WO2011007493A1 - 水素製造方法及び水素製造システム - Google Patents
水素製造方法及び水素製造システム Download PDFInfo
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- WO2011007493A1 WO2011007493A1 PCT/JP2010/003657 JP2010003657W WO2011007493A1 WO 2011007493 A1 WO2011007493 A1 WO 2011007493A1 JP 2010003657 W JP2010003657 W JP 2010003657W WO 2011007493 A1 WO2011007493 A1 WO 2011007493A1
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Definitions
- the present invention relates to a method for producing high-purity hydrogen gas from low-quality fuel such as low-grade coal and biomass.
- the present invention also relates to a hydrogen gas production system that produces high-purity hydrogen gas from coal or low-grade coal and uses liquefied hydrogen at a place other than the coal or low-grade coal production area.
- Patent Document 1 discloses a technique for selectively extracting hydrogen gas by introducing a gas containing carbon dioxide and water vapor after a water gas addition reaction to the deep sea, dissolving the carbon dioxide in seawater.
- Patent Document 2 discloses that in a method for producing hydrogen by catalytic gasification reaction of ashless coal, ashless coal derived from lignite or subbituminous coal is used as the ashless coal, and the gasification temperature is 600 to 650 ° C. And a hydrogen production method using potassium carbonate as a catalyst is disclosed.
- Patent Document 3 discloses a method for producing hydrogen from biomass, wherein (i) a first step of gasifying biomass to produce a mixed gas containing hydrocarbons, hydrogen, and carbon monoxide; ) A second step for purifying the gas mixture obtained in the first step, (iii) a third step for converting hydrocarbons contained in the gas mixture obtained in the second step into hydrogen and carbon monoxide, and ( iv) A method comprising a fourth step of recovering hydrogen from the gas mixture obtained in the third step is disclosed.
- a ruthenium-based catalyst such as Ru / Al 2 O 3 is used and contacted with the mixed gas at 60 to 210 ° C. to selectively convert the carbon monoxide into carbon dioxide.
- oxidizing There is also a technique for oxidizing (Patent Document 4).
- anthracite and bituminous coal with advanced coalization are also called high-grade coal
- sub-bituminous coal, lignite, and peat without advanced coalization are also called low-grade coal.
- Low-grade coal has a low degree of coalification and is considered to be low-grade coal with a lot of moisture and oxygen, and it often exceeds the capacity of the pulverizer / dryer as fuel for pulverized coal boilers, Since the calorific value per weight is low, the transportation cost is high, and if it is dehydrated, it is considered to be an unwieldy coal that is likely to catch fire spontaneously. For this reason, low-grade coal is difficult to transport despite having abundant reserves, so it is limited to power generation around the mine.
- porous coal is mixed with a mixed oil containing heavy oil and solvent oil to make a raw slurry, and the calorific value of low-grade coal is reduced by impregnating the mixed oil into the pores of the porous coal and dehydrating it.
- Patent Document 5 A technique for increasing the transportation efficiency and increasing the transportation efficiency is disclosed in Patent Document 5.
- dimethyl ether which is easier to transport, is synthesized and transported from coal seam gas (methane-containing gas) and natural gas produced from the coal seam, and hydrogen gas is produced by decomposing dimethyl ether at the transport destination, and carbon dioxide is recovered.
- Patent Document 6 discloses a technique in which liquefied carbon dioxide gas is transported to a dimethyl ether production site (coal production site) and injected into a coal bed for disposal.
- CCS Carbon dioxide capture
- CCS carbon dioxide storage
- Patent Document 1 The method of introducing carbon dioxide to the deep sea disclosed in Patent Document 1 can produce hydrogen gas without releasing carbon dioxide from coal into the atmosphere. There is a problem that hydrogen production is limited to the coastal area in order to take out hydrogen gas by press-fitting a gas containing gas into a pressure vessel installed in the deep sea. For this reason, it is difficult to produce hydrogen using coal etc. which exists especially in an inland part from a viewpoint of economical efficiency. This marine isolation is now prohibited by the London Convention 1996 Protocol and the Marine Pollution Control Act.
- the method for modifying porous coal disclosed in Patent Document 5 can exhibit the effect of increasing the transport efficiency of porous coal and increasing the calorific value of the porous coal. Still contains carbon, and it is necessary to separate and recover carbon dioxide in the area where the modified porous coal is consumed. For this reason, the use of the modified porous coal is limited to large thermal power plants equipped with CCS facilities.
- Patent Document 6 also separates and recovers carbon dioxide generated when hydrogen is produced by decomposing dimethyl ether, and produces dimethyl ether and coal from liquefied carbon dioxide gas. Need to be transported to.
- the composition of the generated mixed gas is 37.5% hydrogen (H 2 ), 19% carbon monoxide (CO), carbon dioxide (CO 2 ) 16.6%, steam (H 2 O) 25.3%, methane (CH 4 ) 1.6% in general.
- the carbon monoxide concentration can be reduced by the above-described water gas addition reaction (shift reaction), but 8.9% of carbon monoxide remains.
- Patent Document 3 discloses a carbon monoxide shift reactor (reactor for causing a shift reaction) as means for converting carbon monoxide to carbon dioxide and hydrogen. The problem of remaining carbon cannot be solved.
- the pressure swing method (PSA method) or membrane separation method can be used, but in order to continuously separate hydrogen gas from a large amount of mixed gas, durability and maintenance are required. It is disadvantageous in terms of cost. Therefore, it is conceivable to use a cryogenic separation method with a small separation power, but the boiling points at normal pressure are H 2 : -254 ° C, CO: -190 ° C, and the sublimation point of CO 2 at normal pressure is -78.5. ° C. For this reason, it is easy to separate hydrogen gas and carbon dioxide, but it is not easy to separate hydrogen gas and carbon monoxide because their boiling points are close in consideration of the partial pressure of both gases.
- an alkali absorption method having a small separation power When separating hydrogen continuously from a large amount of mixed gas, an alkali absorption method having a small separation power may be used.
- the alkali absorption method is a method of recovering carbon dioxide by absorbing it in an alkaline absorption liquid.
- the absorption liquid is regenerated by heating to release carbon dioxide, and after cooling, it is repeatedly used for absorption of carbon dioxide. .
- the present invention A heating step of heating the fuel in the presence of water vapor; Of the product gas obtained in the heating step, a conversion step of converting carbon monoxide and water vapor into carbon dioxide and hydrogen by reacting, A reforming step of cooling the product gas after the conversion step and then bringing it into contact with a carbon monoxide selective oxidation catalyst to form a reformed gas; A hydrogen separation step of separating hydrogen from the reformed gas by a gas separator; A hydrogen production method comprising: The carbon monoxide selective oxidation catalyst is cooled by cooling water; The thermal energy recovered by the cooling water that has cooled the carbon monoxide selective oxidation catalyst relates to a hydrogen production method that is used for producing water vapor to be supplied to the conversion step.
- the fuel is preferably coal, low-grade coal or biomass.
- biomass here means what can generate
- the carbon monoxide selective oxidation catalyst is a ruthenium catalyst, and is preferably cooled to 60 ° C. or more and 210 ° C. or less with cooling water.
- the gas separation device is preferably an alkali absorption device that absorbs carbon dioxide by an alkali absorption method.
- alkali absorbers By the absorption liquid being pressurized and sent from the absorption tower to the regeneration tower, the inside of the regeneration tower is maintained near or above the critical pressure of carbon dioxide, When the absorbing liquid is fed from the regeneration tower to the absorption tower, it is preferable that the pressure is reduced by a pressure adjusting device.
- the gas separation device is a cryogenic separation device.
- the cryogenic separator by compressing the liquefied carbon dioxide gas generated in the distillation column, the pressure of the liquefied carbon dioxide gas is maintained near or above the critical pressure of carbon dioxide, It is preferable that the reformed gas is precooled before expansion using liquefied carbon dioxide gas generated in the distillation column and hydrogen extracted from the distillation column.
- the hydrogen gas production method of the present invention when gas is produced by using coal, low-grade coal or biomass as fuel and producing hydrogen gas, the gas produced by the carbon monoxide selective oxidation catalyst after the water gas addition reaction (shift reaction) By oxidizing the carbon monoxide remaining therein into carbon dioxide, it is easy to separate hydrogen and carbon monoxide using a gas separator. As a result, even when low-grade coal or the like is used as fuel, high-purity hydrogen can be produced.
- the carbon monoxide selective oxidation catalyst is cooled by cooling water, and the heat energy recovered by the cooling water that has cooled the carbon monoxide selective oxidation catalyst is transferred to the conversion step. It is also characterized by the configuration used for the production of the supplied steam.
- the reaction that oxidizes carbon monoxide to carbon dioxide is an exothermic reaction, and the product gas after the heating and conversion steps is cooled so that the carbon monoxide selective oxidation catalyst is within a temperature range suitable for the catalytic function.
- steam is supplied from the exhaust heat recovery boiler into the shift reactor that performs the conversion process.
- the carbon monoxide selective oxidation catalyst is indirectly cooled with cooling water, and the recovered thermal energy is recovered. By using it as a preheating source for the makeup water in the exhaust heat recovery boiler, it is possible to simultaneously adjust the temperature of the carbon monoxide selective oxidation catalyst and increase the amount of water vapor generated by heat recovery.
- the hydrogen separation step it is preferable to store carbon dioxide separated from hydrogen using a carbon dioxide storage device.
- the present invention also provides: A hydrogen production system that generates hydrogen by gasifying fuel, Hydrogen gas is separated from other gases by a gas separator after contacting the product gas generated by heating coal or low-grade coal in the presence of water vapor with a ruthenium-based catalyst at 60 ° C or higher and 210 ° C or lower. Is obtained by The hydrogen production system includes: A hydrogen transport means for transporting the hydrogen separated from the gas separator to a hydrogen gas consumption place; Carbon dioxide storage means for fixing and storing carbon dioxide in the other gas in an aquifer, coal seam or mining layer of coal or low-grade coal production place, A hydrogen production system comprising:
- the present invention also provides: A hydrogen production system for generating hydrogen by gasifying fuel coal or low-grade coal, Hydrogen is separated from other gases by gas separation cryogenic equipment after contacting the product gas generated by heating coal or low-grade coal in the presence of water vapor with a ruthenium-based catalyst at 60 ° C or higher and 210 ° C or lower.
- the hydrogen production system includes: Hydrogen liquefying means for liquefying hydrogen; A source storage means for storing liquefied hydrogen in a coal or low grade coal source; Transport means for transporting the stored liquefied hydrogen to the liquid hydrogen consumption area; A consumption area storage means for storing liquefied hydrogen in a liquid hydrogen consumption area, Carbon dioxide storage means for fixing and storing carbon dioxide in the other gas in an aquifer, coal seam or mining layer of coal or low-grade coal production place, A hydrogen production system comprising:
- the hydrogen gas production method of the present invention can easily produce high-purity hydrogen gas even when low-grade coal such as subbituminous coal, lignite, and peat is used as fuel. Since low-grade coal is often difficult to transport, hydrogen gas is produced at the low-grade coal production site, and it is left as hydrogen gas or liquefied hydrogen gas as needed, before it is transferred to the hydrogen consumption area. It is preferable to transport. According to the hydrogen gas production system of the present invention, it is possible to easily produce high-purity hydrogen in the production area of low-grade coal and transport it to the hydrogen consumption area as hydrogen gas or liquefied hydrogen. Even if hydrogen gas is used, carbon dioxide is not generated in the hydrogen consumption area.
- low-grade coal such as subbituminous coal, lignite, and peat is used as fuel. Since low-grade coal is often difficult to transport, hydrogen gas is produced at the low-grade coal production site, and it is left as hydrogen gas or liquefied hydrogen gas as needed, before it is transferred to the hydrogen consumption area. It is preferable
- carbon dioxide separated and stored at the time of hydrogen production can be fixed in an aquifer, coal seam, or mining layer in the production area of low-grade coal, etc.
- carbon dioxide is separated and stored at the time of hydrogen production in a production area such as low-grade coal, it is not necessary to collect and store carbon dioxide in the hydrogen consumption area.
- distributed use of hydrogen automobiles, hydrogen gas turbine power generation, hydrogen gas engines and the like becomes possible.
- high-purity hydrogen having a high utility value can be easily produced even when a low-quality fuel such as low-grade coal or biomass is used.
- carbon-free high purity is produced by immobilizing carbon dioxide in the production area such as low-grade coal while producing high-purity hydrogen in the production area such as low-grade coal. Hydrogen gas can be used in consumption areas.
- Embodiment 1 of this invention It is a figure explaining an example of a spouted bed type gasifier preferably used in the hydrogen production method of the present invention. It is a conceptual diagram showing the method of preparing a fuel slurry from raw coal. It is a figure explaining Embodiment 2 of this invention. It is a figure explaining Embodiment 3 of this invention. It is a figure explaining the alkali absorber preferable to be used by this invention. It is a figure explaining the cryogenic separator preferable to be used by this invention. It is a figure explaining the cryogenic separator preferable to be used by this invention as an oxygen production apparatus.
- a conventional technique for producing hydrogen using a gasifier using coal, low-grade coal, biomass, or the like as a fuel will be described with reference to FIG.
- a fuel such as coal is made into a slurry using a kneader.
- water is appropriately added according to the water content of the original fuel.
- the fuel slurry is supplied into the gasifier by a pump.
- Oxygen is supplied into the gasifier from the oxygen separator simultaneously with the fuel slurry.
- the gasification furnace is connected to a shift reactor, and in the gasification furnace, hydrogen, carbon monoxide, carbon dioxide and methane are generated by fuel vaporization.
- the fuel residue after the reaction is discarded as slag, and the product gas is cooled to about 100 ° C. to 200 ° C. by a gas cooler.
- the shift reactor is connected to exhaust heat recovery, and steam (superheated steam, approximately 260 ° C. to 600 ° C.) produced by the exhaust heat recovery boiler is supplied into the shift reactor.
- steam superheated steam, approximately 260 ° C. to 600 ° C.
- the product gas After removing drain water generated by cooling the product gas, the product gas is supplied to a gas separation device and separated into hydrogen and other gases. At this time, as described above, since it is difficult to separate hydrogen and carbon monoxide, when producing hydrogen from low-grade coal or biomass, the ratio of carbon monoxide in the product gas is high. It was difficult to produce high purity hydrogen.
- Carbon dioxide which can be easily separated from hydrogen, is separately collected from the gas separator and stored after being changed to a state where it is easy to store liquefied carbon dioxide, etc. It is fixed to the stratum, deep sea, etc. and finally disposed.
- a ruthenium-based catalyst (Ru / Al 2 O 3 : ruthenium using alumina as a carrier) is preferable in that the reaction heat can be used for preheating the makeup water of the exhaust heat recovery boiler.
- a ruthenium-based catalyst it is necessary to adjust the catalyst temperature to 60 ° C. or more and 210 ° C. or less.
- the saturation temperature at a gasification pressure of 20 MPa is 212 ° C., and the reaction heat is supplied to the makeup water for the exhaust heat recovery boiler. Can be used effectively for preheating.
- the cooling water after cooling the carbon monoxide selective oxidation catalyst is supplied to an exhaust heat recovery boiler that supplies steam to the shift reactor, and is used as preheated boiler supply water.
- the produced gas that has passed through the catalytic device filled with the carbon monoxide selective oxidation catalyst contains almost no carbon monoxide. For this reason, it is easy to separate hydrogen and other gases (carbon dioxide, water vapor, methane, etc.) by the gas separation device. As a result, even when low-grade coal or the like is used as fuel, high-purity hydrogen can be easily produced.
- the high-purity hydrogen gas obtained by the gas separator is transported to a hydrogen consumption area (hydrogen gas consumption area) far from the production area of low-grade coal etc. by a hydrogen transportation means (hydrogen gas transportation means) such as a pipeline. Is done.
- a hydrogen transportation means hydrogen gas transportation means
- the gas mainly composed of carbon dioxide discharged from the gas separation device is appropriately stored in the carbon dioxide storage device as liquefied carbon dioxide gas. After a certain amount of liquefied carbon dioxide gas is stored, it is stored (immobilized) in a reservoir such as a low-grade coal or the like in an aquifer, coal seam or mining layer.
- carbon dioxide can be separated, recovered and immobilized in the production area such as low-grade coal, so there is no need to separate, recover and immobilize carbon dioxide in the hydrogen consuming area, Carbon-free high-purity hydrogen gas can be used in consumption areas.
- Table 1 shows the relationship between the fuel particle size, residence time, gasification temperature, and ash melting point of each type of gasification furnace.
- FIG. 3 an example of a spouted bed type gasification furnace that is preferably used in the hydrogen production method of the present invention is shown in FIG.
- fuel slurry and oxidant oxygen gas or the like
- the upper inner side of the spouted bed gasifier is covered with a fire wall (fire brick, etc.) with a water pipe (heat transfer pipe) embedded in it, and the fuel slurry is heated to about 1500 ° C to gasify it.
- the water pipe is connected to the steam drum attached to the spouted bed gasifier, and water is circulated inside the water pipe and the steam drum.
- part of the heat energy in the furnace is recovered by the water circulating in the water pipe, and high-temperature water and high-temperature steam can be stored in the steam drum.
- the high-temperature steam in the steam drum can be used as a heating source when kneading low-grade coal or the like into a fuel slurry.
- the fuel slurry is obtained by pulverizing raw coal with a pulverizer and then kneading the pulverized raw coal with heating using a kneader.
- Steam supplied from three steam drums can be used.
- steam from the exhaust heat recovery boiler may be used as the heating source.
- a steam supply port is provided in the vicinity of the upper part of the inside covered with a refractory wall, from which steam is supplied into the furnace as a quench.
- the water vapor supply causes a water gas addition reaction (shift reaction) in the lower part of the gasification furnace.
- shift reaction water gas addition reaction
- the temperature of the gas in the furnace decreases to about 1200 ° C., and the slag generated from the fuel slurry accumulates at the bottom of the gasification furnace.
- a dust removing device After the product gas taken out from the lower part of the spouted bed gasifier is cooled, fine particles and the like are removed by a dust removing device (a ceramic filter is drawn in FIG. 3).
- the ceramic filter needs to be back-washed by periodically backflowing the gas from the downstream side, but it is also possible to supply steam from the steam drum as this backwash gas.
- the product gas removed by the dust removing device is further cooled and then supplied to the shift reaction path.
- FIG. 2 Another example of the embodiment of the present invention will be described with reference to FIG.
- the first embodiment shown in FIG. 2 is the same until high-purity hydrogen is obtained by the gas separation device, and the method for treating carbon dioxide discharged from the gas separation device is also the same. For this reason, only differences from the first embodiment will be described.
- the high purity hydrogen obtained by the gas separation device is liquefied to liquid hydrogen by the hydrogen liquefaction device (hydrogen liquefaction means) and then stored in the hydrogen storage device (output storage means).
- the liquid hydrogen stored in the hydrogen storage device is transported to a hydrogen storage device (consumption place storage means) in the liquid hydrogen consumption place by a transport means such as a tanker or a railroad.
- a transport means such as a tanker or a railroad.
- carbon dioxide can be separated, recovered and immobilized in the production area such as low-grade coal, it is not necessary to separate, recover and immobilize carbon dioxide in the hydrogen consuming area, Carbon-free high-purity hydrogen gas can be used in consuming areas (mainly large power plants and steelworks).
- Embodiment 3 Still another example of the embodiment of the present invention will be described with reference to FIG.
- a hydrogen storage device production place storage means
- hydrogen in a liquid hydrogen consumption place is transported by a transport means (first transport means) such as a tanker or a railroad. It is the same until it is transported to the storage device (consumption area storage means), and the same applies to the method for treating the carbon dioxide discharged from the gas separation device. For this reason, only differences from the second embodiment will be described.
- liquid hydrogen is transported to a hydrogen storage device (consumption place storage means) in a liquid hydrogen consumption place by a first transport means such as a tanker or a railroad. Furthermore, it is transported to a distributed hydrogen storage device (distributed hydrogen storage means) such as a hydrogen station or a hydrogen gas station by a second transport means such as a tank lorry and stored there.
- a hydrogen storage device consistumption place storage means
- a distributed hydrogen storage device distributed hydrogen storage means
- second transport means such as a tank lorry
- a distributed hydrogen storage device appropriately supplies liquid hydrogen to factories, hydrogen gas vehicles, etc., but carbon dioxide is not generated even if the supplied hydrogen gas is burned. Separation and recovery of carbon dioxide associated with gas consumption is unnecessary and can be used as carbon-free hydrogen gas.
- Example Assuming that hydrogen is produced by the process shown in FIG. 2 using low-grade coal as a fuel, the composition of hydrogen produced by computer simulation was calculated.
- the properties of the low-grade coal used are as shown in Table 2, and lignite is assumed, but the same applies to peat or biomass having a similar composition.
- the product gas is cooled to 100 ° C to 200 ° C by an exhaust heat recovery boiler / gas cooler, and then the ruthenium catalyst (Ru / Al 2 O 3 ) is cooled to 60 ° C to 210 ° C, and the product gas is contacted and modified.
- the condition was to quality.
- the gas separation device was assumed to be a cryogenic separation device using a plate type distillation column.
- the numerical value of Table 2 is a value on a dry weight basis except moisture.
- Table 3 shows the amount of fuel, oxidant, amount of water vapor, and amount of hydrogen in the obtained product gas (hydrogen gas) to be supplied to the gasification furnaces of Examples and Comparative Examples.
- Table 4 shows the simulation results of the gas composition before the supply to the cryogenic separator.
- Table 5 shows the composition of the product gas (hydrogen gas) obtained by separation from the cryogenic separator.
- the gas composition of the previous stage (stage after selective oxidation of carbon monoxide with a ruthenium catalyst) supplied to the cryogenic separator is compared.
- H 2 O is substantially the same concentration, and because it is easily separated if the condensed water is compared for the other concentrations.
- CO is as small as 0.03%, and in order to obtain high-purity hydrogen gas, only CO 2 needs to be separated.
- CO is contained at 8.9%, and it is necessary to separate CO 2 and CO.
- Table 5 compares the composition of the product gas (hydrogen gas) obtained by separation in the cryogenic separator.
- the product gas contains 21.4% of CO, which is a carbon-free high-purity hydrogen. It is not preferable. Even in the comparative example, it is possible to further improve the purity of hydrogen gas by adding a cryogenic separator, but the cryogenic separator becomes excessive and additional separation power is required. The amount of heat generated cannot be used effectively.
- H 2 was 97.2%, and it was proved that hydrogen gas with higher purity than that of the comparative example was obtained.
- ⁇ Preferred example 1 of gas separator> In the case where the gas separation device used in the present invention is an alkali absorption device, a configuration as shown in FIG. 7 is preferable. 7 absorbs carbon dioxide, pressurizes the absorption liquid after absorption of carbon dioxide with a high-pressure pump, and supplies it to the regeneration tower, and returns the absorption liquid after regeneration to the absorption tower. In this case, the pressure is reduced by a pressure adjusting device such as an expansion valve or a valve.
- an absorption tower that absorbs carbon dioxide in a low-temperature absorption liquid and a regeneration tower that heats the absorption liquid that has absorbed carbon dioxide and releases carbon dioxide are connected by a circulation path of the absorption liquid.
- both pressures are equal.
- the alkali absorber shown in FIG. 7 pressurizes the absorption liquid in the absorption tower with a high-pressure pump and supplies it to the regeneration tower, and a pressure adjusting valve is provided in the path for returning the absorption liquid from the regeneration tower to the absorption tower. By providing, the pressure in the regeneration tower can be maintained higher than the pressure in the absorption tower.
- hydrogen obtained by gasification of coal or the like can be used at normal pressure, and even when used in a gas turbine with a high pressure ratio, a pressure of about 3.5 MPa is sufficient.
- a pressure of about 3.5 MPa is sufficient.
- the carbon dioxide gas is 7.4 MPa or more.
- the temperature in the absorption tower is about 50 ° C. and the temperature in the regeneration tower is about 125 ° C. It is preferable to exchange heat between the absorption liquid pressurized to 7.4 MPa or more by the high-pressure pump and the absorption liquid returned from the regeneration tower to absorption or the like by a heat exchanger.
- the absorption liquid precooled by the heat exchanger and further cooled to about 50 ° C. by the cooler is depressurized from 7.4 MPa to 2.0 MPa by the pressure regulating valve.
- ⁇ Preferred example 2 of gas separator> When the gas separation device used in the present invention is a cryogenic separation device, the structure as shown in FIG. 8 is preferable. 8 is characterized in that liquefied carbon dioxide gas liquefied in a distillation column is pressurized to 7.4 MPa or more by a high-pressure pump.
- the mixed gas of hydrogen and carbon dioxide (reformed gas) is compressed and cooled as necessary, and sent to the distillation tower by an expansion turbine.
- Carbon dioxide with a high boiling point is distilled as liquefied carbon dioxide gas. It is stored at the bottom of the tower.
- this liquefied carbon dioxide gas is taken out from the distillation tower, it is possible to transport carbon dioxide in a supercritical state to the carbon dioxide storage device by pressurizing to 7.4 MPa or more with a high-pressure pump.
- the liquefied carbon dioxide pressurized by the high-pressure pump is supplied to the heat exchanger in order to pre-cool the mixed gas after compression, and then is supplied to the carbon dioxide storage device as high-pressure room temperature carbon dioxide (supercritical state). And will be transported.
- the hydrogen separated from the carbon dioxide is taken out from the upper part of the distillation tower as a hydrogen cold gas, but is supplied to the liquefier when it is made into liquefied hydrogen.
- the hydrogen cold gas may be supplied to a heat exchanger and used to pre-cool the compressed mixed gas.
- oxygen gas generator It is also preferable to produce oxygen (oxygen gas) supplied as an oxidizing agent to the gasification furnace by applying the cryogenic separation apparatus shown in FIG.
- the basic configuration is the same as that of the cryogenic separator shown in FIG.
- oxygen gas supplied as an oxidizing agent to the gasification furnace.
- the nitrogen gas separated from the liquefied oxygen is taken out from the upper part of the distillation tower as nitrogen cold gas, supplied to the heat exchanger for precooling the compressed air, and then released into the atmosphere as nitrogen gas.
- the hydrogen production method and hydrogen production system of the present invention are useful in the energy field and a wide range of industrial fields using hydrogen.
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Abstract
Description
燃料を水蒸気存在下で加熱する加熱工程と、
加熱工程で得られた生成ガスのうち、一酸化炭素と水蒸気とを反応させることにより二酸化炭素と水素に転化する転化工程と、
転化工程後の生成ガスを冷却した後、一酸化炭素選択的酸化触媒と接触させ改質ガスとする改質工程と、
前記改質ガスからガス分離装置によって水素を分離する水素分離工程と、
を有する水素製造方法であって、
前記一酸化炭素選択的酸化触媒は冷却水によって冷却されており、
前記一酸化炭素選択的酸化触媒を冷却した冷却水が回収した熱エネルギーは、転化工程へ供給する水蒸気の製造に利用される、水素製造方法に関する。
吸収塔から再生塔へと吸収液が加圧されて送られることによって、再生塔内が二酸化炭素の臨界圧付近又は臨界圧以上に維持されており、
再生塔から吸収塔へと吸収液が送液される際、圧力調整装置によって減圧させていることが好ましい。
蒸留塔内で発生した液化炭酸ガス及び蒸留塔から取り出される水素を用いて、前記改質ガスが膨張前に予冷されることが好ましい。
燃料をガス化して水素を発生させる水素製造システムであって、
水素ガスは、水蒸気存在化で石炭又は低品位炭を加熱することによって発生した生成ガスを60℃以上210℃以下でルテニウム系触媒と接触させた後、ガス分離装置によって他のガスから分離されることによって得られるものであり、
前記水素製造システムは、
ガス分離装置から分離された水素を水素ガス消費地へと輸送する水素輸送手段と、
前記他のガス中の二酸化炭素を石炭又は低品位炭産出地の帯水層、炭層又は採掘層へと固定化して貯留する二酸化炭素貯留手段と、
を備える水素製造システムに関する。
燃料石炭又は低品位炭をガス化して水素を発生させる水素製造システムであって、
水素は、水蒸気存在化で石炭又は低品位炭を加熱することによって発生した生成ガスを60℃以上210℃以下でルテニウム系触媒と接触させた後、ガス分離深冷装置によって他のガスから分離されることによって得られるものであり、
前記水素製造システムは、
水素を液化させる水素液化手段と、
液化水素を石炭又は低品位炭産出地に貯蔵する産出地貯蔵手段と、
貯蔵した液化水素を液体水素消費地へと輸送する輸送手段と、
液化水素を液体水素消費地に貯蔵する消費地貯蔵手段と、
前記他のガス中の二酸化炭素を石炭又は低品位炭産出地の帯水層、炭層又は採掘層へと固定化して貯留する二酸化炭素貯留手段と、
を備える水素製造システムに関する。
石炭、低品位炭、バイオマス等を燃料とし、ガス化炉を用いて水素を製造する従来技術を、図1に基づいて説明する。まず、石炭等の燃料は、混練機を用いてスラリーとする。このとき、元の燃料の含水量に応じて、適宜水を添加する。燃料のスラリーは、ポンプによってガス化炉内へと供給される。ガス化炉内へは、燃料のスラリーと同時に酸素分離装置から酸素が供給される。
本発明の実施の形態の一例を、図2に基づいて説明する。低品位炭等を燃料スラリーとし、ガス化炉で発生した生成ガスを冷却するまでの工程は、図1に示した従来技術と同じである。本発明の水素製造方法では、生成ガスを冷却した後、セラミックフィルタ、サイクロン集塵機等の脱塵装置を用いて生成ガス中の微粒子等を除去した上で、一酸化炭素選択的酸化触媒と生成ガスとを接触させ、生成ガス中の一酸化炭素を二酸化炭素へと酸化させることにより、生成ガス中の一酸化炭素の割合を極めて低い水準にまで低減することができる。
本発明の実施の形態の別例を、図5に基づいて説明する。図2に示した実施の形態1とは、ガス分離装置によって高純度水素を得るまでは同一であり、ガス分離装置から排出される二酸化炭素の処理方法についても同一である。このため、実施の形態1との相違部分についてのみ説明する。
本発明の実施の形態のさらなる別例を、図6に基づいて説明する。図5に示した実施の形態2とは、水素貯蔵装置(産出地貯蔵手段)内に液化水素を貯蔵し、タンカー、鉄道等の輸送手段(第一輸送手段)によって、液体水素消費地内の水素貯蔵装置(消費地貯蔵手段)へと輸送するまでは同一であり、ガス分離装置から排出される二酸化炭素の処理方法についても同一である。このため、実施の形態2との相違部分についてのみ説明する。
低品位炭を燃料とし、図2に示した工程によって水素を製造することを想定し、コンピュータシミュレーションによって製造される水素の組成を算出した。使用した低品位炭の性状は表2に示すとおりであり、褐炭を想定しているが、組成の近い泥炭又はバイオマスでも同様である。ガス化炉の条件はガス化圧2.0MPa、O2/C=0.56であり、酸化剤としては純度99.5%の酸素を用いた。
共通部分は実施例と同じ条件として、図1に示した工程によって水素を製造することを想定し、コンピュータシミュレーションを行い、製造される水素の組成を算出した。
本発明で使用するガス分離装置がアルカリ吸収装置である場合、図7に示すような構成であることが好ましい。図7のアルカリ吸収装置は、二酸化炭素を吸収させた後、高圧ポンプによって二酸化炭素吸収後の吸収液を加圧して再生塔へと供給すること、及び再生後の吸収液を吸収塔へと返送する際、膨張弁、バルブ等の圧力調整装置によって減圧させることを特徴とする。
本発明で使用するガス分離装置が深冷分離装置である場合、図8に示すような構成であることが好ましい。図8の深冷分離装置は、蒸留塔内で液化した液化炭酸ガスを高圧ポンプによって7.4MPa以上に加圧することを特徴としている。
図9に示す深冷分離装置を応用して、ガス化炉に酸化剤として供給される酸素(酸素ガス)を製造することも好ましい。基本的な構成は、図8に示した深冷分離装置と同じである。原料となる空気を圧縮機によって圧縮し、冷却及び除湿した後、膨張タービンによって蒸留塔内へ送られ、沸点の高い酸素は液化酸素として蒸留塔底部に貯留される。この液化酸素を蒸留塔から取り出す際、高圧ポンプでガス化炉の内圧以上に加圧することにより、酸素ガスを酸化剤としてガス化炉内に供給することが可能となる。その際、加圧後の液化酸素は、圧縮空気を予冷するために熱交換器へと供給され、高圧常温の酸素ガスとしてガス化炉へと供給される。
Claims (10)
- 燃料を水蒸気存在下で加熱する加熱工程と、
加熱工程で得られた生成ガスのうち、一酸化炭素と水蒸気とを反応させることにより二酸化炭素と水素に転化する転化工程と、
転化工程後の生成ガスを冷却した後、一酸化炭素選択的酸化触媒と接触させ改質ガスとする改質工程と、
前記改質ガスからガス分離装置によって水素を分離する水素分離工程と、
を有する水素製造方法であって、
前記一酸化炭素選択的酸化触媒は冷却水によって冷却されており、
前記一酸化炭素選択的酸化触媒を冷却した冷却水が回収した熱エネルギーは、転化工程へ供給する水蒸気の製造に利用される、水素製造方法。 - 前記燃料が石炭、低品位炭又はバイオマスである請求項1に記載の水素製造方法。
- 前記一酸化炭素選択的酸化触媒がルテニウム系触媒であり、冷却水によって60℃以上210℃以下に冷却されている請求項1に記載の水素製造方法。
- 前記ガス分離装置が、アルカリ吸収法によって二酸化炭素を吸収するアルカリ吸収装置である、請求項1に記載の水素製造方法。
- 前記アルカリ吸収装置において、
吸収塔から再生塔へと吸収液が加圧されて送られることによって、再生塔内が二酸化炭素の臨界圧付近又は臨界圧以上に維持されており、
再生塔から吸収塔へと吸収液が送液される際、圧力調整装置によって減圧させている、請求項4に記載の水素製造方法。 - 前記ガス分離装置が深冷分離装置である請求項1に記載の水素製造方法。
- 前記深冷分離装置において、
蒸留塔内で発生した液化炭酸ガスを圧縮することによって、液化炭酸ガスの圧力を二酸化炭素の臨界圧付近又は臨界圧以上に維持しており、
蒸留塔内で発生した液化炭酸ガス及び蒸留塔から取り出される水素を用いて、前記改質ガスが膨張前に予冷される、請求項6に記載の水素製造方法。 - 前記水素分離工程で水素と分離された二酸化炭素を、二酸化炭素貯留装置を用いて貯留する請求項1に記載の水素製造方法。
- 燃料をガス化して水素を発生させる水素製造システムであって、
水素は、水蒸気存在化で石炭又は低品位炭を加熱することによって発生した生成ガスを60℃以上210℃以下でルテニウム系触媒と接触させた後、ガス分離装置によって他のガスから分離されることによって得られるものであり、
前記水素製造システムは、
ガス分離装置から分離された水素を水素消費地へと輸送する水素輸送手段と、
前記他のガス中の二酸化炭素を石炭又は低品位炭産出地の帯水層、炭層又は採掘層へと固定化して貯留する二酸化炭素貯留手段と、
を備える水素製造システム。 - 燃料をガス化して水素を発生させる水素製造システムであって、
水素は、水蒸気存在化で石炭又は低品位炭を加熱することによって発生した生成ガスを60℃以上210℃以下でルテニウム系触媒と接触させた後、ガス分離装置によって他のガスから分離されることによって得られるものであり、
前記水素製造システムは、
水素を液化させる水素液化手段と、
液化水素を石炭又は低品位炭産出地に貯蔵する産出地貯蔵手段と、
貯蔵した液化水素を液体水素消費地へと輸送する輸送手段と、
液化水素を液体水素消費地に貯蔵する消費地貯蔵手段と、
前記他のガス中の二酸化炭素を石炭又は低品位炭産出地の帯水層、炭層又は採掘層へと固定化して貯留する二酸化炭素貯留手段と、
を備える水素製造システム。
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Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2011057498A (ja) * | 2009-09-09 | 2011-03-24 | Kawasaki Heavy Ind Ltd | 水素製造方法及び水素製造装置 |
JP2014095004A (ja) * | 2012-11-08 | 2014-05-22 | Babcock-Hitachi Co Ltd | 高水分固体燃料のガス化システム |
WO2015011826A1 (ja) * | 2013-07-26 | 2015-01-29 | 株式会社ジャパンブルーエナジー | 水素回収方法 |
JP2020051745A (ja) * | 2020-01-08 | 2020-04-02 | 高砂熱学工業株式会社 | 情報通信機器を収容した室の空調システム |
JP2021045710A (ja) * | 2019-09-18 | 2021-03-25 | 中国電力株式会社 | 二酸化炭素ガス回収設備 |
WO2021084942A1 (ja) * | 2019-10-31 | 2021-05-06 | 株式会社下瀬微生物研究所 | 多孔質物質の乾燥装置及びこれを備えた水素製造装置並びに多孔質物質の乾燥方法 |
WO2021210496A1 (ja) * | 2020-04-13 | 2021-10-21 | 三菱重工業株式会社 | 水素放出・貯蔵システム、水素放出・貯蔵方法、アンモニア製造装置、ガスタービン、燃料電池、および製鉄所 |
WO2024111288A1 (ja) * | 2022-11-25 | 2024-05-30 | 三菱重工業株式会社 | 搬送車両、二酸化炭素回収方法及び二酸化炭素搬送方法 |
Families Citing this family (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2997312B1 (fr) * | 2012-10-25 | 2015-12-11 | Air Liquide | Procede et installation pour eliminer le monoxyde de carbone d'un flux gazeux comprenant du co2 et recuperer l'energie d'un flux sortant de ladite installation |
WO2014127913A2 (en) * | 2013-02-21 | 2014-08-28 | Faramarz Bairamijamal | High pressure process for co2 capture, utilization for heat recovery, power cycle, super-efficient hydrogen based fossil power generation and conversion of liquid co2 with water to syngas and oxygen |
CN103787274B (zh) * | 2014-01-26 | 2015-06-10 | 程礼华 | 远程防爆煤化二氧化碳循环利用制氢装置及其工艺 |
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CN110790231B (zh) * | 2019-10-28 | 2023-08-22 | 中科液态阳光(苏州)氢能科技发展有限公司 | 低压制氢系统用二氧化碳混合余气分离系统及其方法 |
CN111420539A (zh) * | 2020-05-07 | 2020-07-17 | 兰州理工大学 | 一种基于气体水合物法净化汽车尾气系统及方法 |
CN112212610B (zh) * | 2020-09-16 | 2022-04-19 | 中国海洋石油集团有限公司 | 一种lng制备液氢的方法 |
EP4166455A1 (en) * | 2021-10-15 | 2023-04-19 | Beckers Innovation GmbH | Method and system for transmitting energy |
US11685659B2 (en) | 2021-11-24 | 2023-06-27 | Uop Llc | Processes and apparatuses for reducing carbon monoxide levels in a gaseous stream |
JP7251858B2 (ja) | 2022-10-07 | 2023-04-04 | 廣存 高橋 | バイオ多段式水素発生システム |
Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH03242301A (ja) | 1990-02-19 | 1991-10-29 | Nkk Corp | 水素製造方法 |
JPH1072202A (ja) * | 1996-08-29 | 1998-03-17 | Shipbuild Res Assoc Japan | 改質ガス中の一酸化炭素除去方法及び装置 |
JP2003074372A (ja) * | 2001-06-22 | 2003-03-12 | Kawasaki Heavy Ind Ltd | 地下の石炭層を用いて燃料と燃焼ガスのクローズドシステムを構築したガスタービン設備 |
JP2004182501A (ja) | 2002-12-02 | 2004-07-02 | Kansai Electric Power Co Inc:The | バイオマスからの水素製造方法 |
JP2005040660A (ja) * | 2003-07-23 | 2005-02-17 | Nissan Motor Co Ltd | 触媒反応装置、熱交換器、および燃料改質システム |
JP2005330170A (ja) | 2004-05-21 | 2005-12-02 | Toshiba Corp | 水素製造システムおよび水素製造方法 |
JP2008144113A (ja) | 2006-12-13 | 2008-06-26 | Kobe Steel Ltd | 固形燃料の製造方法および製造装置 |
JP2009013320A (ja) | 2007-07-06 | 2009-01-22 | National Institute Of Advanced Industrial & Technology | 水素の製造方法 |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2000059825A1 (fr) * | 1999-04-02 | 2000-10-12 | Ebara Corporation | Procede et appareil de production d'hydrogene par gazeification de matiere combustible |
ATE302737T1 (de) * | 1999-05-03 | 2005-09-15 | Nuvera Fuel Cells | Autothermen dampfreformierungsystem mit integrierten shift betten , reaktor für präferentielle oxidation ,hilfsreaktor und systemsteuerungen |
EP1207132A4 (en) * | 1999-07-09 | 2006-03-29 | Ebara Corp | METHOD FOR PRODUCING HYDROGEN BY GASIFICATION OF COMBUSTIBLE MATERIAL AND METHOD FOR ELECTRIC CURRENT MANUFACTURING USING A FUEL CELL AND POWER GENERATION SYSTEM USING FUEL CELLS |
CA2354343A1 (en) * | 2000-07-31 | 2002-01-31 | H. Power Corp. | Integrated selective oxidation reactor apparatus and process |
AU2002354393B2 (en) * | 2001-11-09 | 2005-06-23 | Kawasaki Jukogyo Kabushiki Kaisha | Gas turbine system comprising closed system between fuel and combustion gas using underground coal layer |
EP2023066A1 (en) * | 2007-07-25 | 2009-02-11 | BP Alternative Energy Holdings Limited | Separation of carbon dioxide and hydrogen |
-
2010
- 2010-06-01 EP EP10799557.3A patent/EP2455336B1/en active Active
- 2010-06-01 NO NO10799557A patent/NO2455336T3/no unknown
- 2010-06-01 WO PCT/JP2010/003657 patent/WO2011007493A1/ja active Application Filing
- 2010-06-01 CN CN201080021415.7A patent/CN102428024B/zh active Active
- 2010-06-01 AU AU2010272097A patent/AU2010272097B2/en active Active
- 2010-06-01 JP JP2011522693A patent/JP5629259B2/ja active Active
Patent Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH03242301A (ja) | 1990-02-19 | 1991-10-29 | Nkk Corp | 水素製造方法 |
JPH1072202A (ja) * | 1996-08-29 | 1998-03-17 | Shipbuild Res Assoc Japan | 改質ガス中の一酸化炭素除去方法及び装置 |
JP2869525B2 (ja) | 1996-08-29 | 1999-03-10 | 社団法人日本造船研究協会 | 改質ガス中の一酸化炭素除去方法及び装置 |
JP2003074372A (ja) * | 2001-06-22 | 2003-03-12 | Kawasaki Heavy Ind Ltd | 地下の石炭層を用いて燃料と燃焼ガスのクローズドシステムを構築したガスタービン設備 |
JP2004182501A (ja) | 2002-12-02 | 2004-07-02 | Kansai Electric Power Co Inc:The | バイオマスからの水素製造方法 |
JP2005040660A (ja) * | 2003-07-23 | 2005-02-17 | Nissan Motor Co Ltd | 触媒反応装置、熱交換器、および燃料改質システム |
JP2005330170A (ja) | 2004-05-21 | 2005-12-02 | Toshiba Corp | 水素製造システムおよび水素製造方法 |
JP2008144113A (ja) | 2006-12-13 | 2008-06-26 | Kobe Steel Ltd | 固形燃料の製造方法および製造装置 |
JP2009013320A (ja) | 2007-07-06 | 2009-01-22 | National Institute Of Advanced Industrial & Technology | 水素の製造方法 |
Cited By (18)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2011057498A (ja) * | 2009-09-09 | 2011-03-24 | Kawasaki Heavy Ind Ltd | 水素製造方法及び水素製造装置 |
JP2014095004A (ja) * | 2012-11-08 | 2014-05-22 | Babcock-Hitachi Co Ltd | 高水分固体燃料のガス化システム |
WO2015011826A1 (ja) * | 2013-07-26 | 2015-01-29 | 株式会社ジャパンブルーエナジー | 水素回収方法 |
JP6055920B2 (ja) * | 2013-07-26 | 2016-12-27 | 株式会社ジャパンブルーエナジー | 水素回収方法 |
JP2021045710A (ja) * | 2019-09-18 | 2021-03-25 | 中国電力株式会社 | 二酸化炭素ガス回収設備 |
JP7360864B2 (ja) | 2019-09-18 | 2023-10-13 | 中国電力株式会社 | 二酸化炭素ガス回収設備 |
CN114207371B (zh) * | 2019-10-31 | 2023-06-27 | 株式会社下濑微生物研究所 | 多孔质物质的干燥装置、具备该干燥装置的氢制造装置以及多孔质物质的干燥方法 |
WO2021084942A1 (ja) * | 2019-10-31 | 2021-05-06 | 株式会社下瀬微生物研究所 | 多孔質物質の乾燥装置及びこれを備えた水素製造装置並びに多孔質物質の乾燥方法 |
JP2021071241A (ja) * | 2019-10-31 | 2021-05-06 | 株式会社下瀬微生物研究所 | 多孔質物質の乾燥装置及びこれを備えた水素製造装置並びに多孔質物質の乾燥方法 |
AU2020376194B2 (en) * | 2019-10-31 | 2023-08-17 | Shimose Microbes Laboratory Corporation | Drying device for porous substance, hydrogen production device comprising same, and method for drying porous substance |
CN114207371A (zh) * | 2019-10-31 | 2022-03-18 | 株式会社下濑微生物研究所 | 多孔质物质的干燥装置、具备该干燥装置的氢制造装置以及多孔质物质的干燥方法 |
JP7146277B2 (ja) | 2019-10-31 | 2022-10-04 | 株式会社下瀬微生物研究所 | 多孔質物質の乾燥装置を備えた水素製造装置、および水素製造方法 |
JP2020051745A (ja) * | 2020-01-08 | 2020-04-02 | 高砂熱学工業株式会社 | 情報通信機器を収容した室の空調システム |
JP2021167263A (ja) * | 2020-04-13 | 2021-10-21 | 三菱重工業株式会社 | 水素放出・貯蔵システム、水素放出・貯蔵方法、アンモニア製造装置、ガスタービン、燃料電池、および製鉄所 |
JP7354051B2 (ja) | 2020-04-13 | 2023-10-02 | 三菱重工業株式会社 | 水素放出・貯蔵システム、水素放出・貯蔵方法、アンモニア製造装置、ガスタービン、燃料電池、および製鉄所 |
WO2021210496A1 (ja) * | 2020-04-13 | 2021-10-21 | 三菱重工業株式会社 | 水素放出・貯蔵システム、水素放出・貯蔵方法、アンモニア製造装置、ガスタービン、燃料電池、および製鉄所 |
AU2021256364B2 (en) * | 2020-04-13 | 2024-04-04 | Mitsubishi Heavy Industries, Ltd. | Hydrogen release/storage system, hydrogen release/storage method, ammonia production equipment, gas turbine, fuel cell, and steel mill |
WO2024111288A1 (ja) * | 2022-11-25 | 2024-05-30 | 三菱重工業株式会社 | 搬送車両、二酸化炭素回収方法及び二酸化炭素搬送方法 |
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AU2010272097A1 (en) | 2012-01-19 |
JP5629259B2 (ja) | 2014-11-19 |
CN102428024A (zh) | 2012-04-25 |
CN102428024B (zh) | 2014-10-08 |
EP2455336B1 (en) | 2018-04-04 |
EP2455336A1 (en) | 2012-05-23 |
AU2010272097B2 (en) | 2013-05-09 |
JPWO2011007493A1 (ja) | 2012-12-20 |
EP2455336A4 (en) | 2013-12-04 |
NO2455336T3 (ja) | 2018-09-01 |
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