WO2022153720A1 - アンモニア分解装置 - Google Patents
アンモニア分解装置 Download PDFInfo
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- WO2022153720A1 WO2022153720A1 PCT/JP2021/044815 JP2021044815W WO2022153720A1 WO 2022153720 A1 WO2022153720 A1 WO 2022153720A1 JP 2021044815 W JP2021044815 W JP 2021044815W WO 2022153720 A1 WO2022153720 A1 WO 2022153720A1
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- ammonia
- gas
- raw material
- reactor
- chamber
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 321
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 150
- 238000000354 decomposition reaction Methods 0.000 title claims abstract description 72
- 239000007789 gas Substances 0.000 claims abstract description 151
- 239000002994 raw material Substances 0.000 claims abstract description 74
- 239000003054 catalyst Substances 0.000 claims abstract description 43
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000001257 hydrogen Substances 0.000 claims abstract description 26
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 26
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000000567 combustion gas Substances 0.000 claims abstract description 17
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 12
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 9
- 238000004891 communication Methods 0.000 claims abstract description 5
- 238000010790 dilution Methods 0.000 claims description 10
- 239000012895 dilution Substances 0.000 claims description 10
- 239000011819 refractory material Substances 0.000 claims description 8
- 239000000463 material Substances 0.000 abstract description 13
- 239000003085 diluting agent Substances 0.000 abstract description 5
- 238000006396 nitration reaction Methods 0.000 abstract 1
- 238000004064 recycling Methods 0.000 description 13
- 238000011084 recovery Methods 0.000 description 12
- 238000007865 diluting Methods 0.000 description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000005121 nitriding Methods 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 238000003860 storage Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000005192 partition Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 239000011449 brick Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 230000004308 accommodation Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
Images
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0278—Feeding reactive fluids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/04—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of inorganic compounds, e.g. ammonia
- C01B3/047—Decomposition of ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00504—Controlling the temperature by means of a burner
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0266—Processes for making hydrogen or synthesis gas containing a decomposition step
- C01B2203/0277—Processes for making hydrogen or synthesis gas containing a decomposition step containing a catalytic decomposition step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/042—Purification by adsorption on solids
- C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
Definitions
- the present disclosure relates to an ammonia decomposition apparatus.
- This application claims priority based on Japanese Patent Application No. 2021-004399 filed with the Japan Patent Office on January 14, 2021, and the contents thereof are incorporated herein by reference.
- Patent Document 1 describes an ammonia decomposition device that decomposes ammonia into hydrogen and nitrogen by heating the catalyst layer from the outside while allowing ammonia to pass through.
- ammonia reacts with the iron-based material to nitrid the iron-based material.
- the mechanical strength is reduced. Then, for example, when the pipe filled with the catalyst is made of an iron-based material, the mechanical strength of the pipe may decrease, which may lead to breakage of the pipe.
- At least one embodiment of the present disclosure is an object of providing an ammonia decomposition apparatus capable of suppressing nitriding of a material of a reactor in which ammonia is decomposed.
- the ammonia decomposition apparatus includes a reactor filled with a catalyst for a decomposition reaction that decomposes ammonia as a raw material into hydrogen and nitrogen, and before the raw material flows into the catalyst.
- a diluted gas supply line for supplying the diluted gas and an ammonia reactor for burning a part of the ammonia are provided so that the diluted gas having a lower ammonia concentration than the raw material and the raw material are mixed.
- the reactor includes a catalyst accommodating portion for accommodating the catalyst, and the inside of the reactor is a first chamber to which the raw material is supplied and a chamber on the downstream side of the first chamber in the direction in which the raw material is distributed.
- the catalyst accommodating portion is provided so as to communicate with each of the first chamber and the second chamber and extend from the second chamber, and is produced from the raw material by the decomposition reaction.
- the effluent gas line in which the crudely decomposed gas flows out from the reactor as effluent gas, communicates with the second chamber on the upstream side of the communication portion where the catalyst accommodating portion communicates with the second chamber, and the ammonia.
- the combustion gas from the reactor is supplied to the second chamber.
- the ammonia decomposition apparatus of the present disclosure since the ammonia concentration in the reactor is lowered by the diluting gas, the nitriding of the material constituting the reactor in which ammonia is decomposed can be suppressed.
- ammonia decomposition apparatus according to the embodiment of the present disclosure will be described with reference to the drawings.
- Such an embodiment shows one aspect of the present disclosure, does not limit the disclosure, and can be arbitrarily modified within the scope of the technical idea of the present disclosure.
- the ammonia decomposition apparatus 1 is an apparatus that decomposes ammonia as a raw material into hydrogen and nitrogen by the reaction represented by the following reaction formula (1).
- the ammonia decomposition apparatus 1 includes a reactor 2 filled with a catalyst 3 for an ammonia decomposition reaction represented by the reaction formula (1). 2NH 3 ⁇ N 2 + 3H 2 ... (1)
- a raw material supply line 4 for supplying raw materials to the reactor is connected to the reactor 2.
- the raw material supply line 4 is provided with an evaporator 5 that evaporates liquid ammonia supplied from a storage facility (not shown) that stores liquid ammonia and evaporates it into gaseous ammonia.
- a storage facility not shown
- an outflow gas line 6 through which the outflow gas flowing out from the reactor 2 flows is connected to the reactor 2.
- the effluent gas contains nitrogen, hydrogen, and unreacted ammonia.
- the other end of the outflow gas line 6 is connected to the ammonia recovery device 7.
- the configuration of the ammonia recovery device 7 is not particularly limited, and may be, for example, a water scrubber, a pressure fluctuation adsorption (PSA) device, or the like.
- the outflow gas line 6 is provided with a cooler 8 for cooling the outflow gas on the upstream side of the ammonia recovery device 7.
- the cooler 8 may be, for example, a heat exchanger that exchanges heat between the liquid ammonia before flowing into the evaporator 5 and the outflow gas. According to this configuration, since the effluent gas is cooled and the temperature of the liquid ammonia is raised, it is possible to reduce the energy for raising the temperature of the liquid ammonia in the evaporator 5.
- a recovered ammonia line 9 is provided in order to return the liquid ammonia recovered by the ammonia recovery device 7 to the raw material supply line 4 on the upstream side of the evaporator 5.
- One end of a refined decomposition gas line 10 for supplying the refined decomposition gas generated by removing ammonia from the effluent gas by the ammonia recovery device 7 to a decomposition gas consuming facility such as a hydrogen station is connected to the ammonia recovery device 7.
- An outflow gas recycling line 11 is provided between the cooler 8 and the ammonia recovery device 7 in which one end is connected to the outflow gas line 6 and the other end is connected to the raw material supply line 4.
- the outflow gas recycling line 11 is provided with a compressor 12.
- the inside of the reactor 2 is divided into a first chamber 23 by a partition member 31 and a second chamber 24 on the downstream side of the first chamber 23 in the direction in which the raw material flows through the reactor 2. It is divided into.
- the raw material supply line 4 communicates with the first chamber 23, and the outflow gas line 6 communicates with the second chamber 24.
- the catalyst accommodating portion 26 including a plurality of tubular accommodating pipes 26a is fixed to the partition member 31 at one end 26b side of each, and the second chamber is directed from one end 26b side to the other end 26c side. It is provided so as to extend within 24.
- Each of the accommodating pipes 26a in which the catalyst 3 is accommodated has one end 26b side communicating with the first chamber 23 and the other end 26c side communicating with the second chamber 24.
- the outflow gas line 6 communicates with the second chamber 24 on the upstream side of the other end 26c, which is a communication portion where each accommodating pipe 26a communicates with the second chamber 24.
- the ammonia branch line 13 branches from the raw material supply line 4 on the upstream side of the evaporator 5, and the ammonia branch line 13 communicates with the second chamber 24 of the reactor 2.
- the ammonia branch line 13 is provided with an ammonia combustor 14 for combusting ammonia, and the ammonia combustor 14 is communicated with a compressor 15 for supplying air to the ammonia combustor 14.
- the liquid ammonia flowing into the ammonia branch line 13 is burned by the air supplied from the compressor 15 in the ammonia combustor 14, and becomes a high-temperature combustion gas containing nitrogen and water as main components, and becomes a high-temperature combustion gas of the reactor 2. It flows into the second room 24.
- the combustion gas that has flowed into the second chamber 24 moves toward the first chamber 23 side together with the coarsely decomposed gas that has flowed out from the other end 26c of the accommodating pipe 26a to the second chamber 24.
- the catalyst 3 and the mixed gas are heated when the combustion gas and the crude decomposition gas move in the second chamber 24 toward the first chamber 23 side.
- the heating efficiency of the mixed gas is high.
- At least a part of ammonia in the mixed gas flowing into the storage pipe 26a is decomposed into hydrogen and nitrogen by the decomposition reaction of ammonia represented by the reaction formula (1) by the catalytic action by the catalyst 3, and is roughly decomposed.
- the combustion gas and the crude decomposition gas that heated the catalyst 3 flow out from the second chamber 24 as outflow gas, and flow through the outflow gas line 6.
- ammonia recovery device 7 After being cooled by the cooler 8, a part of the outflow gas flowing through the outflow gas line 6 flows into the outflow gas recycling line 11, and the rest flows into the ammonia recovery device 7.
- ammonia recovery device 7 ammonia is recovered from the effluent gas, and the refined decomposition gas containing hydrogen, nitrogen, a small amount of unrecovered ammonia, and a small amount of water when the ammonia recovery device 7 is a water scrubber is refined and decomposed.
- the ammonia supplied to the decomposed gas consumption facility via the gas line 10 and recovered is supplied to the raw material supply line 4 on the upstream side of the evaporator 5 via the recovered ammonia line 9.
- the outflow gas that has flowed into the outflow gas recycling line 11 is boosted by the compressor 12 and flows into the raw material supply line 4.
- Ammonia gas and effluent gas are mixed in the raw material supply line 4, but when the ammonia gas is 100% ammonia, the effluent gas contains hydrogen and nitrogen in addition to ammonia, so the former ammonia concentration Since the latter ammonia concentration is lower, the ammonia concentration in the mixed gas of the ammonia gas and the outflow gas is lower than the ammonia concentration of the ammonia gas supplied as the raw material. That is, the outflow gas flowing into the raw material supply line 4 via the outflow gas recycling line 11 functions as a diluting gas for diluting the ammonia gas flowing into the first chamber 23.
- the ammonia concentration in the reactor 2 is the outflow gas. Since it is reduced by the outflow gas supplied through the recycling line 11, it is possible to suppress the nitriding of the material constituting the reactor 2. Further, since the catalyst 3 is heated by the heat of the crude decomposition gas and the combustion gas generated by the mixed gas passing through the catalyst 3, it is possible to eliminate the need for an apparatus for heating the catalyst 3.
- the outflow gas before flowing into the ammonia recovery device 7 is used as the diluting gas, but the present invention is not limited to this embodiment.
- the purified decomposition gas flowing out from the ammonia recovery device 7 may be used as a diluting gas. Since the refined decomposition gas is also a gas obtained by recovering ammonia from the effluent gas, it can be said that the effluent gas has flowed out from the reactor 2.
- the liquid ammonia having a concentration of 100% stored in a storage facility (not shown) is evaporated to the gaseous ammonia in the evaporator 5, but the liquid ammonia having a concentration of 100% is supplied to the evaporator 5.
- the main component mixed with a small amount of the mixture may supply the liquid of ammonia to the evaporator 5.
- the ammonia combustor 14 burns only a part of the liquid ammonia flowing through the raw material supply line 4, but the present invention is not limited to this embodiment.
- a part of the liquid ammonia and a part of the outflow gas (which may be a refined decomposition gas) flowing out from the reactor 2 may be configured to be burned in the ammonia combustor 14.
- ammonia is difficult to burn, so even if only ammonia is burned in the ammonia combustor 14, it may be difficult to obtain a combustion gas having a desired temperature.
- the outflow gas contains hydrogen that is easily combusted, ammonia is easily burned in the ammonia combustor 14, so that a combustion gas having a desired temperature can be easily obtained.
- the outflow gas recycling line 11 is connected to the raw material supply line 4, but the present invention is not limited to this form.
- the outflow gas recycling line 11 may be connected to the reactor 2 so as to communicate with the first chamber 23.
- the effluent gas recycling line 11 may be connected to the raw material supply line 4 or to the reactor 2 so as to communicate with the first chamber 23, but the former configuration is made for the following reasons. Is preferable. In the latter configuration, when ammonia gas flows into the first chamber 23 from the raw material supply line 4, a part of the ammonia gas is sprayed on the partition member 31 and one end 26b of the accommodating pipe 26a, whereby the partition member 31 And the accommodating pipe 26a may be nitrided. On the other hand, in the former configuration, ammonia flows into the first chamber 23 in a state of being diluted in advance in the raw material supply line 4, so that the risk of nitriding can be reduced as compared with the latter configuration.
- the inner surface 2a of the reactor 2 may be covered with a refractory material such as bricks, refractory bricks, and refractory cement.
- a refractory material such as bricks, refractory bricks, and refractory cement.
- nitriding by ammonia may occur in the catalyst accommodating portion 26. Therefore, if the entire inner surface 2a of the reactor 2 is covered with a refractory material, it is unnecessary from the viewpoint of action and effect. The cost will increase.
- connection portion 2b between the raw material supply line 4 and the reactor 2 of the inner surface 2a of the reactor 2 may be nitrided.
- the inner surface 2a is partially covered with the refractory material 44 so as to surround the connection portion 2b, the temperature rise of the connection portion 2b is suppressed by the refractory material 44, so that the cost is higher than necessary. It is possible to reduce the possibility that the connecting portion 2b is nitrided without the need for the connection portion 2b.
- the diluting gas was the outflow gas (crude decomposition gas or refined decomposition gas) flowing out from the reactor 2, but the dilution gas is not limited to the outflow gas.
- a dilution gas different from the outflow gas may be prepared separately, and a dilution gas supply line for communicating the dilution gas supply source with the reactor 2 or the raw material supply line 4 may be provided.
- the effluent gas recycling line 11 constitutes the dilution gas supply line.
- Nitrogen gas and hydrogen gas can be used as the diluting gas other than the effluent gas, and hydrogen gas from the hydrogen pipeline may be used as the hydrogen gas.
- hydrogen-containing gas obtained by steam reforming methane and methanol (2) coal gasification gas, (3) blast furnace gas, (4) coke furnace gas, (5) the above (5) 1)-(4) gas with hydrogen increased by aqueous gas shift reaction, (6) gas with carbon dioxide removed from the above-mentioned (5) gas, (7) water content from the above-mentioned (6) gas (8) Hydrogen-containing gas obtained by catalytic reforming of naphtha, (9) Hydrogen-containing gas obtained by electrolysis of water, (10) Hydrogen-containing gas obtained by thermal decomposition reaction of methane.
- a gas containing hydrogen produced in another hydrogen production process such as a gas
- a gas can be used.
- external ammonia decomposition such as hydrogen-containing gas obtained from an external plant that thermally decomposes ammonia and hydrogen-containing gas obtained from an external plant that decomposes ammonia by the autothermal method.
- a hydrogen-containing gas obtained in the process can be used.
- the ammonia decomposition device 1 In the decomposition reaction of ammonia in the first embodiment, only hydrogen and nitrogen are generated, so carbon dioxide is not emitted. Further, in the ammonia combustor 14 of the first embodiment and the combustor 51 of the fourth embodiment, since ammonia and hydrogen are burned, carbon dioxide is not emitted. As described above, as long as the fossil fuel is not used in the first embodiment and the effluent gas is used as the diluting gas, the raw material of the ammonia decomposition device 1 is completed only with ammonia and does not emit carbon dioxide. Therefore, the ammonia decomposition device 1 Is a preferred form of carbon-free process.
- the ammonia decomposition apparatus is A reactor (2) filled with a catalyst (3) for a decomposition reaction that decomposes ammonia, which is a raw material, into hydrogen and nitrogen.
- a dilution gas supply line (11) for supplying the diluted gas so that the diluted gas having a lower ammonia concentration than the raw material and the raw material are mixed before the raw material flows into the catalyst (3).
- Ammonia combustor (14) for burning a part of the ammonia is provided.
- the reactor (2) includes a catalyst accommodating portion (26) accommodating the catalyst (3).
- the inside of the reactor (2) is divided into a first chamber (23) and a second chamber (24) on the downstream side of the first chamber (23) in the direction in which the raw material is distributed.
- the catalyst accommodating portion (26) is provided so as to communicate with each of the first chamber (23) and the second chamber (24) and extend into the second chamber (24).
- the catalyst accommodating portion (26) is the second chamber (24).
- the combustion gas from the ammonia combustor (14) communicates with the second chamber (24) on the upstream side of the communicating portion (the other end 26c of the accommodating pipe 26a) communicating with the second chamber (24). Be supplied.
- the ammonia decomposition apparatus of the present disclosure since the ammonia concentration in the reactor is lowered by the diluting gas, the nitriding of the material constituting the reactor in which ammonia is decomposed can be suppressed. Further, since the catalyst is heated by the heat of the crude decomposition gas and the combustion gas generated by passing ammonia through the catalyst, it is possible to eliminate the need for an apparatus for heating the catalyst.
- the ammonia decomposition device is the ammonia decomposition device of [1].
- the diluted gas is a part of the outflow gas flowing out from the reactor (2).
- the operating cost of the ammonia decomposition device can be reduced as compared with the case where the diluted gas is separately prepared.
- the ammonia decomposition device is the ammonia decomposition device of [1] or [2]. A part of the raw material and a part of the outflow gas flowing out from the reactor (2) are configured to be burned in the ammonia combustor (14).
- ammonia is difficult to burn, so even if only ammonia is burned in an ammonia combustor, it may be difficult to obtain combustion gas at the desired temperature.
- the outflow gas contains hydrogen that is easily combusted, ammonia is easily burned in the ammonia combustor, so that a combustion gas having a desired temperature can be obtained. It will be easier.
- the ammonia decomposition apparatus is the ammonia decomposition apparatus of [1] to [3].
- a raw material supply line (4) for supplying the raw material to the reactor (2) is provided.
- the downstream end of the diluted gas supply line (11) is connected to the raw material supply line (4).
- the ammonia concentration can be lowered before flowing into the reactor, so that nitriding of the material constituting the reactor in which ammonia is decomposed can be further suppressed.
- the ammonia decomposition apparatus is the ammonia decomposition apparatus of [1] to [3].
- the downstream end of the diluent gas supply line (11) is connected to the reactor (2).
- the heat causes the ammonia to react with the material of the raw material supply line, and the raw material The material of the supply line may be nitrided.
- the ammonia and the diluting gas flow into the reactor separately, the possibility that the material of the raw material supply line is nitrided can be reduced.
- the ammonia decomposition device is the ammonia decomposition device of [5].
- a raw material supply line (4) for supplying the raw material to the reactor (2) is provided.
- the inner surface (2a) of the reactor (2) is at least partially covered with a refractory material (44) so as to surround the connecting portion (2b) between the raw material supply line (4) and the reactor (2). It has been.
- Ammonia decomposition device Reactor 2a (reactor) inner surface 2b Connection part 3 Catalyst 4 Raw material supply line 6 Outflow gas line 11 Outflow gas recycling line (diluted gas supply line) 14 Ammonia combustor 23 1st room 24 2nd room 25 3rd room 26 Catalyst storage part 26a Storage pipe (catalyst storage part) 26c (the other end (communication part) of the accommodating pipe) 41 Heater (heating device) 44 Refractory material 51 Combustor (heating device)
Abstract
Description
本願は、2021年1月14日に日本国特許庁に出願された特願2021-004399号に基づき優先権を主張し、その内容をここに援用する。
図1に示されるように、本開示の実施形態1に係るアンモニア分解装置1は、原料であるアンモニアを、下記反応式(1)で示される反応によって水素と窒素とに分解する装置である。アンモニア分解装置1は、反応式(1)で示されるアンモニアの分解反応の触媒3が充填された反応器2を備えている。
2NH3→N2+3H2 ・・・(1)
次に、図1及び図2を参照しながら本開示の実施形態1に係るアンモニア分解装置1の動作を説明する。原料供給ライン4を流通する液体アンモニアの一部はアンモニア分岐ライン13に流入し、残りは蒸発器5に流入する。蒸発器5に流入した液体アンモニアは、蒸発してアンモニアガスとなった後、流出ガスリサイクルライン11を介して原料供給ライン4に供給された流出ガスと混合されて、混合ガスとして反応器2の第1室23内に流入する。第1室23内に流入した混合ガスは、収容管26aに流入し、収容管26a内を流通して、収容管26aの他端26cから第2室24へ粗分解ガスとして流出する。
実施形態1では、希釈ガスとして、アンモニア回収装置7に流入する前の流出ガスを使用しているが、この形態に限定するものではない。アンモニア回収装置7から流出した精製分解ガスを希釈ガスとして使用してもよい。精製分解ガスも流出ガスからアンモニアを回収したガスであるので、反応器2から流出した流出ガスであると言える。また、実施形態1では、図示しない貯蔵設備に貯蔵された濃度100%の液体アンモニアを蒸発器5において気体のアンモニアに蒸発させていたが、濃度100%の液体アンモニアを蒸発器5に供給することに限定するものではなく、少量の混合物が混合した主成分がアンモニアの液体を蒸発器5に供給するようにしてもよい。
原料であるアンモニアを水素と窒素とに分解する分解反応の触媒(3)が充填された反応器(2)と、
前記原料が前記触媒(3)に流入する前に、アンモニア濃度が前記原料よりも低い希釈ガスと前記原料とが混合するように、前記希釈ガスを供給するための希釈ガス供給ライン(11)と、
前記アンモニアの一部を燃焼させるアンモニア燃焼器(14)と
を備え、
前記反応器(2)は、前記触媒(3)を収容する触媒収容部(26)を備え、
前記反応器(2)の内部は、第1室(23)と、前記原料が流通する方向において前記第1室(23)よりも下流側の第2室(24)とに仕切られており、
前記触媒収容部(26)は、前記第1室(23)及び前記第2室(24)のそれぞれに連通するとともに前記第2室(24)内を延びるように設けられ、
前記分解反応によって前記原料から生成した粗分解ガスが流出ガスとして前記反応器(2)から流出後に流通する流出ガスライン(6)は、前記触媒収容部(26)が前記第2室(24)と連通する連通部分(収容管26aの他端26c)よりも上流側で前記第2室(24)に連通し、前記アンモニア燃焼器(14)からの燃焼ガスは前記第2室(24)に供給される。
前記希釈ガスは、前記反応器(2)から流出した流出ガスの一部である。
前記原料の一部と前記反応器(2)から流出した流出ガスの一部とが前記アンモニア燃焼器(14)において燃焼されるように構成されている。
前記原料を前記反応器(2)に供給する原料供給ライン(4)を備え、
前記希釈ガス供給ライン(11)の下流端は前記原料供給ライン(4)に接続されている。
前記希釈ガス供給ライン(11)の下流端は前記反応器(2)に接続されている。
前記原料を前記反応器(2)に供給する原料供給ライン(4)を備え、
前記反応器(2)の内面(2a)は、前記原料供給ライン(4)と前記反応器(2)との接続部分(2b)を取り囲むように、少なくとも部分的に耐火材(44)で覆われている。
2 反応器
2a (反応器の)内面
2b 接続部分
3 触媒
4 原料供給ライン
6 流出ガスライン
11 流出ガスリサイクルライン(希釈ガス供給ライン)
14 アンモニア燃焼器
23 第1室
24 第2室
25 第3室
26 触媒収容部
26a 収容管(触媒収容部)
26c (収容管の)他端(連通部分)
41 加熱器(昇温装置)
44 耐火材
51 燃焼器(昇温装置)
Claims (6)
- 原料であるアンモニアを水素と窒素とに分解する分解反応の触媒が充填された反応器と、
前記原料が前記触媒に流入する前に、アンモニア濃度が前記原料よりも低い希釈ガスと前記原料とが混合するように、前記希釈ガスを供給するための希釈ガス供給ラインと、
前記アンモニアの一部を燃焼させるアンモニア燃焼器と
を備え、
前記反応器は、前記触媒を収容する触媒収容部を備え、
前記反応器の内部は、前記原料が供給される第1室と、前記原料が流通する方向において前記第1室よりも下流側の第2室とに仕切られており、
前記触媒収容部は、前記第1室及び前記第2室のそれぞれに連通するとともに前記第2室内を延びるように設けられ、
前記分解反応によって前記原料から生成した粗分解ガスが流出ガスとして前記反応器から流出後に流通する流出ガスラインは、前記触媒収容部が前記第2室と連通する連通部分よりも上流側で前記第2室に連通し、前記アンモニア燃焼器からの燃焼ガスは前記第2室に供給されるアンモニア分解装置。 - 前記希釈ガスは、前記反応器から流出した流出ガスの一部である、請求項1に記載のアンモニア分解装置。
- 前記原料の一部と前記反応器から流出した流出ガスの一部とが前記アンモニア燃焼器において燃焼されるように構成されている、請求項1または2に記載のアンモニア分解装置。
- 前記原料を前記反応器に供給する原料供給ラインを備え、
前記希釈ガス供給ラインの下流端は前記原料供給ラインに接続されている、請求項1~3のいずれか一項に記載のアンモニア分解装置。 - 前記希釈ガス供給ラインの下流端は前記反応器に接続されている、請求項1~3のいずれか一項に記載のアンモニア分解装置。
- 前記原料を前記反応器に供給する原料供給ラインを備え、
前記反応器の内面は、前記原料供給ラインと前記反応器との接続部分を取り囲むように、少なくとも部分的に耐火材で覆われている、請求項5に記載のアンモニア分解装置。
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