WO2006114108A1 - Procede de coproduction de methanol et d'ammoniac a partir de gaz naturel - Google Patents

Procede de coproduction de methanol et d'ammoniac a partir de gaz naturel Download PDF

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WO2006114108A1
WO2006114108A1 PCT/EP2005/001329 EP2005001329W WO2006114108A1 WO 2006114108 A1 WO2006114108 A1 WO 2006114108A1 EP 2005001329 W EP2005001329 W EP 2005001329W WO 2006114108 A1 WO2006114108 A1 WO 2006114108A1
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methanol
ammonia
gas
reactor
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German (de)
English (en)
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William Davey
Manfred Meyer
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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
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen; Reversible storage of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification
    • C01B3/52—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
    • 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; Reversible storage of hydrogen
    • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
    • C01B3/025—Preparation or purification of gas mixtures for ammonia synthesis
    • 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; Reversible storage of hydrogen
    • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
    • C01B3/32—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air
    • C01B3/34—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/382—Processes with two or more reaction steps, of which at least one is catalytic, e.g. steam reforming and partial oxidation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/1516—Multisteps
    • C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415—Purification by absorption in liquids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0435—Catalytic purification
    • C01B2203/044—Selective oxidation of carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/061—Methanol production
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/068—Ammonia synthesis
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
    • C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
    • C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus

Definitions

  • the invention relates to a process for coproduction, that is, for the simultaneous production of methanol and ammonia from natural gas in a single uninterrupted process flow.
  • the object of the present invention is to provide a process with which methanol and ammonia are simultaneously produced in a single integrated process.
  • 5,000 t of methanol per day can be obtained.
  • the synthesis of methanol here requires a synthesis gas composition with a stoichiometric number of 2.05 and a carbon dioxide concentration in the range between 2% and 3%.
  • the stoichiometric number S n is calculated according to the following formula:
  • the quantities [H 2 ], [CO 2 ] and [CO] represent the mole fractions of hydrogen, carbon dioxide and carbon monoxide, as present in each case in the synthesis gas.
  • the process according to the invention can produce 4,000 t of ammonia per day. Part of this can be used to make urea.
  • ammonia a mixture of hydrogen and nitrogen in the molar ratio of 3: 1 and with less than 10 ppm of components in which oxygen is contained.
  • stream 1 From natural gas (stream 1) is produced in the reactor A at a pressure of about 40 bar raw synthesis gas (stream 2).
  • the cooled and condensed gas (stream 4) is compressed in the compressor and absorber C at a pressure of 80 bar and fed to a carbon dioxide absorption column. About half of the synthesis gas is taken from the carbon dioxide absorption column in an intermediate stage, reducing the carbon dioxide concentration to about 3% (stream 5). This stream accounts for most of the methanol synthesis gas. The remainder of the gas is treated in a fine wash section of the absorption column to achieve a carbon dioxide concentration of less than 10 ppm and is then passed to the cryogenic separation D (stream 6).
  • the synthesis gas stream from the compressor and absorber C is divided into carbon monoxide added with methane (stream 7) and fed to the methanol synthesis gas (stream 8) and the ammonia synthesis gas (stream 9).
  • the committee, i. Contaminants in the form of methane, argon and carbon monoxide are returned to the fuel system to serve as fuel for the furnaces used in the process.
  • the methanol synthesis gas stream and the ammonia synthesis gas stream are converted to methanol (stream 10) and ammonia (stream 11), respectively.
  • the methanol is purified in unit E by distillation, and in unit F pure ammonia is obtained, which does not require any further purification.
  • From the compressor and absorber C carbon dioxide can be obtained for the synthesis of urea (stream 14).
  • the synthesis gas production takes place. This can include some or all of the following individual steps: desulfurization of natural gas, humidification to saturation with water vapor, preheating in an oven, pre-forming, catalytic partial oxidation with oxygen from an air separation unit and gas cooling in a waste heat boiler for increased steam generation.
  • the used CPOX reactor catalytic material oxidation itself is a conventional, cylindrical container with concave, vertically arranged boundary surfaces. In the upper end of the container, a burner or mixer is attached, through which the natural gas mixes with the water vapor. Steam and oxygen are fed via separate supply lines in the container.
  • the oxygen can, for example, be taken from the air separation unit G, in which the components oxygen (stream 13) and nitrogen (stream 15) are separated off from air (stream 12) by low-temperature desiliation.
  • the burner or mixer favors thorough mixing of the three gas streams in the upper half of the vessel where most of the partial oxidation takes place very rapidly.
  • the hot gases then pass into a reforming catalyst located in the lower half of the vessel where the reforming of the natural gas is completed.
  • Catalytic partial oxidation is typically characterized by the following five chemical reactions:
  • the catalyst typically used in the CPOX reactor is a nickel oxide catalyst, for example of the type G-31 E, G-90LDP and G-90B from Süd-Chemie.
  • the pressure at which the catalytic partial oxidation reaction is carried out is between 25 bar and 100 bar, normally 40 bar.
  • synthesis gas in reactor A is the combination of a steam reformer with the CPOX reactor.
  • a portion of the natural gas is passed to the steam reformer, in which it at temperatures between 700 0 C and 95O 0 C, preferably at 780 0 C, in a Moiverschreib of steam to carbon between 1.5 and 3.0, preferably 2.0, and at a nem Pressure between 25 bar and 50 bar, preferably at 40 bar, is catalytically converted to synthesis gas according to the following reaction equations:
  • this is a nickel / aluminum catalyst, for example, type G-90LDP or G-90B from Süd-Chemie, used.
  • the reformed natural gas is mixed with the part of the natural gas stream bypassed around the steam reformer and passed into the CPOX reactor.
  • it can be dispensed with a division of the natural gas stream by the entire natural gas stream is first passed through the steam reformer and then through the CPOX reactor.
  • the reactor B a portion of the carbon monoxide present in the gas mixture is converted into carbon dioxide in a one-stage or two-stage high-temperature conversion catalysis, cooling between the stages and further cooling of the stream 4 behind the reactor B, resulting in heat recovery ,
  • the synthesis gas from the reactor A is optionally conducted past the carbon monoxide conversion reactor (stream 3). In this way, the production of a desired mixing ratio of carbon dioxide, carbon monoxide and hydrogen at the outlet of the reactor B can be controlled.
  • the raw gas is compressed at elevated pressure and the carbon dioxide is removed from the gas.
  • the removal of carbon dioxide from the crude synthesis gas is accomplished with an absorbent either by a physical wash or a chemical wash.
  • the absorbent is typically cold methanol or glycol ether.
  • the absorbent is typically an alkanolamine, a polyalkanolamine or potassium carbonate.
  • the absorber is a two-stage absorber, wherein in the first stage, that is coarse scrubbing, the carbon dioxide is removed to a level of between 1 mol% and 5 mol% on a dry gas basis, typically up to a level of 2.2 mol%.
  • the carbon dioxide in the raw synthesis gas is up to a content of less than 50 ppmv, usually even less than 10 ppmv, ent ⁇ removed.
  • the pressure at which the carbon dioxide is removed is 45 bar to 100 bar, normally at 80 bar.
  • the compressor and absorber C includes controlled pressure reduction means for the carbon dioxide recovery absorbent, means for regeneration of the absorbent by heat supply, means for maintaining proper composition of the absorbent, and finally means for repressurizing the solvent down to the height of the process pressure. All of the recovered carbon dioxide or parts thereof may be separated and used, for example, for urea synthesis (stream 14).
  • Unconsumed carbon dioxide is discharged into the atmosphere
  • the gas mixture is split behind the absorber C into one (stream 5) and one (stream 6), in each case a suitable ratio for a methanol synthesis (stream 5) and an ammonia synthesis (stream 6 ) to achieve.
  • cryogenic decomposition D the carbon monoxide remaining in the gas is removed by partial condensation at cryogenic temperature, and impurities remaining in the synthesis gas, such as methane, traces of carbon monoxide and argon are washed out of the synthesis gas with liquid nitrogen in a wash column.
  • the cryogenic decomposition products D are a pure stream of ammonia synthesis gas (stream 9) containing hydrogen and nitrogen in a correct stoichiometric ratio, a stream of carbon monoxide contaminated with methane used to enrich the methanol synthesis gas (stream 7), and a stream of any remaining impurities used as fuel gas for the furnaces in the process.
  • the pressure at which the cryogenic separation D is operated is between 45 and 100 bar, normally 75 bar.
  • Cryogenic decomposition D also includes a molecular sieve that removes traces of carbon dioxide and an absorbent that is transported in the carbon dioxide-free synthesis gas and that precedes cleavage at cryogenic temperatures.
  • the methanol synthesis gas (stream 8) is converted to methanol by a catalyst and the methanol is refined by distillation to the required purity (stream 10).
  • the pressure at which the methanol synthesis takes place is between 60 bar and 120 bar, normally at 70 bar.
  • the methanol distillation takes place at about 15 bar to atmospheric pressure.
  • the ammonia synthesis gas (stream 9) is compressed and converted by a catalyst into ammonia (stream 11).
  • the ammonia is separated from the recovered synthesis gas by partial condensation at low temperatures, using liquid ammonia as the coolant.
  • the pressure at which the ammonia synthesis takes place is between 120 bar and 250 bar, normally at 200 bar.
  • the components oxygen (stream 13) and nitrogen (stream 15) are separated from one another by cryogenic distillation from the air.
  • the process of air splitting into its components is well known.
  • the products from the air separation unit G comprise an oxygen stream with a purity between 90% and 99.5%, normally at 99.5%, a stream of nitrogen with a purity of more than 99.995% and a stream of waste gas with the waste products oxygen and nitrogen, which are normally be vented to the atmosphere.
  • the air separation unit G may also, if desired, produce one or more streams of the rare gases such as argon, helium and neon.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

Procédé de coproduction de méthanol et d'ammoniac à partir de gaz naturel qui comporte les étapes suivantes: du gaz naturel (flux 1), de la vapeur et de l'oxygène sont mélangés dans un réacteur A, le gaz naturel étant partiellement oxydé et reformé de manière plus poussée à l'aide de catalyseurs, une partie du monoxyde de carbone présent dans le mélange de gaz (flux 2) est transformé en dioxyde de carbone dans un réacteur B à l'aide de catalyseurs et d'étapes de refroidissement intermédiaires, le mélange de gaz (flux 4) est comprimé dans un compresseur et absorbeur C, le dioxyde de carbone est éliminé par lavage et le mélange de gaz est divisé de manière à obtenir un rapport adapté pour une synthèse du méthanol (flux 5) et une synthèse de l'ammoniac (flux 6), le monoxyde de carbone résiduel est éliminé par condensation partielle à basse température lors d'une décomposition à basse température D, d'autres impuretés telles que le méthane, des traces de monoxyde de carbone et d'argon étant éliminées par lavage à l'aide d'azote liquide (flux 15), le gaz de synthèse de méthanol (flux 8) est transformé en méthanol (flux 10) à l'aide d'un catalyseur dans une unité E et le méthanol est amené par distillation à la pureté exigée, le gaz de synthèse d'ammoniac (flux 9) est comprimé dans une unité F et transformé en ammoniac (flux 11) à l'aide d'un catalyseur, et l'ammoniac est séparé du gaz de synthèse récupéré par condensation partielle.
PCT/EP2005/001329 2004-03-19 2005-02-10 Procede de coproduction de methanol et d'ammoniac a partir de gaz naturel Ceased WO2006114108A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102004013539.8 2004-03-19
DE200410013539 DE102004013539A1 (de) 2004-03-19 2004-03-19 Verfahren zur Koproduktion von Methanol und Ammoniak aus Erdgas

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9321639B2 (en) 2009-08-20 2016-04-26 Saudi Basic Industries Corporation Process for methanol and ammonia co-production
WO2023180114A1 (fr) * 2022-03-21 2023-09-28 Topsoe A/S Procédé de co-production d'ammoniac et de méthanol à teneur réduite en carbone
RU2847803C1 (ru) * 2025-02-14 2025-10-15 Открытое акционерное общество "Красноярский завод цветных металлов имени В.Н. Гулидова", ОАО "Красцветмет" Способ получения аммиака и установка для его осуществления

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102009016402A1 (de) * 2009-04-07 2010-10-14 Uhde Gmbh Verfahren und Anlage zur Behandlung von Synthesegas aus der Vergasung Kohlenstoff-haltiger Feststoffe
DE102016204331A1 (de) * 2016-03-16 2017-08-10 Deutsches Zentrum Für Luft- Und Raumfahrt Verfahren zur Herstellung von Ammoniak aus Rohgas
EP3323786B1 (fr) 2016-11-16 2020-12-02 GasConTec GmbH Procédé de fabrication combinée de méthanol et d'ammoniac
DK3466869T3 (da) 2017-10-09 2020-09-28 Gascontec Ag Fremgangsmåde til kombineret fremstilling af metanol og ammoniak
DE102018210921A1 (de) 2018-07-03 2019-08-14 Thyssenkrupp Ag Vermeidung von VOC und HAP Emissionen aus dem Entgaser von Synthesegas verarbeitenden Anlagen
DE102019204814A1 (de) 2019-04-04 2020-10-08 Thyssenkrupp Ag Reformerdoppelboden
CN113046137B (zh) * 2021-03-12 2021-11-05 蒲城清洁能源化工有限责任公司 一种用于低温甲醇洗系统中氨的捕集采出方法

Citations (6)

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Publication number Priority date Publication date Assignee Title
DE2904008A1 (de) * 1979-02-02 1980-08-07 Linde Ag Verfahren zur herstellung von rohwasserstoff und methanol
DE3336649A1 (de) * 1983-10-08 1985-04-25 Uhde Gmbh, 4600 Dortmund Verfahren zur gemeinsamen herstellung von methanol und ammoniak
DE3712008A1 (de) * 1987-04-09 1988-10-27 Linde Ag Verfahren zur gleichzeitigen erzeugung von methanol und kohlenmonoxid
EP0553631A2 (fr) * 1992-01-23 1993-08-04 The M. W. Kellogg Company Procédé intégré de production de méthanol et d'ammoniaque
US20020098132A1 (en) * 2001-01-22 2002-07-25 Vidalin Kenneth Ebenes Bimodal hydrogen manufacture
WO2003106393A1 (fr) * 2002-06-13 2003-12-24 Lurgi Ag Installation et procede pour produire et separer des gaz de synthese a partir de gaz naturel

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DE2104384A1 (en) * 1971-01-30 1972-08-24 Metallgesellschaft Ag, 6000 Frankfurt Two stage hydrocarbon cracking - for ammonia synthesis

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2904008A1 (de) * 1979-02-02 1980-08-07 Linde Ag Verfahren zur herstellung von rohwasserstoff und methanol
DE3336649A1 (de) * 1983-10-08 1985-04-25 Uhde Gmbh, 4600 Dortmund Verfahren zur gemeinsamen herstellung von methanol und ammoniak
DE3712008A1 (de) * 1987-04-09 1988-10-27 Linde Ag Verfahren zur gleichzeitigen erzeugung von methanol und kohlenmonoxid
EP0553631A2 (fr) * 1992-01-23 1993-08-04 The M. W. Kellogg Company Procédé intégré de production de méthanol et d'ammoniaque
US20020098132A1 (en) * 2001-01-22 2002-07-25 Vidalin Kenneth Ebenes Bimodal hydrogen manufacture
WO2003106393A1 (fr) * 2002-06-13 2003-12-24 Lurgi Ag Installation et procede pour produire et separer des gaz de synthese a partir de gaz naturel

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9321639B2 (en) 2009-08-20 2016-04-26 Saudi Basic Industries Corporation Process for methanol and ammonia co-production
WO2023180114A1 (fr) * 2022-03-21 2023-09-28 Topsoe A/S Procédé de co-production d'ammoniac et de méthanol à teneur réduite en carbone
RU2847803C1 (ru) * 2025-02-14 2025-10-15 Открытое акционерное общество "Красноярский завод цветных металлов имени В.Н. Гулидова", ОАО "Красцветмет" Способ получения аммиака и установка для его осуществления

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