WO2011074524A1 - アンモニアの合成方法 - Google Patents
アンモニアの合成方法 Download PDFInfo
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- WO2011074524A1 WO2011074524A1 PCT/JP2010/072348 JP2010072348W WO2011074524A1 WO 2011074524 A1 WO2011074524 A1 WO 2011074524A1 JP 2010072348 W JP2010072348 W JP 2010072348W WO 2011074524 A1 WO2011074524 A1 WO 2011074524A1
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- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/46—Ruthenium, rhodium, osmium or iridium
- B01J23/464—Rhodium
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- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/42—Platinum
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/46—Ruthenium, rhodium, osmium or iridium
- B01J23/462—Ruthenium
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/03—Preparation from chlorides
- C01B7/05—Preparation from ammonium chloride
- C01B7/055—Preparation of hydrogen chloride from ammonium chloride
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/09—Bromine; Hydrogen bromide
- C01B7/093—Hydrogen bromide
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/13—Iodine; Hydrogen iodide
- C01B7/135—Hydrogen iodide
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/026—Preparation of ammonia from inorganic compounds
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/16—Halides of ammonium
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/133—Renewable energy sources, e.g. sunlight
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- 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
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the present invention relates to a method for synthesizing ammonia.
- ammonia synthesis As for ammonia synthesis, the Harbor Bosch method has been established in the past, and it is notable that it became a raw material for fertilizer and became the driving force for agricultural development as well as the great development of the chemical industry.
- 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 As an industrial catalyst, a catalyst is used in which the catalytic performance of iron is improved by adding alumina and potassium oxide to iron (see Non-Patent Document 1).
- a Ru-based catalyst As another technique, there is an example in which a Ru-based catalyst is proposed (see Patent Document 1).
- the latest issue is the need for technology to prevent resource depletion and global warming.
- the above-mentioned Harbor Bosch method uses so-called fossil resources as raw materials, and is a high-temperature and high-pressure process. Therefore, it consumes a lot of energy in its manufacturing process and uses a large amount of resources to produce a large amount of global warming gas. To be discharged. Instead of this technology, it is desired to propose more sustainable technology by effectively utilizing limited resources on the earth.
- the present invention includes (A) a step of reacting nitrogen and hydrogen halide to obtain halogen and ammonium halide (ammonium step), and (B) halogenation of the ammonium halide obtained in the ammonium step.
- a method of synthesizing ammonia comprising a step of decomposing into hydrogen and ammonia (decomposition step).
- the present invention uses a thermochemical cycle using nitrogen and water as raw materials, it is possible to use renewable energy such as solar energy, which is advantageous in terms of energy compared to conventional techniques without requiring high pressure. It is.
- the present invention can provide a reaction process that can finally take a circulation-type reaction process and hardly generate unnecessary resources and unnecessary energy.
- the halogen produced as a by-product during the ammonia synthesis which is the first invention, is regenerated into a hydrogen halide.
- Any method can be used as long as it regenerates halogen to hydrogen halide, and preferred methods include the following methods.
- halogen is chlorine, it can be performed in one step.
- a step of regenerating the interposed substance can be used (D). Specifically, when sulfur dioxide (SO 2 ) is used as the intervening substance, the sulfuric acid obtained in the step (C-2) (H 2 SO 4 step) is converted into oxygen (O 2 ), sulfur dioxide ( SO 2 ) and a step of decomposing into water (H 2 O) (SO 2 step) are performed.
- the third invention uses the hydrogen halide obtained in the hydrogen halide regeneration step as the hydrogen halide in the ammoniumation step as a circulation step related to the first invention and the second invention (step (E)). and, the SO 2 sulfur dioxide obtained in step (SO 2) and water at least one of (H 2 O), the H 2 SO 4 raw material becomes sulfur dioxide step (SO 2) or water (H 2 O ) (Step (F)).
- the by-product compound can be recycled in addition to the target product, and resources can be effectively utilized.
- the third invention will be described as appropriate in the first invention and the second invention.
- the ammoniumation step (A) of the present invention is an ammonium halide synthesis reaction by a reaction between molecular nitrogen and hydrogen halide, and is a novel reaction that has not been known so far.
- the establishment of a chemical cycle is a completely new idea.
- the elementary reaction of the hydrogen halide regeneration step (C) and the intermediary material regeneration step (D) can be performed by, for example, the IS method (for example, “JAERI-Review” 94-006, edited and published by the Japan Atomic Energy Research Institute, November 1994.
- the feature of the present invention is that the novel ammoniumation process of (A) is used as a core reaction to link a thermochemical cycle with other reactant regeneration processes. It is to complete.
- the first invention comprises an ammoniumation step and a decomposition step. First, the ammonium process will be described.
- nitrogen pure nitrogen is preferable, but it can be used including a gas inert to the reaction such as helium or argon, or water vapor.
- the hydrogen halide may be any as long as it is composed of hydrogen and halogen, but is preferably hydrogen iodide.
- the amount of nitrogen and hydrogen halide is preferably 5 to 90% by volume, more preferably 10 to 80% by volume, and preferably 10 to 95% by volume of hydrogen halide in the reaction gas of the ammoniumation step. More preferably, it is 20 to 90% by volume.
- the reaction temperature is preferably 50 to 250 ° C, more preferably 100 to 200 ° C.
- the reaction pressure is preferably 0.05 to 2.0 MPa, more preferably 0.1 to 1.0 MPa.
- the catalyst is not particularly limited, but a catalyst mainly composed of iron oxide and containing aluminum oxide or potassium oxide or a metal-supported catalyst is preferable. Transition metals and noble metals can be used as the catalyst metal, and platinum, ruthenium, rhodium, palladium, iridium and the like can be exemplified. These metals can be used alone or in combination of two or more.
- the carrier include alumina, titania, zirconia, activated carbon and the like.
- a catalyst in which a metal containing a noble metal such as platinum supported on alumina, rhodium or ruthenium catalyst is supported on a carrier that does not easily react with halogen is particularly preferable.
- the amount of metal supported is not particularly limited and may be supported in an amount effective for the production of ammonium halide.
- the total mass of the ammonium halide production catalyst is preferably 100 to 30% by mass, and more preferably 1 to 30% by mass.
- the content is preferably 2 to 20% by mass.
- the separation method is not particularly limited, and for example, a method such as thermal decomposition can be employed.
- water can also be added, and the addition amount is preferably 0 to 70% by volume, more preferably 0 to 60% by volume, based on the entire reaction gas.
- the decomposition step is a step of decomposing the ammonium halide to obtain hydrogen halide and ammonia.
- 100% by volume of ammonium halide can be used as a reaction gas, but an inert gas such as argon or a gas having a weak oxidizing power such as nitrogen, hydrogen, or water vapor is added and used as the reaction gas. Can do.
- the reaction temperature in the decomposition step is preferably 300 to 600 ° C, more preferably 400 to 550 ° C.
- the reaction pressure in this step is preferably 0.05 to 1.0 MPa, more preferably 0.1 to 0.5 MPa. It is known that hydrogen halide is decomposed by heating (see, for example, “Encyclopedia of Chemistry”, Volume 1, pp. 1019-1020, published by Kyoritsu Publishing, June 1, 1993).
- the ammonia and hydrogen halide obtained by the reaction in the decomposition step can be separated by means such as adsorption onto acid-type zeolite.
- the separated hydrogen halide can be used as a raw material for other ammonium chemical processes as well as a raw material for other chemical industries (process (E)). By recycling the raw material, effective utilization of the raw material and a sustainable reaction can be further realized.
- This step is a step (hydrogen halide regeneration step) in which the halogen obtained in the ammonium step is regenerated to hydrogen halide with water (H 2 O).
- This process is a process in which the halogen produced as a by-product according to the first invention is converted to a hydrogen halide with water (H 2 O).
- the hydrogen halide can be used for other reactions, and can also be used as a raw material of the first invention described below (step (E)).
- the waste of the raw material can be prevented as the whole process of the present invention, whereby a circulation type reaction process can be provided.
- the content of each compound in the reaction gas in the process is as follows.
- the halogen content is preferably 30 to 60% by volume, more preferably 40 to 50% by volume in the reaction gas.
- the water content is preferably 70 to 40% by volume, more preferably 60 to 50% by volume in the reaction gas.
- the total amount of halogen and water is 100% by volume.
- the reaction gas may contain other gas as long as it does not inhibit the reaction.
- sulfur dioxide (SO 2 ) can be added, and the addition amount is preferably 5 to 30 vol. With respect to a total of 100 vol% of halogen, sulfur dioxide (SO 2 ), and water (H 2 O). %, More preferably 15 to 20% by volume.
- the reaction temperature is preferably 10 to 80 ° C., more preferably 25 to 60 ° C.
- the reaction pressure is preferably 0.05 to 1.0 MPa, more preferably 0.1 to 0.2 MPa.
- the halogen content is preferably 10 to 50% by volume, more preferably 20 to 30% by volume in the reaction gas.
- the content of sulfur dioxide (SO 2 ) is preferably 10 to 50% by volume, more preferably 20 to 40% by volume in the reaction gas.
- the content of water (H 2 O) is preferably 10 to 50% by volume, more preferably 20 to 40% by volume in the reaction gas. Note that the total amount of halogen, sulfur dioxide (SO 2 ), and water (H 2 O) is 100% by volume.
- reaction gas may contain other gas such as argon or nitrogen as long as it does not inhibit the reaction.
- the content of the other gas is preferably 1 to 20% by volume, more preferably 5 to 10% by volume with respect to the total of halogen, sulfur dioxide (SO 2 ), and water (H 2 O).
- the reaction temperature is preferably 10 to 80 ° C., more preferably 20 to 60 ° C.
- the reaction pressure is preferably 0.05 to 1.0 MPa.
- the hydrogen halide can be separated by means such as distillation after separation into each layer.
- a process of regenerating the intervening substance when another substance is interposed in the step C-2 will be described. Specifically, when sulfur dioxide (SO 2 ) is used as an intervening substance, sulfuric acid (H 2 SO 4 ) obtained in the C-2 step (hydrogen halide regeneration step) is replaced with oxygen (O 2 ), A process of decomposing into sulfur dioxide (SO 2 ) and water (SO 2 process) is performed (D).
- the obtained sulfur dioxide (SO 2 ) can be used as a raw material for other chemical industries, and can also be used as a raw material for the second invention (step (F)). Further, water (H 2 O) by-produced in the step (F) can also be used as the raw material.
- a circulation type reaction process can be provided.
- the other product is oxygen (O 2 ), and a stable circulation reaction step is achieved by performing the first to third aspects of the invention.
- step (F) 100% by volume of sulfuric acid (H 2 SO 4 ) can be used, but water can also be added, and the amount added is preferably 5 to 4 with respect to sulfuric acid (H 2 SO 4 ). 20% by volume, more preferably 5-10% by volume.
- the reaction temperature is preferably 400 to 1000 ° C, more preferably 500 to 850 ° C.
- the reaction pressure is preferably 0.05 to 0.5 MPa, more preferably 0.1 to 0.2 MPa.
- Example 1 Heat to 100-200 ° C.
- Nitrogen gas is circulated in a glass reactor filled with a catalyst, and hydrogen iodide gas is supplied thereto.
- the content of nitrogen in the reaction gas was 60% by volume, and the content of hydrogen iodide gas in the reaction gas was 40% by volume.
- the reaction pressure is 0.1 MPa.
- the produced ammonium iodide is deposited as a solid at the outlet of the reactor. By cooling the reactor outlet gas to room temperature (25 ° C.), iodine can be precipitated and recovered as a solid.
- the ammonium iodide obtained in the ammoniumation step is decomposed into ammonia and hydrogen iodide by heating to 520 ° C. in an inert gas stream.
- the reaction pressure at this time is 0.1 MPa.
- the obtained ammonia-containing gas is passed through a column packed with USY zeolite to adsorb and separate ammonia.
- the mixture After completion of the reaction, the mixture is allowed to stand until it is separated into two liquid layers, and an aqueous sulfuric acid solution is recovered from the upper layer, and an aqueous hydrogen iodide solution is recovered from the lower layer.
- the sulfuric acid (H 2 SO 4 ) obtained in the H 2 SO 4 step is dehydrated and then sent to a reactor charged with a catalyst heated to 500 to 800 ° C., and thermally decomposed to recover SO 2 .
- the reaction pressure at this time is 0.1 MPa.
- a noble metal supported catalyst such as platinum or palladium or iron oxide is used.
- Example 2 An ammoniumation step was performed according to the following procedure, and ammonium iodide was synthesized by a reaction between hydrogen iodide and nitrogen.
- a glass autoclave (TEM-V100 manufactured by Pressure Glass Industrial Co., Ltd.) having an internal volume of 100 mL was used.
- the catalyst was placed in a stainless steel cage fixed to a thermometer protective tube inside the reactor.
- As a catalyst 1.25 g of a catalyst in which 5% by mass of platinum / ruthenium (atomic ratio 1: 2) was supported on ⁇ -alumina was used.
- the reactor was charged with 10 mL of a 57% by mass aqueous hydrogen iodide solution so as not to come into contact with the catalyst, and the gas phase portion was sufficiently replaced with nitrogen, and then the reactor was heated to 150 ° C. to generate hydrogen iodide vapor, Reacted with nitrogen.
- the composition of the reaction charge gas was 21% by volume of nitrogen, 26% by volume of hydrogen iodide, and 53% by volume of water vapor.
- the reaction was carried out for 60 minutes after the temperature was raised. The pressure during the reaction was 0.7 MPa.
- the produced ammonia was 1.0 ⁇ 10 ⁇ 5 mol.
- Nitrogen in the reaction gas was 4 ⁇ 10 ⁇ 3 mol, and hydrogen iodide in the reaction gas was 7.6 ⁇ 10 ⁇ 2 mol.
- Nitrogen and hydrogen iodide necessary for producing 1 mol of ammonia were 0.5 mol and 3 mol, respectively, and the conversion rates of nitrogen and hydrogen iodide were 0.125% and 0.04%, respectively.
- Example 3 The reaction was performed in the same manner as in Example 2 except that the catalyst used was a catalyst in which 5% by mass of ruthenium was supported on ⁇ -alumina, and the reaction temperature was 180 ° C. The amount of catalyst used and the results are shown in Table 1.
- Example 4 The reaction was carried out in the same manner as in Example 3 except that the catalyst used was changed to a catalyst in which 5% by mass of rhodium was supported on ⁇ -alumina. The amount of catalyst used and the results are shown in Table 1.
- Example 5 The reaction was carried out in the same manner as in Example 3 except that the catalyst used was changed to a catalyst in which 5% by mass of rhodium / ruthenium (atomic ratio 2: 1) was supported on ⁇ -alumina. The amount of catalyst used and the results are shown in Table 1.
- Example 6 The reaction was carried out in the same manner as in Example 3 except that the catalyst used was changed to a catalyst in which 5% by mass of palladium / ruthenium (atomic ratio 2: 1) was supported on ⁇ -alumina. The amount of catalyst used and the results are shown in Table 1.
- Example 7 The reaction was performed in the same manner as in Example 3 except that the catalyst used was changed to a catalyst in which 5% by mass of platinum was supported on ⁇ -alumina. The amount of catalyst used and the results are shown in Table 1.
- the present invention proposes a novel ammonia synthesis method that hardly generates unnecessary resources and unnecessary energy, and ammonia can be used as a basic raw material and a new fuel in the chemical industry. Similarly, by-produced hydrogen halide, sulfuric acid and the like can be used as raw materials for the chemical industry.
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Abstract
Description
当該アンモニウム化工程で得られたハロゲンを、水(H2O)に含まれる水素を用いてハロゲン化水素を再生する工程(ハロゲン化水素再生工程)を行うものである。この時、水(H2O)に含まれる酸素は酸素分子となる。
ハロゲンが臭素あるいはヨウ素の場合は、他の物質を介在させることが好ましい。具体的には、ハロゲンに二酸化硫黄(SO2)と水(H2O)とを加え、ハロゲン化水素と硫酸(H2SO4)とを得る工程を行うものである。
第一発明は、アンモニウム化工程と分解工程とから構成されるものである。まず、アンモニウム化工程について説明する。
まず、(C-1)を説明した後(C-2)を説明する。
本工程は、当該アンモニウム化工程で得られたハロゲンを、水(H2O)によってハロゲン化水素に再生する工程(ハロゲン化水素再生工程)である。
ハロゲンが臭素あるいはヨウ素の場合は、ハロゲンに二酸化硫黄(SO2)と水(H2O)とを加え、ハロゲン化水素と硫酸(H2SO4)とを得る工程(H2SO4工程)を行うことが好ましい。当該ハロゲンの含有量は、反応ガス中に好ましくは10~50容量%、より好ましくは20~30容量%である。二酸化硫黄(SO2)の含有量は、反応ガス中に好ましくは10~50容量%、より好ましくは20~40容量%である。また、水(H2O)の含有量は、反応ガス中に好ましくは10~50容量%、より好ましくは20~40容量%である。なお、ハロゲン、二酸化硫黄(SO2)、水(H2O)は合計で100容量%である。
当該C-2工程で他の物質を介在させた場合の、当該介在物質を再生する工程を説明する。具体的には、介在する物質として二酸化硫黄(SO2)を用いた場合、当該C-2工程(ハロゲン化水素再生工程)で得られた硫酸(H2SO4)を酸素(O2)、二酸化硫黄(SO2)、および水に分解する工程(SO2工程)を行うものである(D)。得られた二酸化硫黄(SO2)は、他の化学工業の原料に使用することができる他、第二発明の原料として用いることもできる((F)工程)。また、(F)工程で副生する水(H2O)も、当該原料として用いることができる。第二発明の原料として用いたときは、本発明の工程全体として原料の無駄を防止することができることから、循環型の反応工程を提供することができる。当該(F)工程において、他の生成物は酸素(O2)であり、当該第一から第三の発明までを行うことで、安定的な循環反応工程が達成される。
(アンモニウム化工程)
100℃~200℃に加熱する。触媒が充填されたガラス製反応器中に窒素ガスを流通させ、そこにヨウ化水素ガスを供給する。反応ガス中の窒素の含有量は60容量%、反応ガス中のヨウ化水素ガスの含有量は40容量%であった。反応圧力は0.1MPaである。生成したヨウ化アンモニウムは、反応器出口に固体となって析出する。反応器出口ガスは、室温(25℃)まで冷却することにより、ヨウ素が固体となって析出し回収することができる。
アンモニウム化工程で得られたヨウ化アンモニウムを、不活性ガス気流下、520℃に加熱することでアンモニアとヨウ化水素とに分解する。この際の反応圧力は0.1MPaである。得られたアンモニア含有ガスを、USYゼオライトを充填したカラムに流通させてアンモニアを吸着分離する。
攪拌機付きの反応器に水を仕込み、アンモニウム工程で回収されたヨウ素を分散させる。室温(25℃)で、SO2ガスを撹拌しながら吹き込み反応させた。反応液中のヨウ素の含有量は70質量%である。また、反応温度は80℃、反応圧力は0.1MPaである。
H2SO4工程で得られる硫酸(H2SO4)は、脱水した後、500~800℃に加熱した触媒を充填した反応器へ送り、熱分解してSO2を回収する。この際の反応圧力は0.1MPaである。触媒としては、白金・パラジウムなどの貴金属担持触媒や酸化鉄を用いる。
以下の手順でアンモニウム化工程を行い、ヨウ化水素と窒素との反応でヨウ化アンモニウムを合成した。
用いる触媒をγ-アルミナにルテニウムを5質量%担持した触媒に変え、反応温度を180℃としたこと以外は、実施例2と同様に反応を行った。使用触媒量と結果とを表1に示した。
用いる触媒をγ-アルミナにロジウムを5質量%担持した触媒に変えたこと以外は、実施例3と同様に反応を行った。使用触媒量と結果とを表1に示した。
用いる触媒をγ-アルミナにロジウム・ルテニウム(原子比2:1)を5質量%担持した触媒に変えたこと以外は、実施例3と同様に反応を行った。使用触媒量と結果とを表1に示した。
用いる触媒をγ-アルミナにパラジウム・ルテニウム(原子比2:1)を5質量%担持した触媒に変えたこと以外は実施例3と同様に反応を行った。使用触媒量と結果とを表1に示した。
用いる触媒をγ-アルミナに白金を5質量%担持した触媒に変えたこと以外は実施例3と同様に反応を行った。使用触媒量と結果とを表1に示した。
Claims (9)
- (A)窒素とハロゲン化水素とを反応させハロゲンとハロゲン化アンモニウムとを得る工程(アンモニウム化工程)と、
(B)当該アンモニウム化工程で得られたハロゲン化アンモニウムを、ハロゲン化水素とアンモニアとに分解する工程(分解工程)と、
を含むことを特徴とする、アンモニアの合成方法。 - さらに、(C)当該ハロゲンをハロゲン化水素に再生する工程を含むことを特徴とする、請求項1に記載のアンモニアの合成方法。
- 当該ハロゲン化水素に再生する工程は、(C-1)当該アンモニウム化工程で得られたハロゲンに、水を加えハロゲン化水素を得る工程(ハロゲン化水素再生工程)であることを特徴とする、請求項2に記載のアンモニアの合成方法。
- 当該ハロゲン化水素に再生する工程は、(C-2)当該アンモニウム化工程で得られたハロゲンに、二酸化硫黄と水とを加え、ハロゲン化水素と硫酸とを得る工程(H2SO4工程)であることを特徴とする、請求項2に記載のアンモニアの合成方法。
- 当該H2SO4工程に次いで、(D)当該H2SO4工程で得られた硫酸を、酸素、二酸化硫黄、および水に分解する工程(SO2工程)を行うことを特徴とする、請求項4に記載のアンモニアの合成方法。
- 当該ハロゲン化水素再生工程で得られた当該ハロゲン化水素を、当該アンモニウム化工程におけるハロゲン化水素として用いることを特徴とする、請求項3に記載のアンモニアの合成方法。
- 当該SO2工程において得られた二酸化硫黄および水の少なくとも一方を、当該H2SO4工程において用いることを特徴とする、請求項5に記載のアンモニアの合成方法。
- 当該ハロゲンがヨウ素であることを特徴とする、請求項1~7のいずれか1項に記載のアンモニアの合成方法。
- 当該アンモニウム化工程に用いる触媒が金属担持触媒であることを特徴とする、請求項1~8のいずれか1項に記載のアンモニアの合成方法。
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AU2010331314A AU2010331314A1 (en) | 2009-12-14 | 2010-12-13 | Process for synthesis of ammonia |
EP10837550.2A EP2514719A4 (en) | 2009-12-14 | 2010-12-13 | PROCESS FOR SYNTHESIS OF AMMONIA |
US13/515,336 US20120258033A1 (en) | 2009-12-14 | 2010-12-13 | Method for synthesizing ammonia |
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EP (1) | EP2514719A4 (ja) |
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JP2015054803A (ja) * | 2013-09-13 | 2015-03-23 | 国立大学法人東京農工大学 | 熱化学サイクルによるアンモニア合成方法 |
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JP2015120118A (ja) | 2013-12-24 | 2015-07-02 | 株式会社デンソー | アンモニア合成触媒 |
CN114789053A (zh) * | 2022-05-06 | 2022-07-26 | 福州大学 | 一种钌基温和合成氨催化剂及其制备方法和应用 |
CN117163919B (zh) * | 2023-11-02 | 2024-02-23 | 浙江百能科技有限公司 | 一种基于氨的制氢系统和方法 |
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- 2010-12-13 JP JP2010276967A patent/JP5660493B2/ja not_active Expired - Fee Related
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EP2514719A1 (en) | 2012-10-24 |
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JP2011144102A (ja) | 2011-07-28 |
JP5660493B2 (ja) | 2015-01-28 |
AU2010331314A1 (en) | 2012-06-28 |
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