carbon monoxide mixture according to the present invention.
Fig. 8 shows another embodiment of the gasification apparatus, fig. 8(a) is a cross-sectional view showing a conditioning reaction part, and fig. 8(b) is a cross-sectional view showing a gasification reaction part.
FIG. 9 is a block diagram illustrating another embodiment of a coal bed gas supply system.
Fig. 10 is a cross-sectional view showing another embodiment of a partial oxidation apparatus.
In the following detailed description of an embodiment of a fuel/electric power plant including a system for producing a hydrogen/carbon monoxide mixture according to the present invention, with reference to the accompanying drawings, fig. 1 is a block diagram showing an embodiment of a fuel/electric power plant including a system for producing a hydrogen/carbon monoxide mixture according to the present invention. In fig. 1, a system 10 for producing a hydrogen/carbon monoxide mixture is a system for producing a hydrogen/carbon monoxide mixture by gasifying coal 1 and coal bed gas 2 of a carbon-based fuel with oxygen 3 and by causing a shift reaction of the produced carbon monoxide with steam 4. The system 10 for producing a hydrogen/carbon monoxide mixed gas is constructed such that coal 1 and coal bed gas 2 are supplied to a gasification apparatus 20, gas is produced in the gasification apparatus 20 by performing a gasification reaction of the coal 1 and the coal bed gas 2, and a ratio of hydrogen/carbon monoxide is adjusted by adjusting a ratio of supply amounts of the coal 1, the coal bed gas 2, oxygen 3 and steam 4 with an adjusting apparatus 30.
The gasification apparatus 20 includes a gasification reaction section 21 in which a gasification reaction between coal 1 and a coal bed gas 2 is mainly performed and an adjustment reaction section 22 in which an adjustment reaction of a hydrogen/carbon monoxide ratio in a produced mixed gas 5 is mainly performed, and is structured to adjust the hydrogen/carbon monoxide ratio in the gasification apparatus 20 by adjusting the ratio of the supply amounts of coal 1, the coal bed gas 2, oxygen 3 and steam 4 with an adjustment apparatus 30.
That is, pulverized coal 1 and coal bed gas 2 are supplied as raw materials from a coal supply system 11 and a coal bed gas supply system 12, respectively, to a gasification facility 20, and are gasified by oxygen 3 supplied from an oxygen supply system 13 as an oxidant to form a mixed gas containing hydrogen and carbon monoxide as main components. Part of the formed carbon monoxide is converted into hydrogen by the steam 4 supplied from the steam supply system 14 and discharged as a mixed gas 5 through a gas discharge hole at the top. Inside the gasification plant 20 a zone is formed with a temperature above 1500 ℃, and the ash of the coal 1 is discharged from the bottom of the gasification plant 20 as slag 6.
In the case where the coal bed gas 2 contains a large amount of oxygen as its component, the coal bed gas supply system 12 may be configured to react the oxygen with methane in the coal bed gas 2, and the partially oxidized coal bed gas 2A having a reduced oxygen concentration is supplied under pressure to the gasification apparatus 20. The coal bed gas supply system 12 will be described in detail herein, and referring to fig. 2 and 3, the coal bed gas 2 stored in the coal bed gas holder 121 is supplied to the partial oxidation device 122. In the partial oxidation unit 122, methane in the coal bed gas 2 is partially oxidized by oxygen. Although the partial oxidation apparatus 122 used is a reaction apparatus capable of achieving a high reaction rate by maintaining a high pressure without using any catalyst, a reaction apparatus capable of performing a reaction at a relatively low pressure using a catalyst may be used. The coal bed gas 2A partially oxidized by the partial oxidation device 122 is cooled by the heat exchanger 123, compressed by the compressor 124, and supplied to the gasification facility 20.
The partial oxidation apparatus 122 of this embodiment has a structure in which a fuel nozzle 122b for injecting coal bed gas is disposed inside a container 122a, and the partial oxidation apparatus 122 has a structure in which the entire apparatus is heated by burning fuel such as light oil or propane by a temperature increasing means (not shown). Therefore, the temperature at a location near the fuel nozzle 122b is kept higher than the ignition temperature of methane (630 ± 20 ℃). Maintaining a temperature above that at a location proximate to the fuel nozzle 122b is necessary for safe operation. The coal bed gas 2 flows through the partial oxidation device 122 to become a partially oxidized coal bed gas 2A.
The gasification apparatus 20 will be described in detail with reference to fig. 4 and 5, and fig. 4 is a view showing a detailed structure of the gasification apparatus of fig. 1. Fig. 5(a) is a cross-sectional view illustrating the conditioning reaction part of fig. 4, and fig. 5(b) is a cross-sectional view illustrating the gasification reaction part of fig. 4. Referring to fig. 4 and 5, the gasification apparatus 20 is an apparatus of a one-chamber two-stage type furnace, and is constructed such that the formed mixed gas 5 flows from one side (bottom) to the other side (top). Since the injection portions of the coal 1, the coal bed gas 2, the oxygen 3 and the steam 4 are located at one position of the lower portion and another position of the upper portion, a lower stage burner 23 is disposed at the lower stage and an upper stage burner 24 is disposed at the upper stage. Coal 1, coal bed gas 2, oxygen 3 and steam 4 are supplied to the gasification facility 20 through a lower stage burner 23 and an upper stage burner 24.
A gasification reaction section 21 in which gasification reaction of the coal 1 and the coal bed gas 2 is mainly performed is formed in a lower section of the gasification apparatus 20, and an adjustment reaction section 22 in which adjustment reaction of the hydrogen/carbon monoxide ratio is mainly performed is formed in an upper section. By adjusting the ratio of coal 1, coal bed gas 2, oxygen 3 and steam 4 supplied through the injection portions of the lower stage burner 23 and the upper stage burner 24, the hydrogen/carbon monoxide ratio of the produced hydrogen/carbon monoxide mixed gas 5 can be adjusted. The slag (coal ash) 6 melted in the gasification reaction section 21 is discharged outside the furnace through the slag outlet 25. The slag 6 is quenched with water filled in the slag quenching zone 26 to be crushed into small pieces.
Fig. 5(a) is a view showing an example of the arrangement of the upper stage combustor 24. In this embodiment, coal 1, oxygen 3 and steam 4 are supplied from the upper stage burner 24. The coal 1 particles as the raw material are supplied to form a vortex having a diameter D1 in order to ensure a long residence time in the furnace. Thus, the upper stage burners 24are arranged such that coal, oxygen and steam are injected tangentially to the horizontal circumference of the gasification apparatus 20, as shown in FIG. 5. In the embodiment of fig. 5, the upper stage burners 24a,24b,24d and 24e supply coal 1 and oxygen 3, and the upper stage burners 24c and 24f supply steam 4.
Fig. 5(b) is a view showing an example of the arrangement of the lower burner 23. In this embodiment, the lower stage burner 23 supplies coal 1, coal bed gas 2, oxygen 3 and steam 4. The lower burner 23 supplies the raw material to form a vortex, similarly to the upper burner 24. However, since a high-temperature flame is formed in the lower stage region, the furnace wall may be damaged if the diameter of the vortex is large. Therefore, it is necessary to make the vortex diameter D2 smaller than that of the upper section. In the embodiment of fig. 5, the lower burners 23a and 23d supply coal 1 and oxygen 3, the lower burners 23b and 23e supply coal bed gas 2 and oxygen 3, and the lower burners 23c and 23f supply steam 4.
Now, referring to fig. 6, an adjusting device 30 that adjusts the hydrogen/carbon monoxide ratio in the formed mixed gas 5 by adjusting the mixing ratio of coal 1 and coal bed gas 2 will be described. Fig. 6 is a schematic diagram showing a control system of the adjusting apparatus 30. A mixture composition detector 31 for measuring the hydrogen/carbon monoxide ratio in the formed mixture 5 is connected to a pipe extending from the discharge hole of the gasification apparatus 20, and a gas chromatograph may be used as the detector 31. In this case, since the shortest measurement time is 2 to 3 minutes when using the gas chromatograph, it is possible to measure the concentrations of carbon monoxide, carbon dioxide and methane using an infrared absorption device capable of continuous analysis for more precise control, and the ratio of hydrogen to carbon monoxide can be estimated by inputting the measured concentrations to the analysis module of the gasification apparatus 20.
The temperature and pressure of the formed mixed gas 5 are detected by a temperature detector 32 for detecting the temperature of the formed mixed gas and a pressure detector 33 for detecting the pressure of the formed mixed gas, respectively, in addition to the hydrogen/carbon monoxide ratio, and the detected data are inputted to a raw material supply controller 34. In addition, a temperature detector 35 is provided to detect the temperature of the conditioning reaction section 22 in the upper stage of the gasification apparatus 20, and a temperature detector 36 is provided to detect the temperature of the gasification reaction section 21 in the lower stage of the gasification apparatus 20, and these data are also inputted to the raw material supply controller 34.
There are many cases where the temperature of the gasification reaction section 21 in the lower stage cannot be measured, because the slag adheres to the temperature test section. In this case, it is preferable to provide a prediction module for predicting the temperature of the lower gasification reaction section on the raw material supply controller 34. The function of the feed supply controller 34 is to determine the status of the gasification plant 20 and calculate the optimal coal bed gas/coal ratio, the optimal oxygen/coal ratio and the steam/coal ratio. Signal lines controlling the coal supply control valve 37, the coal bed gas supply control valve 38, the oxygen supply control valve 39, and the 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 the gasification reaction section 21 and the conditioning reaction section 22 of the gasification facility 20. However, in the case where the reaction portion is adjusted without supplying the coal bed gas 2 into the upper stage, the upper coal supply system 12 is not necessary, and accordingly the supply system may be changed as needed. In addition, the supply systems may be configured 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 each only one, and each supply system is branched into the gasification reaction section 21 of the lower stage and the conditioning reaction section 22 of the upper stage.
As described above, the combined fuel/electric power plant shown in fig. 1 includes: the system for producing a hydrogen/carbon monoxide mixture gas 10, the gas purification apparatus 45, the fuel synthesis apparatus 50 and the power generation system 55, and the mixture gas 5 produced by the system for producing a hydrogen/carbon monoxide mixture gas 10 is supplied to the gas purification apparatus 45. In the gas purification apparatus 45, the mixed gas 5 is subjected to dust removal and desulfurization. Cyclone separators, filters, etc. may be used to remove dust. The sulfur compounds contained in the produced mixed gas 5 are hydrogen sulfide and carbonyl sulfide, and the desulfurization method includes wet desulfurization and dry desulfurization. In wet desulfurization, there are methods using physical absorption such as the selexsol method and the recitisol method, and also methods using chemical absorption such as the methyldiethanolamine method. In dry desulfurization, iron oxide particles are used. As described above, the mixed gas 5 is subjected to dust removal and desulfurization in the gas purification apparatus 45 to become the refined gas 7.
The refined gas 7 is directed to a fuel synthesis plant 50 or a power generation system 55. The fuel synthesizing facility 50 is composed of a fuel synthesizing apparatus 51 and a fuel distilling apparatus52, and methanol, dimethyl ether, FT synthesis oil, and the like are used as synthetic fuels. In the fuel synthesizing apparatus 51, if methanol is synthesized as a fuel, a Cu/Zn group catalyst is used, and reaction conditions are: 220 ℃ to 300 ℃ and 50 to 100 atmospheres. The synthesis reactor in the fuel synthesis apparatus 51 is of a quench type, an adiabatic external cooling type, a tubular cooling type, a steam generation type (steam generation type), a liquid phase type, a fluidized bed type, or the like. The fuel distillation apparatus 52 functions to distill the fuel such as methanol synthesized in the fuel synthesis apparatus 51.
In the fuel synthesizing apparatus 51, if dimethyl ether is synthesized as a fuel, since dimethyl ether produced does not require high purity, the synthesis gas is passed through a catalyst such as Cu/Zn group catalyst for methanol synthesis and γ -Al for dimethyl ether synthesis2O3The catalyst is dissolved in the organic solvent to form a slurry, and a method of reacting the refining gas 7 to produce dimethyl ether using one reaction vessel can be used. When constructed as described above, the cost of the fuel synthesizing apparatus 50 can be reduced.
The FT synthetic oil is hydrocarbon obtained by the Fischer-Tropsch reaction of a mixed gas of hydrogen and carbon monoxide. The hydrocarbons in the FT synthesis oil are not constituted by one kind of hydrocarbon but have a certain distribution of composition. The reaction conditions are as follows: at 200-300 deg.C and about 30 atm, and Fe, Co or Ru as catalyst.
The fuel 8 synthesized by the fuel synthesizing apparatus 50, such as methanol, dimethyl ether and FT synthesis oil, is stored in a fuel storage tank 60 and supplied to the power generating system 55 through a fuel reforming apparatus 61. The fuel synthesis reaction of the hydrogen/carbon monoxide mixture in the fuel synthesis apparatus 50 is anequilibrium reaction, so there is always unreacted hydrogen and unreacted carbon monoxide. Part of these unreacted gases 9 are recycled from the fuel distillation unit 52 to the fuel synthesis unit 51, and the rest is supplied to the power generation system 55, so that the system synthesizes fuel and generates power at the same time.
As the power generation system 55, there can be used: a steam power generation system for recovering heat of the combustion fuel 8 as steam by a steam turbine to generate power; a gas turbine power generation system using a gas turbine; a combined cycle power generation system for generating power using a gas turbine and a steam turbine; a power generation system using a diesel generator and a steam turbine, and a fuel cell system.
The operation of the combined fuel/electric power plant including one embodiment of the system for producing a hydrogen/carbon monoxide mixture constructed as described above will be described below. Pulverized coal 1 is supplied from coal supply system 11 to gasification facility 20 through regulation facility 30, and likewise, oxygen 3 is supplied from oxygen supply system 13 to gasification facility 20 through regulation facility 30, and steam 4 is supplied from steam supply system 14 to gasification facility 20 through regulation facility 30. In addition, the coal bed gas 2 discharged from the coal bed gas holder 121 of the coal bed gas supply system 12 is changed into the partially oxidized coal bed gas 2A having a reduced oxygen content by partial oxidation in the partial oxidation device 122, and since the temperature of the partially oxidized coal bed gas 2A is raised by the partial oxidation reaction, it is cooled by passing through a heat exchanger 123 before compression, and then the cooled partially oxidized coal bed gas 2A is compressed by a compressor 124 and supplied to the gasification apparatus 20.
The coal bed gas 2used herein is a gas having a methane content slightly reduced by a partial oxidation reaction and an oxygen content reduced to almost zero, and its composition is shown in table 1, and then the coal bed gas 2 is pressurized to about 30 atmospheres and supplied to the gasification apparatus 20. This coal bed gas, even if compressed to high pressure, does not react rapidly because it does not contain oxygen. The coal bed gas 2 shown in table 1 is only an example, and its composition varies from one mine site to another.
TABLE 1
| Coal bed gas (vol.%) | Partial oxidation of coal bed gas (vol.％) | |
| Methane | 42.6 | 29.3 |
| Nitrogen gas | 47.4 | 42.4 |
| Oxygen gas | 7.9 | 0.0 |
| Carbon dioxide | 2.1 | 7.2 |
| Hydrogen gas | 0.0 | 17.6 |
| Carbon monoxide | 0.0 | 3.5 |
As shown in table 1, for example, the methane content in the coal bed gas 2 is about 42.6 vol.%, and the oxygen content is about 7.9 vol.%, but, after the coal bed gas is reacted at 600 ℃ by using a catalyst in the partial oxidation unit 122, the discharged gas, that is, the oxygen content in the partially oxidized coal bed gas 2A, is almost zero, and the discharged gas composition is: methane about 29.3 vol%, carbon monoxide about 3.5 vol%, hydrogen about 17.6 vol%.
In the gasification facility 20, coal 1, coal bed gas 2, oxygen 3 and steam 4, in which coal is represented by CH and gasification reaction of the above chemical reaction formula (2) occurs, are supplied from a lower stage burner 23 at a position of a lower gasification reaction section 21, and gasification reaction of the above chemical reaction formula (1) in which coal bed gas is represented by CH occurs4And (4) showing. Since the amount of oxygen actually supplied is slightly larger than the amount determined by the stoichiometric ratio in order to maintain the reaction temperature, carbon dioxide is also generated. In the gasification reaction section 21, the temperature is maintained at more than 1500 ℃ in order to perform the gasification reaction and to melt ash in the coal for discharge to the outside of the furnace. The lower burner 23 generates a flame vortex of small diameter because the flame temperature is high so that the furnace wall is not damaged.
From the chemical reaction formula (1), it can be known that: the ratio of hydrogen to carbon monoxide in the gas obtained by coal gasification is about 0.5, as can be seen from the chemical reaction formula (2): the hydrogen/carbon monoxide ratio of the gas obtained by gasifying coal bed gas is about 2. Thus, mixing these gases can adjust the hydrogen/carbon monoxide ratio. As shown in chemical reaction formula (2), in the gasification reaction section 21, a partial oxidation reaction occurs between methane and oxygen in the coal bed gas.
On the other hand, at another position of the upper regulation reaction section 22, coal 1, oxygen 3 and steam 4 are supplied from the upper stage burner 24, and the shift reaction of the above chemical reaction formula (3) occurs to regulate the hydrogen/carbon monoxide ratio. In order to carry out the above reaction without using a catalyst, the temperature in this zone is maintained above 1300 ℃. Since the temperature of the upper stage burner 24 is lower than that of the lower stage burner 23, the diameter of the flame vortex is made larger, so that the residence time of the gas can be extended.
The mixed gas 5 produced in the gasification apparatus 20 is discharged from the discharge hole at the top of the gasification apparatus 20 and supplied to the gas purification apparatus 45. The composition of the mixed gas 5 is detected by the mixed gas composition detector 31 at a position between the discharge port and the gas purification apparatus, and data of the composition is inputted to the raw material supply controller 34, and at the same time, data signals detected by the temperature detectors 32,35,36 and the pressure detector 33 are inputted to the raw material supply controller 34. The raw material supply controller 34 estimates the state of the gasification apparatus 20, calculates an optimum bed gas/coal ratio, oxygen/coal ratio and steam/coal ratio, and then controls the coal supply control valve 37, the bed gas supply control valve 38, the oxygen supply control valve 39 and the steam supply control valve 40 to adjust the degree of opening thereof.
By these operations as described above, an optimum hydrogen/carbon monoxide ratio for use in synthesizing fuels such as methanol, dimethyl ether, FT synthesis oil, and the like can be obtained by setting the hydrogen/carbon monoxide ratio of the mixed gas 5 to an optimum state. The mixed gas 5 is subjected to dust removal and desulfurization in the gas purification apparatus 45 to become the refined gas 7. The partially refined gas 7 is transferred to the fuel synthesis apparatus 50 to synthesize fuel 8, stored in the fuel storage tank 60, reformed into a mixed gas of hydrogen and carbon monoxide in the fuel reforming apparatus 61, and then supplied to the power generation system 55 as required. On the other hand, the unreacted gas 9 discharged from the fuel distillation apparatus 52 is returned to the fuel synthesis apparatus 51 or supplied to the power generation system 55 for effective use. In this case, the refined gas 7 can be directly supplied from the fuel storage tank 60 to the power generation system 55 without passing through the fuel reforming device 61.
Fuels such as methanol, dimethyl ether, FT synthesis oil, and the like are synthesized in the fuel synthesizing apparatus 50. The methanol synthesis reaction is an exothermic reaction represented by chemical reaction formula (4) and chemical reaction formula (5), and a composition suitable for synthesis is such that the ratio of hydrogen/carbon monoxide is 2 (mol/mol). In methanol synthesis using a Cu/Zn family catalyst, the reaction conditions are: 220 ℃ to 300 ℃ and 50 to 100 atmospheres.
Dimethyl ether can be produced by dehydration reaction represented by the chemical reaction formula (6). In the dimethyl ether synthesis reaction, a methanol synthesis reaction shown in chemical reaction formula (4) and a shift reaction shown in chemical reaction formula (7) also occur, and these reactions can be combined into one reaction shown in chemical reaction formula (8). In this case, the composition suitable for synthesis is such that the hydrogen/carbon monoxide ratio is 1 (mol/mol). Methanol and dimethyl ether can be synthesized by the above reaction.
In the past, dimethyl ether was synthesized using two different reactors, one methanol synthesis apparatus and one dimethyl ether synthesis apparatus. However, since dimethyl ether produced in fuel production does not require high purity, it is preferable to use a method of reacting synthesis gas to produce dimethyl ether with one reactor from the viewpoint of cost reduction. For example, there is a method of passing a synthesis gas stream over a Cu/Zn group catalyst to be used for methanol synthesis and gamma-Al for dimethyl ether synthesis2O3The catalyst is dissolved in an organic solvent to form a slurry.
Referring now to fig. 7, another embodiment of a fuel/power combination including a system for producing a hydrogen/carbon monoxide mixture according to the present invention will be described in detail. FIG. 7 is a block diagram illustrating another embodiment of a combined fuel/power plant including a system for producing a hydrogen/carbon monoxide mixture according to the present invention. In contrast to the above-described embodiment, this embodiment is characterized in that the refined gas 7 purified in the gas purification apparatus 45 is entirely supplied to the fuel synthesis apparatus 50. Other structures substantially the same as those in the above-described embodiment are denoted by the same symbols and will not be described in detail. According to the present invention, a large number of pipes can be reduced and the structure can be simplified.
Referring now to FIG. 8, another embodiment of a gasification plant is described. In contrast to the above-described embodiment, the gasification apparatus of fig. 8 is characterized in that the coal bed gas 2 is supplied only to the adjustment reaction section 22. That is, in fig. 8(a), the upper stage burners 64a,64d supply the coal bed gas 2. On the other hand, the lower stage burners 63b,63e supply coal 1 and oxygen 3. The other structures are substantially the same as those of the above-described embodiment. When constructed as described above, the structure of the burners 23,24 can be simplified, and the piping can be simplified.
Referring now to FIG. 9, another embodiment of a coal bed gas supply system is described. FIG. 9 is a block diagram illustrating another embodiment of a coal bed gas supply system. In the coal bed gas supply system 72, the collected coal bed gas 2 is initially supplied to the partial oxidation device 721. In the partial oxidation unit 721, methane in the coal bed gas 2 is partially oxidized by oxygen. Although the partial oxidation apparatus 721 is a reaction apparatus capable of achieving a high reaction rate by maintaining a high pressure without using any catalyst, a reaction apparatus capable of performing a reaction at a relatively low pressure using a catalyst may be used. The partially oxidized coal bed gas 2A is cooled by the heat exchanger 722 and compressed by the compressor 124 before being stored in the coal bed gas holder 723. The partially oxidized coal bed gas 2A is compressed by a compressor 724 and then supplied to the gasification facility 20 as needed.
Referring now to FIG. 10, another embodiment of a partial oxidation unit is described. Fig. 10 is a cross-sectional view showing another embodiment of a partial oxidation apparatus. In the tank 721a of the partial oxidation device 721, a fuel injection nozzle 721b that injects the bed gas is disposed at the upstream end, and a combustion catalyst 721c is disposed at the downstream end. According to such a partial oxidation unit 721, the reaction between methane and oxygen may be performed at a temperature lower than that in the absence of the catalyst. The temperature at which methane starts to burn is 370 to 380 ℃ and can be completely burned at a temperature of 400 to 450 ℃ due to the use of a catalyst such as platinum and by the use of the catalyst.
Although coal is described above as an example of a carbon-based fuel, it is naturally possible to construct the system to use other carbon-based fuels such as heavy oil. This can be handled by changing the burner of the injection section to a gasification plant.
Claims (14)
1. A method for producing a hydrogen/carbon monoxide mixture from a carbon-based 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-based fuel and said coal bed gas; and
reacting a portion of said carbon monoxide with steam to form hydrogen to increase the hydrogen ratio of said hydrogen/carbon monoxide mixture.
2. A method of producing a hydrogen/carbon monoxide mixture according to claim 1, further comprising the steps of:
supplying said carbon-based fuel and said coal bed gas and oxidant to an upstream region of a gasification unit wherein said carbon-based fuel and said coal bed gas are partially oxidized and gas flows in one direction; and
the carbon monoxide formed by said partial oxidation is subjected to a shift reaction by supplying steam to a downstream region of said gasification apparatus.
3. A method for producing a hydrogen/carbon monoxide mixture from a carbon-based fuel and a coal bed gas containing methane as a main component, the method comprising the steps of:
partially oxidizing said carbon-based fuel in two regions, an upstream region and a downstream region of a gasification apparatus in which the gas flows in one direction;
combusting a portion of said carbon-based fuel in said upstream region and partially oxidizing said coal bed gas; and
in said downstream region, said formed carbon monoxide is subjected to a shift reaction to increase the hydrogen ratio of said hydrogen/carbon monoxide mixture.
4. A method for producing ahydrogen/carbon monoxide mixture gas as defined in any one of claims 2 and 3, wherein water vapor for preventing an increase in the temperature of the furnace wall of said gasification facility is supplied to the upper region of said gasification facility.
5. A process for producing a hydrogen/carbon monoxide gas mixture according to any one of claims 2 and 3, wherein the gasification reaction in each of the upstream and downstream regions is carried out by forming a swirl of the supplied raw material, the swirl of the downstream region having a magnitude larger than that of the upstream region.
6. A method for producing a hydrogen/carbon monoxide mixed gas from a carbon-based fuel and a coal bed gas containing methane as a main component as raw materials by using a gasification apparatus of a pressurized gas type, comprising the steps of:
supplying said coal bed gas to a front portion of said gasification facility to partially oxidize said coal bed gas to reduce the oxygen content of said coal bed gas; then the
Partially oxidizing said coal bed gas and said carbon based fuel by supplying said reduced oxygen content coal bed gas and said carbon based fuel and oxidant to said gasification facility; and
a portion of the carbon monoxide formed by said partial oxidation is subjected to a shift reaction by supplying steam to a downstream region of said gasification apparatus.
7. A system for producing a hydrogen/carbon monoxide mixture gas using a gasification facility as a feedstock from a carbon-based fuel and a coal bed gas containing methane as a main component, comprising:
said gasification apparatus in which gasflows in one direction;
a supply system for supplying said carbon-based fuel and said coal bed gas and oxidant to an upstream region of said gasification facility for partial oxidation of said carbon-based fuel and said coal bed gas in said upstream region; and
a supply system for supplying steam to a downstream region of said gasification unit to cause a portion of said carbon monoxide formed in said upstream region to be transferred to hydrogen in said downstream region.
8. A system for producing a hydrogen/carbon monoxide mixture gas using a gasification facility as a feedstock from a carbon-based fuel and a coal bed gas containing methane as a main component, comprising:
a gasification device in which gas flows in one direction;
a supply system for supplying said carbon-based fuel and said coal bed gas and oxidant to an upstream region of said gasification facility for partially oxidizing and combusting said carbon-based fuel in said upstream region and for partially oxidizing said coal bed gas in said upstream region; and
a supply system for supplying said carbon-based fuel and oxidant and steam to a downstream region of said gasification facility for partially oxidizing said carbon-based fuel in said downstream region and for effecting a shift reaction of carbon monoxide formed in part by the partial oxidation of said carbon-based fuel and said coal bed gas.
9. A system for producing a hydrogen/carbon monoxide mixture as defined in any one of claims 7 and 8 including a system for supplying steam to said upstream region of said gasification facility.
10. A system for producing a hydrogen/carbon monoxide gas mixture according to any one of claims 7 and 8, wherein a raw material supply system and an oxidant supply system and a steam supply system are included so as to form a swirl of the raw material, the oxidant and the steam in both of an upstream region and a downstream region of said gasification apparatus, a magnitude of the swirl in said downstream region being larger than a magnitude of the swirl in said upstream region.
11. A system for producing a hydrogen/carbon monoxide mixed gas using a gasification apparatus of a pressurized gas type as a raw material, which uses a carbon-based fuel and a coal bed gas containing methane as a main component, comprising: said gasification apparatus in which gas flows in one direction;
a supply system for supplying said carbon-based fuel and said coal bed gas and oxidant to an upstream region of said gasification facility for partial oxidation of said carbon-based fuel and said coal bed gas in said upstream region;
a supply system for supplying steam to a downstream region of said gasification facility to shift react in said downstream region a portion of said carbon monoxide formed by partial oxidation of said carbon-based fuel and said coal bed gas; and
a partial oxidation unit for partially oxidizing said coal bed gas with oxygen contained in said coal bed gas to reduce the oxygen content of said coal bed gas before supplying said coal bed gas to said upstream region.
12. A system for producing a hydrogen/carbon monoxide mixed gas using a gasification apparatus of a pressurized gas type as a raw material, which uses a carbon-based fuel and a coal bed gas containing methane as a main component, comprising: said gasification apparatus in which gas flows in one direction;
a supply system for supplying said carbon-based fuel and said coal bed gas and oxidant to an upstream region of said gasification facility such that said carbon-based fuel is partially oxidized and combusted in said upstream region, said coal bed gas being partially oxidized in said upstream region;
a supply system for supplying said carbon-based fuel and oxidant and steam to a downstream region of said gasification unit for shift reaction of a portion of said carbon monoxide formed by partial oxidation of said carbon-based fuel and said coal bed gas in a downstream region; and
a partial oxidation unit for partially oxidizing said coal bed gas with oxygen contained in said coal bed gas to reduce the oxygen content of said coal bed gas before supplying said coal bed gas to said upstream region.
13. A combined fuel/power plant, comprising:
a system for producing a hydrogen/carbon monoxide mixture according to any one of claims 7,8,11 and 12;
a gas purification means for purifying the hydrogen/carbon monoxide mixture produced by said system for producing a hydrogen/carbon monoxide mixture;
a fuel synthesizing means for synthesizing any one of methanol, dimethyl ether and FT synthetic oil from said hydrogen/carbon monoxide mixed gas purified by said gas purifying means; and
a power generation system for generating power by using said fuel synthesized by said fuel synthesizing apparatus as an energy source.
14. A combined fuel/power plant, comprising:
a system for producing a hydrogen/carbon monoxide mixture according to any one of claims 7,8,11 and 12;
a gas purification means for purifying the hydrogen/carbon monoxide mixture produced by said system for producing a hydrogen/carbon monoxide mixture;
a fuel synthesizing means for synthesizing any one of methanol, dimethyl ether and FT synthetic oil from said hydrogen/carbon monoxide mixed gas purified by said gas purifying means; and
a power generation system for generating power by using said fuel synthesized by said fuel synthesizing apparatus and unreacted gas as energy.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP31375699A JP2001139303A (en) | 1999-11-04 | 1999-11-04 | Method and apparatus for producing hydrogen / carbon monoxide mixed gas |
| JP313756/1999 | 1999-11-04 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1298926A true CN1298926A (en) | 2001-06-13 |
| CN1155683C CN1155683C (en) | 2004-06-30 |
Family
ID=18045167
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB001366297A Expired - Fee Related CN1155683C (en) | 1999-11-04 | 2000-11-03 | Process and system for prodn. of hydrogen/carbon mono oxide mixture, and fuel/electric power combination installation |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JP2001139303A (en) |
| CN (1) | CN1155683C (en) |
| AU (1) | AU742742B2 (en) |
| ID (1) | ID29057A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100582201C (en) * | 2007-06-22 | 2010-01-20 | 清华大学 | Electricity-alternative natural gas cogeneration system and process based on coal gasification and methanation |
| CN108779403A (en) * | 2016-03-11 | 2018-11-09 | 三菱日立电力系统株式会社 | Carbon raw material gasification system and its Oxidizer distribution proportion setting method |
| 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 |
| CN111961499A (en) * | 2019-05-20 | 2020-11-20 | 斗山重工业建设有限公司 | Operation guidance system of coal gasification plant and device and method for same |
Families Citing this family (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
| CN102186954A (en) * | 2008-08-22 | 2011-09-14 | 株式会社微细能源 | Gasification device, 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 |
| 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 |
| JP6454583B2 (en) * | 2015-03-30 | 2019-01-16 | 株式会社クボタ | Gasification furnace and operation method of gasification furnace |
| 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 |
| 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 | A high-efficiency gasifier and its working method |
| 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 |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| ATE156778T1 (en) * | 1991-07-09 | 1997-08-15 | Ici Plc | SYNTHESIS GAS GENERATION |
-
1999
- 1999-11-04 JP JP31375699A patent/JP2001139303A/en active Pending
-
2000
- 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
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100582201C (en) * | 2007-06-22 | 2010-01-20 | 清华大学 | Electricity-alternative natural gas cogeneration system and process based on coal gasification and methanation |
| CN108779403A (en) * | 2016-03-11 | 2018-11-09 | 三菱日立电力系统株式会社 | Carbon raw material gasification system and its Oxidizer distribution proportion setting method |
| CN108779403B (en) * | 2016-03-11 | 2021-02-19 | 三菱动力株式会社 | Carbon-containing raw material gasification system and oxidant distribution ratio setting method thereof |
| CN111961499A (en) * | 2019-05-20 | 2020-11-20 | 斗山重工业建设有限公司 | Operation guidance system of coal gasification plant and device and method for same |
| CN111961499B (en) * | 2019-05-20 | 2022-01-14 | 斗山重工业建设有限公司 | Operation guidance system of coal gasification plant and device and method for same |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1155683C (en) | 2004-06-30 |
| ID29057A (en) | 2001-07-26 |
| AU6969600A (en) | 2001-05-17 |
| AU742742B2 (en) | 2002-01-10 |
| JP2001139303A (en) | 2001-05-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1298926A (en) | Process and system for prodn. of hydrogen/carbon mono oxide mixture, and fuel/electric power combination installation | |
| EP2883940B1 (en) | Method and device for biomass gasification by cycling of carbon dioxide without oxygen | |
| US9206360B2 (en) | Producing liquid fuel from organic material such as biomass and waste residues | |
| US5900224A (en) | Method for treating wastes by gasification | |
| EP1606370B1 (en) | Method for producing synthesis gas | |
| Klinghoffer et al. | Gasification and pyrolysis of municipal solid waste (MSW) | |
| ES2618420T3 (en) | Production of synthesis gas by heating oxidized biomass with a hot gas obtained from oxidation of residual products | |
| US20080098654A1 (en) | Synthetic fuel production methods and apparatuses | |
| JP2014111768A (en) | Methods for producing synthesis gas | |
| CA2610806A1 (en) | A system for the conversion of carbonaceous feedstocks to a gas of a specified composition | |
| SE1051371A1 (en) | Two stage carburetors using high temperature preheated steam | |
| US20150005399A1 (en) | Method and device for producing synthetic gas and method and device for synthesizing liquid fuel | |
| US6902711B1 (en) | Apparatus for treating wastes by gasification | |
| CN1137249C (en) | Method and device for treating waste by gasification | |
| JPH0967582A (en) | Method and apparatus for producing hydrogen / carbon monoxide mixed gas | |
| CN101511724A (en) | Methods for producing synthesis gas | |
| CN100447221C (en) | Gasification method and gasification system | |
| JP2003171675A (en) | Liquid fuel synthesis system | |
| JP3904161B2 (en) | Method and apparatus for producing hydrogen / carbon monoxide mixed gas | |
| JPH05523B2 (en) | ||
| KR102860915B1 (en) | Hydrogen Production and High Quality Gas Production System using combustible renewable fuels Pyrolysis Gasification and Steam-plasma Gasification Reform | |
| JP7192901B2 (en) | Blast Furnace Operation Method and Blast Furnace Incidental Equipment | |
| JP3997524B2 (en) | Gasification method and gas conversion apparatus for organic waste | |
| JPH10132234A (en) | Gas turbine combined cycle method | |
| US20140191162A1 (en) | Method and apparatus for biomass gasification |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |