WO2017149718A1 - アンモニアの製造方法 - Google Patents
アンモニアの製造方法 Download PDFInfo
- Publication number
- WO2017149718A1 WO2017149718A1 PCT/JP2016/056556 JP2016056556W WO2017149718A1 WO 2017149718 A1 WO2017149718 A1 WO 2017149718A1 JP 2016056556 W JP2016056556 W JP 2016056556W WO 2017149718 A1 WO2017149718 A1 WO 2017149718A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- ammonia
- gas
- concentration
- psa
- nitrogen
- Prior art date
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/04—Preparation of ammonia by synthesis in the gas phase
- C01C1/0494—Preparation of ammonia by synthesis in the gas phase using plasma or electric discharge
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/04—Preparation of ammonia by synthesis in the gas phase
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/12—Separation of ammonia from gases and vapours
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/22—Fuel cells in which the fuel is based on materials comprising carbon or oxygen or hydrogen and other elements; Fuel cells in which the fuel is based on materials comprising only elements other than carbon, oxygen or hydrogen
- H01M8/222—Fuel cells in which the fuel is based on compounds containing nitrogen, e.g. hydrazine, ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/406—Ammonia
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
- F02C3/04—Gas-turbine plants characterised by the use of combustion products as the working fluid having a turbine driving a compressor
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F05—INDEXING SCHEMES RELATING TO ENGINES OR PUMPS IN VARIOUS SUBCLASSES OF CLASSES F01-F04
- F05D—INDEXING SCHEME FOR ASPECTS RELATING TO NON-POSITIVE-DISPLACEMENT MACHINES OR ENGINES, GAS-TURBINES OR JET-PROPULSION PLANTS
- F05D2210/00—Working fluids
- F05D2210/10—Kind or type
- F05D2210/12—Kind or type gaseous, i.e. compressible
-
- 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
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Definitions
- the present invention relates to an industrial ammonia production method in an ammonia synthesis process using electrolysis using nitrogen gas and water as raw materials.
- ammonia is widely produced at the industrial level by the Harbor Bosch method.
- the Harbor Bosch method ammonia is obtained by reacting hydrogen and nitrogen under high pressure conditions of 400 to 600 ° C. and 20 to 40 MPa using a catalyst mainly composed of iron.
- a catalyst in which the catalytic performance of iron is improved by adding alumina and potassium oxide to iron is used.
- a Ru-based catalyst is proposed.
- FIG. 1 Such a conventional ammonia synthesis process is shown in FIG.
- An ammonia component is recovered as liquid ammonia from a product gas obtained by reacting a mixed gas of nitrogen and hydrogen as an ammonia source gas with an ammonia synthesis reactor under pressure.
- the product gas contains hydrogen, nitrogen, and argon as raw materials as impurities.
- the ammonia is liquefied and separated at high pressure and low temperature. There is a need.
- reaction and recovery under pressure are required, it is necessary to design a pressure vessel, and power consumption accompanying pressurization, heating, and cooling is large, consuming a lot of energy, and as a raw material
- fossil fuels such as natural gas are used, and carbon dioxide, which is said to cause global warming, is emitted.
- Patent Document 1 discloses an ammonia electrosynthesis method using a proton conductive oxide as a solid electrolyte.
- Patent Document 2 Japanese Patent Laid-Open No. 2014-40336 (Patent Document 2), a proton exchange membrane is used as a material that transmits hydrogen ions, and an ionic liquid in which a metallocene complex is dissolved is used as a catalyst.
- An ammonia production process is disclosed in which a predetermined potential is applied in a state in which is isolated from each other.
- Patent Document 3 proposes a process of combining an ammonia synthesis process with an ammonia separation membrane device that separates only ammonia gas.
- Patent Document 3 by applying a membrane separation method, it is possible to efficiently separate ammonia by using the self-pressure of synthesis gas by ammonia synthesis, so that the refrigeration system power for liquefied ammonium production can be reduced. It shows that you can.
- JP 2013-209684 A Japanese Unexamined Patent Publication No. 2014-40336 Japanese Unexamined Patent Publication No. 2014-162662
- ammonia synthesis process such as the Harbor Bosch method
- hydrogen and nitrogen as raw materials are included as impurities in addition to ammonia as a product in the product gas.
- ammonia was liquefied and separated in order to separate these impurities at low cost.
- the ammonia concentration in the unreacted return gas separated from the membrane so that the membrane alone separates almost 100% ammonia and the ammonia concentration is preferably 2% or less at the inlet of the ammonia synthesis tower.
- a separation membrane is required.
- Such a film has a high technical difficulty, so that it becomes expensive and there are problems such as leakage of an inert to the high purity ammonia side.
- the ammonia production process using electrolysis supplies only the amount of hydrogen required for ammonia synthesis via the proton exchange membrane or anion exchange membrane. Therefore, it has the characteristic that the operation
- the reaction conditions for the ammonia synthesis reaction are usually normal temperature and normal pressure, unlike conventional methods such as the Harbor Bosch method.
- ammonia synthesis gas such as the conventional Harbor Bosch method
- hydrogen and ammonia must be separated if ammonia is to be recovered on the permeate side or non-adsorption side, even if an attempt is made to use a concentration separation process such as membrane separation or PSA.
- a concentration separation process such as membrane separation or PSA.
- the ammonia recovery rate is extremely reduced, and the gas pressure decreases by adsorbing ammonia, There is a problem that the power of recompression is an issue. For this reason, techniques such as membrane separation are difficult to adopt with conventional ammonia synthesis gas.
- the present invention by combining an electrolysis method, an ammonia separation membrane or PSA, and a liquefaction separation device, even when the separation membrane or PSA alone has a leakage of inert components such as nitrogen to the ammonia side of about 20%. It is characterized by a power reduction effect.
- an inert component is allowed to be mixed into the high-concentration ammonia side, for example, a cheaper ammonia separation membrane can be selected than the invention described in Patent Document 3, and an inert component can be mixed.
- an inert component can be mixed.
- Patent Document 3 discloses that a membrane is separated by an ammonia separation membrane in the previous step of cooling and liquefying ammonia, but this is a case where hydrogen transfer is not taken into consideration, suggesting that it is combined with an electrolysis method. Not what you want.
- a part of the residual gas to be recycled is discharged out of the system as a purge gas to suppress the concentration of argon, and at least a part of the discharged purge gas is recovered from the ammonia separation membrane or ammonia PSA.
- [3] A power generation method for generating power by burning the high-concentration ammonia obtained by the method of [1] or [2] and driving a gas turbine using the obtained gas as a working medium.
- [4] A method for using high-concentration ammonia, wherein the high-concentration ammonia obtained in [1] or [2] is introduced as a fuel for an ammonia fuel cell.
- ammonia is synthesized using an electrolysis method in which hydrogen is not substantially contained in ammonia synthesis, and combined with membrane separation and PSA ammonia separation / recovery treatment. This makes it possible to synthesize and recover highly concentrated ammonia with high efficiency throughout the process.
- the process configuration of the present invention can be configured without the need for an external heat source, and can be easily operated only by electric power, and therefore has a very good compatibility with renewable energy such as solar power generation and wind power generation.
- Renewable energy such as solar power generation and wind power generation.
- High-purity ammonia can be easily liquefied, and in recent years, development as a fuel for gas turbines for power generation has also been advanced. Therefore, it can be used as a means for storing and transporting liquid fuel derived from renewable energy, and its utility value is very high.
- the schematic diagram of one mode of the ammonia synthesis process of the present invention is shown.
- a schematic diagram of a conventional ammonia synthesis process is shown.
- mode of the ammonia synthesis process at the time of applying a prior art is shown.
- 1 shows a schematic diagram of one embodiment of an ammonia synthesis process of the present invention.
- 1 shows a schematic diagram of one embodiment of an ammonia synthesis process of the present invention.
- 1 shows a schematic diagram of one embodiment of an ammonia synthesis process of the present invention.
- 1 shows a schematic diagram of one embodiment of an ammonia synthesis process of the present invention.
- 1 shows a schematic diagram of one embodiment of an ammonia synthesis process of the present invention.
- 1 shows a schematic diagram of one embodiment of an ammonia synthesis process of the present invention.
- 1 shows a schematic diagram of one embodiment of an ammonia synthesis process of the present invention.
- 1 shows a schematic diagram of one embodiment of an ammonia synthesis process of the present invention.
- 1 shows a schematic diagram of one embodiment of an ammonia synthesis process of the present invention.
- FIGS 1 and 7 show typical process configurations in this patent.
- ammonia separation membrane FIG. 1
- ammonia PSA FIG. 7
- Liquid ammonia is produced by liquefying concentrated ammonia.
- the ammonia treatment at this time may be performed by either the ammonia separation membrane (FIG. 1) or the ammonia PSA (FIG. 7), but both may be combined. In this case, the order is not particularly limited.
- ammonia production process using electrolysis has the feature that it can be operated with almost no hydrogen gas in the product gas.
- a membrane separation process and a PSA process which are rarely used in the conventional ammonia production process, are employed in order to separate and produce ammonia more inexpensively and efficiently.
- membrane separation or ammonia separation by PSA it is inevitable that a certain amount of nitrogen is mixed on the high concentration ammonia side, and conversely, a certain amount of ammonia is mixed on the residual gas side. For this reason, when combining ammonia synthesis by electrolysis and separation / recovery means, it is necessary to construct a process that takes into consideration the characteristics of the product gas, reaction conditions, and the separation / recovery means.
- ammonia raw material In the ammonia synthesis reactor, ammonia is synthesized by reacting nitrogen and water as raw materials by electrolysis.
- air is as nitrogen used as a raw material. Since the efficiency of the ammonia production reaction and impurities such as oxygen and carbon dioxide contained in the air cause an increase in the processing load at the separation equipment during ammonia separation and recovery, the nitrogen concentration should be as high as possible at the raw material stage. It is preferable to use a containing gas. Specifically, it is preferred to use a nitrogen-containing gas containing 78 to 100 mol%, preferably 98 to 100 mol% of nitrogen.
- the gas contained other than nitrogen may be any gas as long as it is inert to the reaction, such as water vapor, hydrogen, argon, carbon dioxide, and the like.
- PSA pressure swing adsorption method
- TSA temperature swing adsorption method
- PTSA pressure temperature swing adsorption method
- the adsorbent is filled with activated carbon, molecular sieve, zeolite or the like. Utilizing the difference in adsorption rate between oxygen and nitrogen and preferentially adsorbing oxygen and the like within a short time under pressure to efficiently obtain nitrogen having a higher purity than air. In these separation methods, it is difficult to remove argon in the air, but argon can be easily removed by a subsequent ammonia liquefaction apparatus, and concentration can be avoided by purging or the like.
- a cryogenic separation type air separation device can be used as a means for obtaining ultra-high purity nitrogen gas.
- the cryogenic separation type air separation apparatus it is possible to obtain nitrogen containing no argon.
- the nitrogen gas as a raw material is preferably supplied after being compressed within a range of 0.1 MPaG to 8 MPaG, and 8 MPaG is a pressure generally used when liquefying ammonia. After liquefaction, a liquid pump which is a more efficient compression means can be used.
- the 2) ammonia synthesis reaction using ammonia synthesis electrolysis, H + mediated and the proton exchange membrane method and OH - the there is a anion exchange membrane method was mediated, either method is also water and nitrogen in the raw material It is a reaction that generates oxygen from the anode side and ammonia from the cathode side, and either can be applied.
- an ammonia production apparatus for example, an ammonia production apparatus disclosed in JP-A-2014-40336 can be exemplified. That is, it is an apparatus for electrochemically synthesizing ammonia from nitrogen gas and water, and a proton exchange membrane that does not permeate water molecules but permeates hydrogen ions (protons). In this state, nitrogen is introduced into the ionic liquid and a predetermined potential is applied between the ionic liquid and water to electrochemically obtain ammonia.
- Nitrogen is introduced to the cathode side of the ammonia synthesizer.
- the cathode side is separated from the anode side by a proton exchange membrane or an anion exchange membrane.
- Another raw material, water is introduced into the anode side of the ammonia synthesizer after impurities are removed by an ion exchange membrane or the like.
- Oxygen is generated from the anode side by electrolysis, and hydrogen is supplied to the cathode side through a proton exchange membrane, and ammonia is synthesized in the presence of the catalyst.
- An ionic liquid is a salt that is composed of a cation and an anion and is in a liquid state at less than 100 ° C.
- the ionic liquid it is particularly preferable to use a liquid that is in a liquid state at room temperature.
- the cation include quaternary ammonium, quaternary phosphonium, tertiary sulfonium, imidazolium, and pyridinium.
- the anion A ⁇ include Cl ⁇ , Br ⁇ , I ⁇ , and BF 4 ⁇ .
- Nafion (registered trademark) NR-212 can be used as a proton exchange membrane.
- anion exchange membrane include hydrocarbon polymers.
- the ionic liquid and water are separated from the ionic liquid and water by a cation exchange membrane, an anion exchange membrane, etc., so that the decomposition of the catalyst in the ionic liquid due to contact with water is suppressed, and the hydrogen ion Since the permeation is adjusted by the proton exchange membrane and the anion exchange membrane, an excessive amount of hydrogen does not exist at the time of ammonia synthesis, so that the amount of hydrogen contained in the ammonia-producing gas can be reduced.
- One of the characteristics of the ammonia synthesis reaction using the electrolysis method is that the reaction can be performed at room temperature, but the operating conditions can be changed in the range of 1 to 300 ° C.
- a method of blowing steam into the raw water may be used.
- the reaction may be normal pressure, but may be pressurized. However, from the viewpoint of power reduction, it is preferable to supply nitrogen and water as raw materials at a higher pressure. This is because the reaction of N 2 + 6H + ⁇ 2NH 3 occurs in the reactor, so that it expands to about twice the volume in the process of synthesis of ammonia gas from nitrogen gas, and more compression energy is required. Because.
- the pressure of the raw material gas although there is a problem of the pressure resistance of the reactor, it is possible to increase the pressure to a pressure generally used when liquefying ammonia, and after the liquefaction, the liquid is a more efficient compression means A pump is available. Specifically, nitrogen is preferably supplied after being compressed in the range of 0.1 MPaG to 8 MPaG.
- the ammonia production process using the electrolysis method at the time of the above ammonia synthesis has almost no hydrogen gas in the produced gas. It has characteristics.
- the ammonia-producing gas obtained by the above electrolysis method contains ammonia, nitrogen, argon contained in the raw material nitrogen, etc., but does not substantially contain hydrogen and is 1 mol% or less.
- the ratio of nitrogen and ammonia varies depending on the reaction conditions and the like, but is appropriately selected depending on the concentration of the target high-concentration ammonia. In the case of electrolysis, the ammonia concentration in the product gas is 1 to 20 mol%.
- ammonia liquefaction is caused because the ammonia concentration in the product gas is low. It requires a lot of energy in the process and is inefficient.
- the ammonia separation membrane is not particularly limited as long as it is a known separation membrane. Examples thereof include a separation membrane made of a synthetic resin, a carbon separation membrane, and the like. Furthermore, examples of the ammonia separation membrane include a porous silica membrane and a carbon membrane.
- the ammonia separation membrane may be one that allows ammonia to permeate, or one that permeates nitrogen or the like and does not permeate ammonia to form a residual gas.
- PSA is an adsorption method in which a plurality of adsorption towers arranged in parallel is used as an adsorption tower, and the pressure is varied (swinged) to separate and recover.
- the adsorbent tower is filled with an adsorbent such as activated carbon or zeolite, and ammonia is separated and recovered by using the pores of the adsorbent and depending on the difference in adsorption capacity due to pressure.
- an adsorption step is performed with pressure in one column, while the desorption step is performed under reduced pressure in the other column, and the adsorption / desorption cycle is repeated in a plurality of columns.
- Ammonia present in the product gas is a polar gas, and oxygen and nitrogen, which are main impurities, are nonpolar gases, and therefore can be easily separated by these methods.
- ammonia can be set on both the adsorption side and the non-adsorption side of the adsorption tower, it is preferable to set ammonia on the non-adsorption side of these processes from the viewpoint of ammonia recovery rate and pressure, but this is not restrictive.
- Impurities in the product gas, especially nitrogen, are mainly removed, but carbon dioxide and oxygen are also removed in this process.
- FIG. 1 is an example in which ammonia is permeated through an ammonia separation membrane to obtain high-concentration ammonia gas.
- the residual gas remaining in the separation membrane includes nitrogen, ammonia that has not permeated, and argon as an impurity.
- FIG. 7 shows an example in which ammonia is adsorbed with ammonia PSA and then diffused to obtain high-concentration ammonia.
- the residual gas that has passed without being adsorbed with PSA contains nitrogen and ammonia that has not been adsorbed. It is. Therefore, in the present invention, this is recycled as the nitrogen side raw material of the ammonia synthesis reactor.
- the residual gas is reused as the nitrogen-side raw material of the ammonia synthesis reactor, and the ammonia in the residual gas is recycled, so that the yield of ammonia is improved and the amount of make-up nitrogen gas is reduced. Therefore, the size of the nitrogen PSA can be reduced.
- the residual gas obtained by membrane separation and PSA is higher in pressure than nitrogen obtained by nitrogen PSA, so the effect of reducing the compression power of the nitrogen side raw material can also be expected, yield of ammonia, construction of nitrogen PSA There are advantages in terms of cost and compression power of raw material nitrogen.
- the purge gas also contains ammonia at a low concentration.
- the purge gas needs to be discharged out of the loop system, but may be mixed into the recovered high-concentration ammonia side as shown in FIG. According to this, it is possible to recover the ammonia in the residual gas without having to provide ammonia discharge facilities such as neutralization while suppressing the concentration of argon.
- the method of mixing the purge gas with the high-concentration ammonia gas is particularly effective when high-concentration ammonia is used as a fuel for an ammonia gas turbine or an ammonia fuel cell that does not require high-purity ammonia.
- the operation conditions can be set without particular limitation as long as the ammonia concentration can be higher than the ammonia concentration in the product gas input to the ammonia separation membrane.
- the ammonia concentration in the high-concentration ammonia to be separated is preferably 50 mol% or more. Therefore, the higher the ammonia concentration performance, the higher the overall efficiency of the process.
- the obtained high-concentration ammonia can be used as it is as a fuel for an ammonia gas turbine and as a fuel for an ammonia fuel cell.
- the high-concentration ammonia thus separated is liquefied. Impurities can be further removed by liquefying with an ammonia liquefier. By using liquid ammonia, portability can be improved.
- Ammonia liquefaction treatment the recovered high-concentration ammonia is liquefied. Liquefaction is performed by temperature reduction / cooling due to compression and expansion.
- High purity ammonia discharged from the separator is introduced into the ammonia liquefier.
- the ammonia component is condensed by lowering the temperature with a heat exchanger using the temperature decrease due to depressurization, and the liquid ammonia is recovered with a gas-liquid separator.
- Impurities such as argon and nitrogen contained in the high-purity ammonia are recovered as an unliquefied gas from the gas side of the gas-liquid separator.
- ammonia liquefier After compressing to about 4-8MPaG, ammonia is liquefied by combining depressurization and cooling process.
- the compression power and cooling energy required per the same amount of liquid ammonia obtained by the ammonia liquefier are smaller as the ammonia concentration in the raw material gas is higher.
- the operation method of increasing the pressure of the liquefier or reducing the temperature of the liquefier as much as possible to reduce the ammonia concentration in the unliquefied gas Is generally taken. For example, when the gas pressure supplied to the liquefier is about 8 MPaG, the operating temperature of the liquefier is cooled to a range of ⁇ 30 ° C. to ⁇ 35 ° C. to be liquefied.
- ammonia liquefier examples include a compressor system that compresses high-concentration ammonia and an ammonia liquefier that cools with a refrigerant to liquefy ammonia.
- the refrigerant ammonia itself can be used as the refrigerant.
- a refrigeration facility for supplying a refrigerant, an ammonia storage tank for storing liquefied ammonia, and the like may be provided.
- the unliquefied gas is treated again with an ammonia separation membrane or PSA.
- an ammonia separation membrane or PSA When the entire amount of unliquefied gas is recycled, there is a problem that impurities are usually concentrated, and there is a problem that power is lost when compressing low-concentration ammonia again.
- the ammonia separation membrane or ammonia PSA It is also possible to process again at
- ammonia separation membrane or ammonia PSA without returning the non-liquefied gas to the ammonia separation membrane or ammonia PSA, for example, a small ammonia separation membrane or ammonia PSA is separately installed for recycling as shown in FIG.
- the ammonia content can be combined with high-concentration ammonia gas, and the remaining gas can be reused as a nitrogen-side raw material.
- FIG. 1 shows an example of a typical process configuration in this patent.
- electrolysis is performed using water and nitrogen as raw materials to synthesize ammonia, and then the resulting product gas is treated with an ammonia separation membrane to produce high-concentration ammonia, and the high-concentration ammonia on the permeate side is liquefied.
- a series of schematic process drawing which manufactures liquid ammonia by liquefying with an apparatus is shown.
- nitrogen used as a raw material is nitrogen gas purified from air by nitrogen PSA.
- the nitrogen gas obtained with nitrogen PSA is pressurized to 1 MPaG and introduced into the cathode side of the proton exchange membrane ammonia synthesizer.
- the cathode side is separated from the anode side by a proton exchange membrane.
- Water, which is another raw material is introduced into the anode side of the proton exchange membrane ammonia synthesizer after impurities are removed by the ion exchange membrane.
- oxygen is generated from the anode side by electrolysis, hydrogen is supplied to the cathode side through the proton exchange membrane, and ammonia is synthesized by the catalyst filled on the anode side.
- Impurities are removed from the product gas obtained in the proton exchange membrane ammonia synthesizer by the ammonia separation membrane, and high concentration ammonia is obtained.
- High concentration ammonia also contains nitrogen gas and argon at a certain concentration.
- high concentration ammonia is liquefied with an ammonia liquefier, and liquid ammonia is recovered.
- the residual gas separated by the ammonia separation membrane is recycled as the nitrogen side raw material of the ammonia synthesis reactor.
- the unliquefied gas recovered from the liquefier is sent to the ammonia separation membrane and the ammonia PSA and separated again together with the product gas.
- Table 1 shows a table comparing the production amount and power consumption of liquid ammonia synthesized by the process configuration according to the present invention.
- the ammonia synthesis reactor uses a proton exchange membrane in FIG. Water was introduced through a proton exchange membrane, and the reaction temperature was 30 ° C. Nitrogen gas is introduced at a pressure of 1 MPa through nitrogen PSA, and the liquefaction device compresses to 8 MPa (temperature: ⁇ 30 ° C.) to perform liquefaction.
- the process configuration on the extension line of the conventional ammonia production technology as shown in FIG. 3 requires a lot of energy in the ammonia liquefaction process and is inefficient.
- Table 3 even if the ammonia concentration in the unliquefied gas is allowed to increase, the loss of product ammonia is not affected. As a result, the energy required for the ammonia liquefier can be greatly reduced. Because it became.
- the operating temperature of the ammonia liquefier can be raised to room temperature or higher, after cooling to about 40-50 ° C with an air-cooling device, a part of the product liquid ammonia is compressed with an ammonia pump and then depressurized. It is also possible to cover the energy required for liquefaction with the cold heat obtained by rapid expansion. Ammonia used for utilizing the cold heat is reused as a liquid ammonia raw material by introducing it again into the ammonia liquefier. With such a configuration, the ammonia liquefying apparatus can be operated without an external cooling source, and an effect of reducing equipment costs can be expected.
- FIG. 4 shows the process configuration of FIG. 1.
- the high concentration ammonia side treated with an ammonia separation membrane is used to recover ammonia in the purge gas while preventing the concentration of impurities such as argon. Recycled process configuration.
- the process configuration of FIG. 1 and the process configuration of FIG. 4 may be selected from the location to which the present invention is applied and the market price, which is more competitive by comparing the market price of liquid ammonia and the power price. .
- FIG. 1 shows a configuration including a step of treating an unliquefied gas supplied from an ammonia liquefier with an ammonia separation membrane again.
- the same ammonia separation membrane is recycled.
- the same effect can be obtained with a configuration in which a small ammonia separation membrane is separately prepared for recycling as shown in FIG.
- the unliquefied gas delivered from the ammonia liquefier contains a certain amount of ammonia. Normally, when ammonia in the unliquefied gas is discharged out of the system, the production amount of product ammonia is equivalent to that amount. Decrease. For this reason, in the ammonia liquefier, in order to increase the yield of product ammonia as much as possible, ammonia in unliquefied gas is treated by treating high-concentration ammonia at higher pressure and lower temperature so that more ammonia is liquefied. The concentration is lowered. When the non-liquefied gas is reused as the raw material gas as in the process configuration of FIGS. 1 and 4, ammonia loss can be reduced even if the ammonia concentration in the non-liquefied gas is increased.
- FIG. 6 shows the case where a membrane from which high-concentration ammonia is obtained from the non-permeating side of the ammonia separation membrane is selected.
- Table 4 shows the gas composition of each stream in the embodiment of FIG.
- the amount of power of the recycle compressor is high, and the power consumption per mole of product liquid ammonia is slightly high. This is because, as a result of the high-concentration ammonia becoming the non-permeate side, argon that is also largely distributed to the non-permeate side is concentrated by the ammonia liquefaction device, which requires a lot of cooling energy, and the recycle compressor also has a remaining amount. This is probably because more pressure power was required as a result of the gas becoming the permeate side.
- ammonia production efficiency it is desirable in terms of ammonia production efficiency to select an ammonia separation membrane so that high-concentration ammonia is discharged from the permeate side of the ammonia separation membrane.
- the obtained high-concentration ammonia can be used as fuel for an ammonia gas turbine or an ammonia fuel cell as it is.
- FIG. 7 shows a configuration including a step of treating the non-liquefied gas supplied from the ammonia liquefier with ammonia PSA again. By reprocessing the unliquefied gas as a raw material gas, it is possible to increase the amount of ammonia produced.
- FIG. 8 shows the process configuration of FIG. 7.
- FIG. 9 shows a configuration in which high-concentration ammonia is recovered on the PSA permeation side through which ammonia is permeated without being adsorbed.
- the power consumption of the recycle compressor is high, and the power consumption per mole of product liquid ammonia is slightly high. This is because, as a result of high-concentration ammonia on the permeate side, argon, which is also largely distributed to the PSA permeate side, is concentrated in the ammonia liquefaction device, requiring a lot of cooling energy, and the recycle compressor also has residual gas. This is probably because more pressure power was required as a result of the fact that became the permeate side.
- FIG. 10 shows a detailed view of a liquid ammonia production process using a proton exchange membrane as an ammonia synthesis method by electrolysis and using an ammonia separation membrane.
- FIG. 10 describes the device configuration of the main configuration unit of the process with respect to the process configuration of FIG. Moreover, although the power consumption rate for each unit for each type is described in Table 1 and Table 5, this uses the sum of the power consumed by the component equipment for each main component unit of the process. .
- FIG. 11 shows a detailed view of a liquid ammonia production process using an anion exchange membrane.
- the supply location of water to the ammonia synthesis reactor is different from that in FIG. 10, the supply of the source gas and the generation of the product gas are the same as in the case of using a proton exchange membrane, and the present invention is applied without any problem. be able to.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Electrochemistry (AREA)
- Metallurgy (AREA)
- Materials Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Physics & Mathematics (AREA)
- Plasma & Fusion (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Fuel Cell (AREA)
- Separation Of Gases By Adsorption (AREA)
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
Description
得られた生成ガスをアンモニア分離膜もしくはアンモニアPSAにて処理して、高濃度アンモニアと残ガスとに分離し、
残ガスをアンモニア合成反応器の窒素ガス原料としてリサイクルするとともに、
アンモニア分離膜もしくはアンモニアPSAにて回収された高濃度アンモニアガスを、さらに液化し、
液化アンモニアから分離された未液化ガスを、再度アンモニア分離膜もしくはアンモニアPSAにて処理することを特徴とする高濃度アンモニアの製造方法。
アンモニア合成反応器では原料として、窒素と水とを電気分解により反応させてアンモニアを合成する。
電気分解を利用したアンモニア合成反応としては、H+を媒介としたプロトン交換膜方式とOH-を媒介としたアニオン交換膜方式があるが、どちらの方式も水と窒素を原料に陽極側から酸素、陰極側からアンモニアを発生する反応であり、どちらでも適応可能である。
得られた生成ガスを、アンモニア分離膜もしくはアンモニアPSAにて処理して高濃度アンモニアを回収する。
本発明では回収した高濃度アンモニアを、液化する。液化は、圧縮および膨張による温度低下/または冷却により行われる。
図1に本特許における代表的なプロセス構成の一例を示す。図1では、水と窒素を原料に電気分解を行い、アンモニアを合成したのち、得られた生成ガスをアンモニア分離膜にて処理して高濃度アンモニアを製造し、透過側の高濃度アンモニアを液化装置にて液化して液体アンモニアを製造する一連の概略工程図を示す。
Claims (4)
- 水と窒素を原料に電気分解を行い、アンモニアを合成したのち、
得られた生成ガスをアンモニア分離膜もしくはアンモニアPSAにて処理して、高濃度アンモニアと残ガスとに分離し、
残ガスをアンモニア合成反応器の窒素ガス原料としてリサイクルするとともに、アンモニア分離膜もしくはアンモニアPSAにて回収された高濃度アンモニアガスを、さらに液化し、
液化アンモニアから分離された未液化ガスを、再度アンモニア分離膜もしくはアンモニアPSAにて処理することを特徴とする高濃度アンモニアの製造方法。 - リサイクルされる残ガスの一部をパージガスとして系外に排出して、アルゴンの濃縮を抑制するとともに、排出されるパージガスの少なくとも一部をアンモニア分離膜もしくはアンモニアPSAから回収される高濃度アンモニアガスに混入させることを特徴とする請求項1に記載の高濃度アンモニアの製造方法。
- 前記請求項1または2に記載の方法で得られた高濃度アンモニアを燃焼し、得られたガスを作動媒体としてガスタービンを駆動して動力を発生する発電方法。
- 前記請求項1または2に記載の方法で得られた高濃度アンモニアをアンモニア燃料電池の燃料として導入することを特徴とする高濃度アンモニアの使用方法。
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2018502447A JPWO2017149718A1 (ja) | 2016-03-03 | 2016-03-03 | アンモニアの製造方法 |
US16/080,673 US10597301B2 (en) | 2016-03-03 | 2016-03-03 | Ammonia production method |
EP16892558.4A EP3441505B1 (en) | 2016-03-03 | 2016-03-03 | Ammonia production method |
PCT/JP2016/056556 WO2017149718A1 (ja) | 2016-03-03 | 2016-03-03 | アンモニアの製造方法 |
AU2016395665A AU2016395665B2 (en) | 2016-03-03 | 2016-03-03 | Ammonia production method |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/JP2016/056556 WO2017149718A1 (ja) | 2016-03-03 | 2016-03-03 | アンモニアの製造方法 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2017149718A1 true WO2017149718A1 (ja) | 2017-09-08 |
Family
ID=59743652
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2016/056556 WO2017149718A1 (ja) | 2016-03-03 | 2016-03-03 | アンモニアの製造方法 |
Country Status (5)
Country | Link |
---|---|
US (1) | US10597301B2 (ja) |
EP (1) | EP3441505B1 (ja) |
JP (1) | JPWO2017149718A1 (ja) |
AU (1) | AU2016395665B2 (ja) |
WO (1) | WO2017149718A1 (ja) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2018015287A1 (de) * | 2016-07-21 | 2018-01-25 | Thyssenkrupp Industrial Solutions Ag | Verfahren zur elektrochemischen herstellung von ammoniak |
CN108744882A (zh) * | 2018-05-29 | 2018-11-06 | 浙江天采云集科技股份有限公司 | 一种led-mocvd制程废气全温程变压吸附提氨再利用的方法 |
WO2019052824A1 (en) * | 2017-09-13 | 2019-03-21 | Haldor Topsøe A/S | PROCESS FOR THE PRODUCTION OF AMMONIA |
WO2019215925A1 (ja) * | 2018-05-11 | 2019-11-14 | 日揮グローバル株式会社 | アンモニア製造プラントおよびアンモニアの製造方法 |
WO2020085324A1 (ja) | 2018-10-23 | 2020-04-30 | つばめBhb株式会社 | アンモニア合成システムおよびアンモニアの製造方法 |
WO2023120031A1 (ja) | 2021-12-21 | 2023-06-29 | 三菱造船株式会社 | 浮体及び浮体の不活性ガス排出方法 |
Families Citing this family (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20220093950A1 (en) * | 2019-01-02 | 2022-03-24 | Ariel University Of Samaria | Solid oxide fuel cell arrangement generating ammonia as byproduct and utilizing ammonia as secondary fuel |
US11885029B2 (en) * | 2019-02-12 | 2024-01-30 | Georgia Tech Research Corporation | Systems and methods for forming nitrogen-based compounds |
EP4061771A1 (en) | 2019-11-21 | 2022-09-28 | Ohmium International, Inc. | Systems and methods of ammonia synthesis |
CN112645353B (zh) * | 2021-01-27 | 2022-05-20 | 复旦大学 | 常温常压水相下球磨氮氢混合气体增强合成氨选择性的方法 |
CN113582200B (zh) * | 2021-06-29 | 2022-09-16 | 福州大学化肥催化剂国家工程研究中心 | 一种耦合氨分离与原料气净化的可再生能源合成氨系统 |
WO2023089602A1 (en) * | 2021-11-17 | 2023-05-25 | Ariel University Of Samaria | Solid oxide fuel cell arrangement generating ammonia as byproduct and utilizing ammonia as secondary fuel |
WO2023156444A1 (de) * | 2022-02-16 | 2023-08-24 | Thyssenkrupp Industrial Solutions Ag | Elektrochemische und chemische synthese von ammoniak |
BE1030273B1 (de) * | 2022-02-16 | 2023-09-11 | Thyssenkrupp Ind Solutions Ag | Elektrochemische und chemische Synthese von Ammoniak |
US20230357941A1 (en) * | 2022-05-06 | 2023-11-09 | Ohmium International, Inc. | Systems and methods for hydrogen and ammonia production |
KR102456434B1 (ko) * | 2022-06-29 | 2022-10-19 | 주식회사 블루텍 | 암모니아를 원료로 활용하는 연소 시스템 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH11292531A (ja) * | 1998-04-16 | 1999-10-26 | Nkk Sogo Sekkei Kk | 排ガス脱硝用の舶用アンモニア製造装置 |
JP2012025985A (ja) * | 2010-07-21 | 2012-02-09 | Hitachi Zosen Corp | アンモニアの合成方法 |
JP2012184132A (ja) * | 2011-03-04 | 2012-09-27 | Nagoya Institute Of Technology | アンモニア製造方法 |
JP2013209684A (ja) * | 2012-03-30 | 2013-10-10 | Nippon Shokubai Co Ltd | アンモニア製造用電気化学セル及びこれを用いたアンモニア合成方法 |
Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6065306A (en) * | 1998-05-19 | 2000-05-23 | The Boc Group, Inc. | Method and apparatus for purifying ammonia |
US20050034479A1 (en) * | 2003-08-13 | 2005-02-17 | The Boc Group | Process and apparatus for enriching ammonia |
US7300642B1 (en) * | 2003-12-03 | 2007-11-27 | Rentech, Inc. | Process for the production of ammonia and Fischer-Tropsch liquids |
JP5966762B2 (ja) | 2012-08-21 | 2016-08-10 | 国立大学法人 名古屋工業大学 | アンモニア製造方法およびアンモニア製造装置 |
JP2014162662A (ja) * | 2013-02-21 | 2014-09-08 | Mitsubishi Heavy Ind Ltd | アンモニア合成システム及び方法 |
KR102301134B1 (ko) * | 2013-08-14 | 2021-09-13 | 커먼웰쓰 사이언티픽 앤드 인더스트리얼 리서치 오가니제이션 | 선택적 투과성 멤브레인을 사용하는 방법 |
US10159969B2 (en) * | 2015-03-31 | 2018-12-25 | Colorado School Of Mines | Ammonia synthesis at moderate conditions using hydrogen permeable membrane reactors |
-
2016
- 2016-03-03 US US16/080,673 patent/US10597301B2/en active Active
- 2016-03-03 WO PCT/JP2016/056556 patent/WO2017149718A1/ja active Application Filing
- 2016-03-03 JP JP2018502447A patent/JPWO2017149718A1/ja active Pending
- 2016-03-03 AU AU2016395665A patent/AU2016395665B2/en active Active
- 2016-03-03 EP EP16892558.4A patent/EP3441505B1/en active Active
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH11292531A (ja) * | 1998-04-16 | 1999-10-26 | Nkk Sogo Sekkei Kk | 排ガス脱硝用の舶用アンモニア製造装置 |
JP2012025985A (ja) * | 2010-07-21 | 2012-02-09 | Hitachi Zosen Corp | アンモニアの合成方法 |
JP2012184132A (ja) * | 2011-03-04 | 2012-09-27 | Nagoya Institute Of Technology | アンモニア製造方法 |
JP2013209684A (ja) * | 2012-03-30 | 2013-10-10 | Nippon Shokubai Co Ltd | アンモニア製造用電気化学セル及びこれを用いたアンモニア合成方法 |
Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2018015287A1 (de) * | 2016-07-21 | 2018-01-25 | Thyssenkrupp Industrial Solutions Ag | Verfahren zur elektrochemischen herstellung von ammoniak |
WO2019052824A1 (en) * | 2017-09-13 | 2019-03-21 | Haldor Topsøe A/S | PROCESS FOR THE PRODUCTION OF AMMONIA |
WO2019215925A1 (ja) * | 2018-05-11 | 2019-11-14 | 日揮グローバル株式会社 | アンモニア製造プラントおよびアンモニアの製造方法 |
JP6664033B1 (ja) * | 2018-05-11 | 2020-03-13 | 日揮グローバル株式会社 | アンモニア製造プラントおよびアンモニアの製造方法 |
US11021373B2 (en) | 2018-05-11 | 2021-06-01 | Jgc Corporation | Ammonia production plant and ammonia production method |
CN108744882A (zh) * | 2018-05-29 | 2018-11-06 | 浙江天采云集科技股份有限公司 | 一种led-mocvd制程废气全温程变压吸附提氨再利用的方法 |
WO2020085324A1 (ja) | 2018-10-23 | 2020-04-30 | つばめBhb株式会社 | アンモニア合成システムおよびアンモニアの製造方法 |
WO2023120031A1 (ja) | 2021-12-21 | 2023-06-29 | 三菱造船株式会社 | 浮体及び浮体の不活性ガス排出方法 |
Also Published As
Publication number | Publication date |
---|---|
AU2016395665A1 (en) | 2018-07-26 |
JPWO2017149718A1 (ja) | 2018-12-27 |
EP3441505A1 (en) | 2019-02-13 |
EP3441505A4 (en) | 2019-11-27 |
EP3441505B1 (en) | 2020-08-26 |
AU2016395665B2 (en) | 2019-07-11 |
US20190092645A1 (en) | 2019-03-28 |
US10597301B2 (en) | 2020-03-24 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2017149718A1 (ja) | アンモニアの製造方法 | |
US20210388511A1 (en) | Process for electrochemical preparation of ammonia | |
WO2017104021A1 (ja) | アンモニアの製造方法 | |
CN108698985B (zh) | 用于供给二氧化碳以合成尿素的方法 | |
RU2592794C2 (ru) | Способ и система для производства хлористого водорода высокой чистоты | |
KR20220038076A (ko) | 화학 물질들의 동시 발생을 구비하는 가스 스트림들로부터의 co2의 알칼리계 제거 | |
US20200131647A1 (en) | Method and system for producing a gas product containing carbon monoxide | |
CN111727273B (zh) | 一氧化碳和/或合成气的电化学制取 | |
JP2024520877A (ja) | モジュール式で輸送可能なクリーンな水素-アンモニア製造装置 | |
EP3717103B1 (en) | A method and an apparatus for separating chlorine gas from a gaseous anode outlet stream of an electrochemical reactor | |
JP2018090436A (ja) | アンモニアの回収方法 | |
JP2014188405A (ja) | 二酸化炭素分離装置及び二酸化炭素分離方法 | |
JP5357465B2 (ja) | 高純度水素製造方法 | |
JP4187569B2 (ja) | 水素製造装置 | |
US20220235478A1 (en) | Method and plant for producing a carbon-monoxide-rich gas product | |
JP2024059655A (ja) | アンモニア水の製造方法 | |
WO2019008741A1 (ja) | アンモニアの回収方法および回収装置 | |
CN117585686A (zh) | 一种合成氨方法 | |
JP2011251864A (ja) | 高圧下における二酸化炭素の分離装置及びその方法 | |
CN117599703A (zh) | 一种合成氨系统 | |
JP2011073909A (ja) | Co2回収方法及びco2回収装置 | |
WO2019043875A1 (ja) | 高窒素含有天然ガスを用いたアンモニアの製造方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
ENP | Entry into the national phase |
Ref document number: 2018502447 Country of ref document: JP Kind code of ref document: A |
|
ENP | Entry into the national phase |
Ref document number: 2016395665 Country of ref document: AU Date of ref document: 20160303 Kind code of ref document: A |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2016892558 Country of ref document: EP |
|
ENP | Entry into the national phase |
Ref document number: 2016892558 Country of ref document: EP Effective date: 20181004 |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 16892558 Country of ref document: EP Kind code of ref document: A1 |