WO2023090644A1 - Catalyseur au ruthénium pour réaction de décomposition d'ammoniac, son procédé de préparation et procédé de production d'hydrogène l'utilisant - Google Patents

Catalyseur au ruthénium pour réaction de décomposition d'ammoniac, son procédé de préparation et procédé de production d'hydrogène l'utilisant Download PDF

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WO2023090644A1
WO2023090644A1 PCT/KR2022/015241 KR2022015241W WO2023090644A1 WO 2023090644 A1 WO2023090644 A1 WO 2023090644A1 KR 2022015241 W KR2022015241 W KR 2022015241W WO 2023090644 A1 WO2023090644 A1 WO 2023090644A1
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ruthenium
decomposition reaction
ammonia decomposition
catalyst
carrier
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Korean (ko)
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박은덕
김한봄
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아주대학교산학협력단
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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
    • 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
    • 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
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • B01J21/04—Alumina
    • 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
    • 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
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/0201—Impregnation
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/08—Heat treatment
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/16—Reducing
    • 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
    • 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
    • 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
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis

Definitions

  • the present invention relates to a ruthenium catalyst for ammonia decomposition reaction capable of producing hydrogen from ammonia, a method for preparing the same, and a method for producing hydrogen using the same.
  • Hydrogen itself is a very clean fuel, and when burned, only water is produced without generating carbon dioxide, and when used as a fuel for a fuel cell, electricity and heat can be produced simultaneously with high efficiency.
  • hydrogen cannot exist alone in nature and exists in nature in a form combined with other elements, hydrogen can be widely used as a fuel only when technology development for extracting, transporting and storing hydrogen from them is accompanied.
  • Ammonia is a hydrogen source that can stably exist by combining hydrogen and nitrogen, and can be industrially produced in large quantities by the Haber-Bosch method, and has advantages in transportation and storage because it is easily liquefied. In addition, it has an eco-friendly advantage because only harmless nitrogen and hydrogen are produced during ammonia decomposition.
  • the ammonia decomposition reaction is an endothermic reaction in which 2 moles of ammonia are produced as 3 moles of hydrogen, as shown in Scheme 1 below.
  • the decomposition reaction of ammonia is thermodynamically capable of converting more than 99% of ammonia at 400 ° C and 1 atm, but in reality, it is known that ammonia is decomposed at 500 to 900 ° C due to a reaction kinetic barrier.
  • ruthenium and nickel show high catalytic activity for the ammonia decomposition reaction.
  • the ruthenium catalyst shows the highest activity for ammonia decomposition when used with a carbon nanotube (CNT) support, but carbon nanotubes (CNT) are expensive to produce and inefficient in large-scale production processes, so ammonia decomposition There are limits to its use in reactions.
  • One object of the present invention is to increase the rate of hydrogen production in a relatively low temperature range by including an active ruthenium component supported on an alumina carrier in an alpha crystal phase so that the dispersion degree is 2.0 to 20%, as measured through selective chemical adsorption of carbon monoxide. It is to provide a ruthenium catalyst capable of reducing the amount of ruthenium used while improving.
  • Another object of the present invention is to provide a method for preparing the ruthenium catalyst.
  • Another object of the present invention is to provide a method for generating hydrogen from ammonia using the ruthenium catalyst.
  • a ruthenium catalyst for ammonia decomposition reaction is a catalyst for promoting hydrogen production through ammonia decomposition reaction, and includes a support and a ruthenium active component supported on the surface of the support, wherein the ruthenium active component
  • the dispersion of ruthenium measured through selective chemisorption of carbon monoxide on the surface of the carrier may be 2.0% to 20%.
  • the carrier may include an alpha alumina material.
  • the ruthenium active ingredient has a dispersion of 2.7% of ruthenium measured through selective chemical adsorption of carbon monoxide on the surface of the carrier. More than 16% can be supported.
  • the ruthenium active ingredient has a dispersion of 3.1% of ruthenium measured through selective chemisorption of carbon monoxide on the surface of the carrier. more than 12% It can be supported below.
  • a method for preparing a ruthenium catalyst for ammonia decomposition reaction includes a first step of impregnating a carrier with a ruthenium precursor compound; A second step of drying the carrier impregnated with the ruthenium precursor compound; and a third step of forming a ruthenium metal phase on the surface of the carrier by reducing the ruthenium precursor compound in the carrier on which the dried ruthenium precursor compound is supported, wherein the ruthenium metal phase forms a selective chemical reaction of carbon monoxide on the surface of the carrier. It may be formed such that the dispersion of ruthenium measured through adsorption is 2.0% or more and 20% or less.
  • the carrier may include an alpha alumina material.
  • the ruthenium precursor compound may include one or more compounds selected from the group consisting of a ruthenium carbonyl compound, ruthenium nitride, and ruthenium chloride.
  • the carrier impregnated with the ruthenium precursor compound in the second step, may be dried under a normal pressure or reduced pressure condition less than normal pressure and a temperature condition of 50 to 250°C.
  • the ruthenium metal phase is formed on the surface of the support by heat-treating the support on which the ruthenium precursor compound is supported at a temperature of 100° C. or more and 700° C. or less in a reducing gas atmosphere containing hydrogen. can do.
  • the reducing agent in the third step, after mixing the carrier supported with the ruthenium precursor compound and a reducing agent in a single or mixed solvent selected from the group consisting of water, acetone, cyclohexane, hexane and decane, the reducing agent It is possible to form the ruthenium metal phase on the surface of the support by reducing the ruthenium precursor compound by using.
  • a method for generating hydrogen from ammonia includes a first step of injecting a fuel gas containing ammonia into an inlet of a tubular reactor filled with a ruthenium catalyst for the ammonia decomposition reaction; and selectively recovering hydrogen from gases discharged through an outlet of the tubular reactor.
  • the temperature inside the tubular reactor during the first step may be adjusted to 200 ° C or more and 700 ° C or less.
  • the temperature inside the tubular reactor may be adjusted to 550° C. or more and 600° C. or less.
  • the ammonia decomposition ruthenium catalyst for hydrogen production of the present invention is characterized in that the support is formed of alpha alumina and the dispersion of ruthenium measured through selective chemisorption of carbon monoxide is about 2.0% to 20%, and is relatively low-temperature In a wide temperature range, the ammonia decomposition reaction of Scheme 1 may proceed predominantly.
  • FIG. 1 is a flowchart illustrating a method for preparing a ruthenium catalyst for ammonia decomposition reaction according to an embodiment of the present invention.
  • Figure 2 is a graph showing ammonia conversion (NH 3 Conversion) according to temperature in the reaction using the ruthenium catalyst of Comparative Examples 1 to 4 and Example 1.
  • the ruthenium catalyst for ammonia decomposition reaction for generating hydrogen is a catalyst that promotes the reaction of Reaction Formula 1 below, and may include a carrier and a ruthenium active component supported on the carrier.
  • the carrier may include alpha alumina ( ⁇ -Al 2 O 3 ).
  • Alumina has a stronger interaction with metal than other carriers, so that metal can be widely dispersed and supported.
  • metal catalyst it is not easily sintered at a high temperature and may have advantages of high thermal conductivity and low cost.
  • the support is formed of alpha alumina, it can be manufactured to have various surface areas and shapes by controlling the conditions of the manufacturing process.
  • the ruthenium active ingredient may be supported on the surface of the carrier and may include a ruthenium metal phase.
  • the ruthenium active component in the ruthenium catalyst for the ammonia decomposition reaction, may be supported on the surface of the carrier with a degree of dispersion measured through selective chemical adsorption of carbon monoxide at about 2.0% to 20%.
  • a catalyst having a dispersion of the ruthenium active component of less than 2.0% may use a large amount of expensive ruthenium to exhibit low-temperature catalytic activity, resulting in an increase in cost of the catalyst.
  • the degree of dispersion of the ruthenium active component exceeds 20%, low-temperature activity of the ruthenium catalyst for the ammonia decomposition reaction may not appear.
  • the ruthenium active ingredient may be supported on the surface of the carrier with a ruthenium dispersion of about 2.7% to about 16%, as measured through selective chemical adsorption of carbon monoxide.
  • the ruthenium active component may be supported on the alpha-alumina carrier in an amount of about 0.5 to 3.0 wt% based on the total weight of the ruthenium catalyst.
  • the ruthenium active ingredient may be formed through heat treatment of a ruthenium precursor compound.
  • the ruthenium precursor compound may be a ruthenium carbonyl compound, ruthenium nitride, ruthenium chloride, or the like, and a ruthenium metal phase may be induced from the precursor compound through a heat treatment process under a reducing atmosphere. At this time, some of the carbon, nitrogen, and chlorine components of the ruthenium precursor compound may remain in the ruthenium catalyst for the ammonia decomposition reaction.
  • the support is formed of alpha alumina, and the ruthenium active component is supported on the support so that the dispersion of ruthenium measured through selective chemical adsorption of carbon monoxide is about 2.0% to 20%, In a relatively low temperature range, the ammonia decomposition reaction of Scheme 1 may proceed predominantly.
  • FIG. 1 is a flowchart illustrating a method for preparing a ruthenium catalyst for ammonia decomposition reaction according to an embodiment of the present invention.
  • a method for preparing a ruthenium catalyst for ammonia decomposition reaction includes a first step (S110) of impregnating a carrier with a ruthenium precursor compound; A second step (S120) of drying the carrier impregnated with the ruthenium precursor compound; and a third step ( S130 ) of forming a ruthenium metal phase on the surface of the carrier by reducing the ruthenium precursor compound in the carrier on which the dried ruthenium precursor compound is supported.
  • the ruthenium precursor compound may be dissolved in a solvent and then the alpha-alumina carrier may be mixed with the carrier to impregnate the carrier with the ruthenium precursor compound.
  • deionized water, ethanol, etc. may be used as the solvent, and a ruthenium carbonyl compound, ruthenium nitride, ruthenium chloride, or the like may be used as the ruthenium precursor compound.
  • the ruthenium precursor compound and the alpha alumina may be supported on the surface of the support so that the ruthenium dispersion degree measured through selective chemical adsorption of carbon monoxide is about 2.0% to 20%.
  • the mixing ratio of the carrier can be adjusted.
  • the drying temperature, pressure, drying atmosphere, etc. of the carrier impregnated with the ruthenium precursor compound are not particularly limited.
  • the carrier impregnated with the ruthenium precursor compound may be dried under normal pressure or reduced pressure conditions below normal pressure and under a temperature condition of about 50 to 250 ° C.
  • the drying process is carried out in an oxidizing atmosphere containing oxygen or hydrogen. It may be performed in a reducing atmosphere including the like.
  • a reduction treatment may be performed on the support carrying the ruthenium precursor compound to form a ruthenium metal phase, which is a catalytically active component, on the surface of the support.
  • the catalyst of the present invention can have more improved catalytic activity in the ammonia decomposition reaction.
  • a method of forming the ruthenium metal phase by reducing the ruthenium precursor compound on the surface of the carrier is not particularly limited.
  • the ruthenium precursor compound may be reduced through a vapor phase reduction method or a liquid phase reduction method to form the ruthenium metal phase.
  • the ruthenium metal phase is formed from the ruthenium precursor compound using the vapor phase reduction method
  • the ruthenium metal phase is formed on the surface of the carrier by heat-treating the carrier supported with the ruthenium precursor compound in a reducing gas atmosphere containing hydrogen or the like. can do.
  • the heat treatment may be performed at 100° C. or higher, which is the minimum temperature capable of reducing ruthenium, and 700° C. or lower, which is the sublimation temperature of ruthenium.
  • the heat treatment temperature exceeds 700° C., a problem of loss of ruthenium may occur, and when it is less than 100° C., a significant amount of ruthenium is not reduced, and thus, a problem of lowering the content of the ruthenium metal phase may occur.
  • the heat treatment may be performed at a temperature of about 150 to 500 ° C. in a reducing atmosphere.
  • the ruthenium metal phase is formed from the ruthenium precursor compound using the liquid phase reduction method, after adding a carrier carrying the ruthenium precursor compound and a reducing agent in a solvent, the ruthenium precursor compound is reduced using the reducing agent to form the ruthenium precursor compound.
  • a metal phase can be formed.
  • the solvent is not particularly limited, and water, acetone, cyclohexane, hexane, decane, and the like can be used.
  • the reducing agent may be any compound capable of generating hydrogen.
  • alcohol compounds such as sodium borohydride (NaBH4) and ethylene glycol, aldehyde compounds such as formaldehyde, and the like may be used.
  • the reduction temperature, pressure, etc. can be variously controlled under the condition that the liquid phase is maintained.
  • the reduction temperature may be set to about 0 to 100 °C.
  • the method for manufacturing a ruthenium catalyst according to an embodiment of the present invention includes a fourth step of performing heat treatment in an oxidizing atmosphere containing oxygen after the second step (S120) or the third step (S130) ( (not shown) may further include, and when the heat treatment is performed in the oxidizing atmosphere after the third step (S130), the step of activating the ruthenium catalyst through the step of heat treatment in a reducing atmosphere after the fourth step is additionally performed can do.
  • a method for generating hydrogen from ammonia includes injecting a fuel gas containing ammonia into an inlet of a tubular reactor filled with a ruthenium catalyst for the ammonia decomposition reaction; and selectively recovering hydrogen from a reaction gas discharged through an outlet of the tubular reactor.
  • the temperature inside the tubular reactor may be adjusted to about 200° C. or higher and 700° C. or lower through a heater disposed outside the tubular reactor.
  • a ruthenium catalyst was prepared by activating the ruthenium precursor catalyst through a vapor phase reduction method in which heat treatment was performed at about 350° C. under a hydrogen atmosphere.
  • a ruthenium catalyst was prepared in the same manner as in Example 1, except that the amount of 1.5 wt% ruthenium nitrosyl nitrate (Ru(NO)(NO 3 ) 3 ) aqueous solution was 18 ml.
  • a ruthenium catalyst was prepared in the same manner as in Example 1, except that the amount of 1.5 wt% ruthenium nitrosyl nitrate (Ru(NO)(NO 3 ) 3 ) aqueous solution was 15 ml.
  • a ruthenium catalyst was prepared in the same manner as in Example 1, except that 12 ml of a 1.5 wt% ruthenium nitrosyl nitrate (Ru(NO)(NO 3 ) 3 ) aqueous solution was used.
  • a ruthenium catalyst was prepared in the same manner as in Example 1, except that the amount of 1.5 wt% ruthenium nitrosyl nitrate (Ru(NO)(NO 3 ) 3 ) aqueous solution was 9.0 ml.
  • a ruthenium catalyst was prepared in the same manner as in Example 1, except that the amount of 1.5 wt% ruthenium nitrosyl nitrate (Ru(NO)(NO 3 ) 3 ) aqueous solution was 4.1 ml.
  • a ruthenium catalyst was prepared in the same manner as in Example 1, except that the amount of 1.5 wt% ruthenium nitrosyl nitrate (Ru(NO)(NO 3 ) 3 ) aqueous solution was 3.0 ml.
  • a ruthenium catalyst was prepared in the same manner as in Example 1, except that 1.8 ml of a 1.5 wt% ruthenium nitrosyl nitrate (Ru(NO)(NO 3 ) 3 ) aqueous solution was used.
  • Ru(NO)(NO 3 ) 3 ruthenium nitrosyl nitrate
  • a ruthenium catalyst was prepared in the same manner as in Example 1, except that the amount of 1.5 wt% ruthenium nitrosyl nitrate (Ru(NO)(NO 3 ) 3 ) aqueous solution was 65 ml.
  • a ruthenium catalyst was prepared in the same manner as in Example 1, except that the amount of 1.5 wt% ruthenium nitrosyl nitrate (Ru(NO)(NO 3 ) 3 ) aqueous solution was 44 ml.
  • a ruthenium catalyst was prepared in the same manner as in Example 1, except that the amount of 1.5 wt% ruthenium nitrosyl nitrate (Ru(NO)(NO 3 ) 3 ) aqueous solution was 31 ml.
  • a ruthenium catalyst was prepared in the same manner as in Example 1, except that the prepared ruthenium precursor catalyst was heat-treated in an air atmosphere at 300 °C.
  • a ruthenium catalyst was prepared in the same manner as in Example 1, except that the amount of 1.5 wt% ruthenium nitrosyl nitrate (Ru(NO)(NO 3 ) 3 ) aqueous solution was 0.59 ml.
  • the ruthenium catalysts of Examples 1 to 8 and Comparative Examples 1 to 9 were powdered and charged into a fixed-bed tubular reactor.
  • a mixed gas having a composition of 25% ammonia (NH 3 ), 70% helium (He), and 5% methane (CH 4 ) based on the number of moles flows at normal pressure, and then the temperature is increased at a rate of 0.33 °C / min while The composition of the gas stream at the outlet was analyzed.
  • the total flow rate of the mixed gas was fixed at 100 ml per minute, and the amount of catalyst used was fixed at 0.1 g.
  • the ruthenium catalysts of Examples 1 to 8 and Comparative Examples 1 to 9 were powdered, filled with 0.1 g in an adsorption tube (U-shaped quartz tube), and activated through a vapor phase reduction method in which heat treatment was performed at about 350 ° C. under a hydrogen atmosphere, and then the temperature was lowered and pulsed a mixed gas mixed with 10 mol% of carbon monoxide and 90 mol% of helium at 35° C., and the measurement was performed until the ruthenium catalyst was saturated with the mixed gas.
  • One molecule of adsorbed carbon monoxide is regarded as having formed a chemical bond with one atom on the ruthenium surface, and the degree of dispersion is calculated.
  • a chemical adsorption analyzer Autochem 2920, Micromeritics
  • TCD thermal conductivity detector
  • Tables 1 and 2 show the results of measuring the range of hydrogen production rates at a reaction temperature of 400° C. according to the degree of dispersion of the ruthenium catalysts of Examples 1 to 8 and Comparative Examples 1 to 9.
  • Figure 2 is a graph showing the results of measuring the ammonia conversion rate according to temperature in the reaction using the ruthenium catalyst of Comparative Examples 1 to 4 and Example 1.
  • the hydrogen generation rate is highest when the catalyst of Example 1 is applied. That is, among alumina supports having various crystalline phases, it can be seen that the case in which alpha-alumina is used as the support is most preferable.
  • the catalysts of Examples 2 to 8 have high hydrogen production rates (mol/g Ru /min). can know This means that the catalysts of Examples 2 to 8 are excellent in ammonia decomposition ability.
  • the dispersion degree of the ruthenium catalyst supported on the alpha-alumina support is 2.0% or more and 20% or less, preferably 2.7% or more and 16% or less, more preferably 3.1% or more and 12% or less, or 8% or more 12% or more. % or less, it can be seen that it has excellent ammonia decomposition ability in a low temperature range.

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Abstract

L'invention concerne un catalyseur au ruthénium favorisant une réaction de décomposition de l'ammoniac pour la production d'hydrogène. Le catalyseur au ruthénium comprend un support alpha-alumine ; et un ingrédient actif au ruthénium supporté sur la surface du support, l'ingrédient actif au ruthénium ayant une dispersité de ruthénium de 2,0 à 20 %, mesurée par chimisorption sélective de monoxyde de carbone sur la surface du support.
PCT/KR2022/015241 2021-11-16 2022-10-11 Catalyseur au ruthénium pour réaction de décomposition d'ammoniac, son procédé de préparation et procédé de production d'hydrogène l'utilisant WO2023090644A1 (fr)

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KR1020210157465A KR102697807B1 (ko) 2021-11-16 2021-11-16 암모니아 분해 반응용 루테늄 촉매, 이의 제조 방법 및 이를 이용하여 수소를 생산하는 방법
KR10-2021-0157465 2021-11-16

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JPH0884910A (ja) * 1994-07-21 1996-04-02 Japan Pionics Co Ltd アンモニアの分解方法
JP2016159209A (ja) * 2015-02-27 2016-09-05 国立研究開発法人産業技術総合研究所 アンモニア分解触媒及び該触媒の製造方法並びに該触媒を用いたアンモニアの分解方法
JP2016198720A (ja) * 2015-04-09 2016-12-01 国立大学法人宇都宮大学 アンモニア分解触媒、アンモニア分解触媒の製造方法、水素の製造方法及び水素の製造装置
WO2019188219A1 (fr) * 2018-03-26 2019-10-03 昭和電工株式会社 Catalyseur de décomposition d'ammoniac et procédé de sa production, et procédé de production de gaz d'hydrogène

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AU2002315873A1 (en) * 2002-06-24 2004-01-06 Tanaka Kikinzoku Kogyo K.K. Catalyst for selective oxidation of carbon monoxide in reformed gas

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Publication number Priority date Publication date Assignee Title
JPH0884910A (ja) * 1994-07-21 1996-04-02 Japan Pionics Co Ltd アンモニアの分解方法
JP2016159209A (ja) * 2015-02-27 2016-09-05 国立研究開発法人産業技術総合研究所 アンモニア分解触媒及び該触媒の製造方法並びに該触媒を用いたアンモニアの分解方法
JP2016198720A (ja) * 2015-04-09 2016-12-01 国立大学法人宇都宮大学 アンモニア分解触媒、アンモニア分解触媒の製造方法、水素の製造方法及び水素の製造装置
WO2019188219A1 (fr) * 2018-03-26 2019-10-03 昭和電工株式会社 Catalyseur de décomposition d'ammoniac et procédé de sa production, et procédé de production de gaz d'hydrogène

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Title
KIM HAN BOM, PARK EUN DUCK: "Ammonia decomposition over Ru catalysts supported on alumina with different crystalline phases", CATALYSIS TODAY, ELSEVIER, AMSTERDAM, NL, vol. 411-412, 1 March 2023 (2023-03-01), AMSTERDAM, NL , pages 113817, XP093068156, ISSN: 0920-5861, DOI: 10.1016/j.cattod.2022.06.032 *

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