WO2006049526A1 - Procede de decomposition de sulfure d'hydrogene et/ou de thiols - Google Patents

Procede de decomposition de sulfure d'hydrogene et/ou de thiols Download PDF

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Publication number
WO2006049526A1
WO2006049526A1 PCT/RU2004/000447 RU2004000447W WO2006049526A1 WO 2006049526 A1 WO2006049526 A1 WO 2006049526A1 RU 2004000447 W RU2004000447 W RU 2004000447W WO 2006049526 A1 WO2006049526 A1 WO 2006049526A1
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Prior art keywords
gas
hydrogen sulfide
catalyst
hydrogen
temperature
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PCT/RU2004/000447
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English (en)
Russian (ru)
Inventor
Anatolii Nikolaevich Startsev
Valentin Nikolaevich Parmon
Olga Valeryevna Voroshina
Ivan Ivanovich Zakharov
Anastasia Viktorovna Pashigreva
Original Assignee
Institut Kataliza Imeni G.K. Boreskova Sibirskogo Otdeleniya Rossiiskoi Akademii Nauk
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Priority to PCT/RU2004/000447 priority Critical patent/WO2006049526A1/fr
Publication of WO2006049526A1 publication Critical patent/WO2006049526A1/fr

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    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8603—Removing sulfur compounds
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/02—Preparation of sulfur; Purification
    • C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/0495—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by dissociation of hydrogen sulfide into the elements
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/304—Hydrogen sulfide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/306—Organic sulfur compounds, e.g. mercaptans
    • 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
    • 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
    • Y02P20/584—Recycling of catalysts

Definitions

  • the invention relates to the field of gas and oil refining, and in particular to methods for the decomposition and disposal of hydrogen sulfide and mercaptans (thiols), and can be used for the production of hydrogen and sulfur from hydrogen sulfide, as well as for purification of hydrogen sulfide and mercaptans gas mixtures.
  • Hydrogen sulfide is the main by-product of oil refining and hydrometallurgy, in large quantities up to 50 vol.% Is found in gas condensate deposits of natural gas, is the main decomposition product of many mineral and organic substances.
  • hydrogen sulfide is a strong toxic poison, causing poisoning of living organisms. Therefore, the exhaust gases of all industrial plants must be thoroughly cleaned of hydrogen sulfide.
  • hydrogen sulfide can be the feedstock for the production of a valuable chemical product - hydrogen.
  • Mercaptans are by-products of the decomposition of mineral and organic substances, are present in the form of impurities in gaseous products of oil refining, and can be present in significant quantities in gas condensate deposits of natural gas. Mercaptans are toxic substances with a very unpleasant odor, so the exhaust gases of industrial production must be thoroughly cleaned of mercaptans. At the same time, mercaptans are widely used as odorants for household gases, where they are used to detect leakage. The presence of mercaptans in hydrocarbon gases leads to the deactivation of the catalysts for the conversion of these gases into valuable products, so these gases must also be thoroughly cleaned of mercaptans. Direct thermal decomposition of hydrogen sulfide into hydrogen and sulfur by reaction:
  • H 2 S o H 2 + S - Q (1) is a highly endothermic process and can occur at a noticeable rate only at high temperatures.
  • There is a method of thermal decomposition of hydrogen sulfide into hydrogen and sulfur including passing a hydrogen sulfide-containing gas through a reaction zone at a temperature of 850 - 1600 0 C, where HgS decomposes into hydrogen and sulfur, and then cooling said gas to a temperature of 110 - 150 0 C to condense the sulfur formed ( US 4302434, C01B 17/04, 11.24.81).
  • the disadvantages of this method are: the high temperature required to achieve a high degree of decomposition of hydrogen sulfide; high energy consumption for the implementation of the reaction and compensation for possible heat loss; the ability to reduce the degree of decomposition of hydrogen sulfide due to the inverse interaction of hydrogen and sulfur during gas cooling; the impossibility of using the method for the processing of gases containing hydrocarbons and other impurities that may be subjected to pyrolysis at high temperature; low efficiency of the process while reducing the concentration of hydrogen sulfide in the source of hydrogen sulfide-containing gas; the need to use special expensive structural materials with increased heat resistance to design a high-temperature reaction zone.
  • catalysts do not affect the shift in the equilibrium of reaction (1), however, their use allows, in some cases, to shift the equilibrium of reaction (1) towards the formation of products.
  • One of the known methods demonstrates a method for the catalytic decomposition of hydrogen sulfide into hydrogen and sulfur, including circulation hydrogen sulfide-containing gas through a catalyst bed at a temperature of 450-800 0 C with the removal of sulfur formed from the circulating gas (US 3962409, C01 B 17/04, 8.06.76).
  • the advantage of the method is the relatively low temperature of the decomposition reaction of hydrogen sulfide.
  • the disadvantage of this method is the low equilibrium degree of decomposition of hydrogen sulfide in the specified temperature range of not more than 15%.
  • a known method of decomposition of hydrogen sulfide into hydrogen and sulfur including the periodic passage of a hydrogen sulfide-containing gas through a layer of sorbent containing sulfides of iron, cobalt or nickel, at a temperature of 258-536 0 C, which is alternated with periodic heating of the sorbent to temperatures of about 700 0 C for its regeneration ( US 2979384, 423/573, 04/01/61).
  • these components of the sorbent interact with hydrogen sulfide to form hydrogen gas and solid polysulfides of these metals.
  • thermal decomposition of these polysulfides occurs with the formation of the initial sulfides and elemental sulfur vapors.
  • the advantage of this method is the ability to achieve a high degree of decomposition of hydrogen sulfide.
  • the disadvantage of this method is the relatively high decomposition temperature of hydrogen sulfide, a further decrease in which is limited by the low rate of occurrence of these chemical reactions at a reduced temperature, as well as the high temperature of sorbent regeneration.
  • the use of catalysts allows directing reaction (1) along a new route, which can significantly lower the reaction temperature (1).
  • This opportunity is inherent in this invention.
  • the technical effect of the developed method consists in combining the coupled chemisorption-catalytic decomposition of hydrogen sulfide and / or mercaptans on the surface of the catalyst at a temperature below the melting point of sulfur, followed by periodic removal of sulfur from the surface of the catalyst at a temperature above its melting point.
  • the developed method allows to lower the temperature of the chemisorption-catalytic stage below the melting point of sulfur (110-120 0 C), and lowering the temperature favors an increase in the degree of surface coverage by dissociative chemisorbed hydrogen sulfide, and, consequently, the catalyst capacity in relation to adsorbed hydrogen sulfide increases.
  • the thermodynamic effect is achieved by obtaining sulfur in a condensed state, therefore, the temperature of catalyst regeneration is significantly reduced above 11O 0 C, but below 35O 0 C and condensation of solid sulfur.
  • the process of decomposition of mercaptans proceeds similarly.
  • the method is as follows.
  • a hydrogen sulfide-containing and / or mercaptan-containing gas with an initial temperature below the melting point of sulfur is passed through a layer of a solid catalyst capable of dissociatively chemisorbing hydrogen sulfide and / or mercaptan in this temperature range.
  • the coupled chemisorption of hydrogen sulfide and / or mercaptan with the formation of gaseous hydrogen and / or hydrocarbon and solid sulfur-containing chemisorption products on the surface of the solid catalyst is directed to the evolution of product hydrogen or hydrocarbon, or is used in some other way.
  • the gas transmission through the solid catalyst layer is stopped and reactivating gas containing no hydrogen sulfide or containing it at a concentration not exceeding its concentration in the initial hydrogen sulfide-containing gas begins to pass through said layer.
  • the temperature of the reactive gas should be lower than the melting temperature of sulfur 110-12O 0 C, so sulfur is not removed from the surface of the catalyst, but condenses on the surface of the catalyst, releasing catalytically active centers. Thus, reactivation of the catalyst occurs.
  • the feed gas is fed again, after filling the surface of the catalyst with chemisorbed hydrogen sulfide and / or mercaptan, reactive gas is again passed through at a temperature below the melting point of sulfur, and solid sulfur is accumulated on the catalyst surface.
  • This cycle of chemisorption - reactivation of the catalyst continues many times without changing the chemisorption capacity of the catalyst, while solid sulfur accumulates on the surface of the catalyst in an amount of up to 50-100 wt.%.
  • the regeneration temperature is raised to a temperature above the melting sulfur, liquid sulfur flows off the surface of the catalyst and condenses in a condenser located directly behind the catalyst bed. Thus, regeneration of the catalyst occurs.
  • the cycle of chemisorption – reactivation – regeneration processes is carried out repeatedly without changing the chemisorption capacity and catalyst activity.
  • the final product is hydrogen and / or hydrocarbon and solid sulfur.
  • the method is conducted in parallel in at least two layers of solid catalyst, in each of which alternating transmission modes of the source gas, reactivating and regenerating gas.
  • One of the embodiments of the developed method is the contacting of a hydrogen sulfide-containing and / or mercaptan-containing gas with a catalyst in a closed volume with or without gas phase circulation.
  • reactivation catalyst can be carried out in a closed volume with the circulation of the gas phase through a layer of chemisorbent - catalyst or without it.
  • the stage of regeneration of the catalyst can also be carried out in a closed volume with the circulation of the gas phase through a layer of chemisorbent-catalyst or without it.
  • the main advantage of the proposed method is the possibility of decomposition of hydrogen sulfide and / or mercaptans at low temperatures, for example, room temperature and below, while the sulfur formed accumulates on the catalyst surface, but without deactivating the active component of the catalyst.
  • the catalyst As the surface of the catalyst is filled with solid sulfur to a level where the blocking of the active component with solid sulfur begins, the catalyst is heated in the atmosphere of the regenerating gas to a temperature above the melting point of sulfur. Liquid sulfur flows off the surface of the catalyst and condenses in a condenser located directly behind the catalytic zone. Thus, the surface of the catalyst is released and the active component is regenerated.
  • Example 1 Processing is subjected to natural gas containing
  • Hydrogen sulfide as well as nitrogen, carbon dioxide and water vapor.
  • the specified gas is passed at a temperature of 25 0 C through a layer of granular graphite-like carbon material obtained by a known method (US 4978649, C01 31/10, 12/18/90).
  • the gas leaving the layer of this material contains hydrogen in a concentration of up to 3 vol.%, As well as nitrogen, carbon dioxide and water vapor, and there is no hydrogen sulfide.
  • the reactive gas begins to pass through the catalyst at a temperature of 4O 0 C, after 30 minutes the reactivation is stopped, and the starting hydrogen sulfide-containing gas is again fed at room temperature.
  • the capacity of the catalyst for hydrogen sulfide does not change. This chemisorption - reactivation procedure is continued many times without reducing the catalyst capacity for hydrogen sulfide. After the accumulation of solid sulfur on the surface of the catalyst in an amount of more than 20 wt.%, The catalyst capacity for hydrogen sulfide begins to decrease, therefore, the catalyst regeneration procedure is carried out.
  • reactivation gas begins to pass through the catalyst bed at a temperature of 15O 0 C, while liquid sulfur flows off the catalyst surface and condenses in a condenser located directly behind the catalyst bed and cooled to room temperature.
  • the regenerative gas is passed through for 30 minutes, after which the hydrogen sulfide-containing gas is passed again, and so on.
  • Example 2 Processing is subjected to gas containing 5 vol.% Hydrogen sulfide, as well as nitrogen, oxygen and a mixture of light hydrocarbons.
  • the specified gas is passed at a temperature of O 0 C through a layer of molybdenum disulfide MoS 2 .
  • the gas leaving the layer of said material contains hydrogen in an amount of 5 vol.%, As well as nitrogen, oxygen and a mixture of light hydrocarbons; there is no hydrogen sulfide. 40 minutes after the start of the transmission of the hydrogen sulfide-containing gas, hydrogen sulfide appears at the outlet of the layer of the indicated material, therefore, the supply of the source gas is stopped and reactive gas, nitrogen, starts to be supplied at a temperature of 5O 0 C.
  • This cycle of chemisorption-catalytic decomposition of hydrogen sulfide - reactivation of a solid catalyst - regeneration of a catalyst with condensation of sulfur in a condenser located directly behind the catalytic zone is carried out repeatedly with 100% conversion of hydrogen sulfide and without loss of quality of the gas leaving the solid material layer.
  • Example 3 Natural gas containing 40 vol.% Hydrogen sulfide is subjected to processing.
  • the specified gas is passed through a layer of chemisorption-catalytic material - co x Sy cobalt sulfide at a temperature of -5 0 C.
  • Natural gas exiting from the sulfide catalyst layer contains up to 40 vol.% Hydrogen, hydrogen sulfide is absent. 20 minutes after the start of passing the specified gas at the outlet of the sulfide catalyst layer, the hydrogen concentration begins to decrease and hydrogen sulfide appears, therefore, the transmission of the source gas is stopped and the reaction volume is isolated by known methods. After that, the gas phase begins to circulate through the catalyst bed at a temperature of 45 ° C.
  • Processing is subjected to a gas consisting of a mixture of synthesis gas (CO + H 2 ) and 0.1 vol. % hydrogen sulfide.
  • the specified gas is passed through a layer of sulfide catalyst composition Co x Mo y S z , cooled to -1O 0 C.
  • the processed gas contains CO and hydrogen, there is no hydrogen sulfide. 45 minutes after the start of transmission, hydrogen sulfide appears in the exhaust gas, therefore, the supply of the source gas is stopped and reactive gas, nitrogen, is supplied at a temperature of 6O 0 C. After 20 minutes, the reactivation is completed and the feed gas mixture is again fed at a temperature of -1O 0 C.
  • Cycles chemisorption - reactivation is repeated many times until the surface of the catalyst is filled with solid sulfur. Then, the catalyst bed is insulated and heated at a temperature of 12 0 0 C, liquid sulfur flows off the catalyst surface and condenses in a condenser located immediately after the catalytic layer and cooled to 0 0 C. 50 min after the start of catalyst regeneration, the initial hydrogen sulfide-containing gas is fed again. The process is carried out in batch mode repeatedly without reducing 100% hydrogen sulfide conversion and without reducing the chemisorption capacity of the catalyst. Example 5. Processing is subjected to a gas consisting of a mixture of 90 vol. % nitrogen and 10 vol. % hydrogen sulfide.
  • the specified gas is passed through a layer of chemisorption-catalytic material - porous metallic nickel, cooled to -20 0 C.
  • the processed gas contains nitrogen and hydrogen, there is no hydrogen sulfide.
  • the supply of the source gas is stopped and reactivating gas, hydrogen, is supplied at a temperature of 6O 0 C.
  • the reactivation is completed and they start feeding the initial gas mixture again at a temperature of –2O 0 C.
  • Chemisorption cycles reactivation is repeated many times until the surface of the catalyst is filled with solid sulfur.
  • a regenerating gas — nitrogen — is supplied through a layer of the indicated catalyst at a temperature of 300 0 C, liquid sulfur flows off the surface of the catalyst and condenses in a condenser located immediately after the catalytic layer and cooled to O 0 C. 50 minutes after the start of catalyst regeneration, the supply of regenerating gas is stopped and re-fed source gas containing hydrogen sulfide at a temperature of -2O 0 C. The process is carried out batchwise repeatedly without reducing 100% conversion of hydrogen sulphide and without diminishing chemisorption constant capacitance catalyst.
  • Example 6 Processing is subjected to a gas consisting of a mixture of oxygen and 0.01 vol.% Hydrogen sulfide.
  • the specified gas is passed through a layer of chemisorption-catalytic material - porous nickel boride, cooled to 2O 0 C.
  • the processed gas contains oxygen and hydrogen, there is no hydrogen sulfide. 10 minutes after the start of transmission, hydrogen sulfide appears in the exhaust gas, therefore, the supply of the source gas is stopped and reactive gas, nitrogen, is supplied at a temperature of 6O 0 C. After 20 minutes, the reactivation is completed and the feed gas mixture is again fed at a temperature of 2O 0 C.
  • Chemisorption cycles - reactivation is repeated many times until the surface of the catalyst is filled with solid sulfur. Then, a nitrogen regenerating gas is fed through a layer of the indicated catalyst at a temperature of 14O 0 C, liquid sulfur flows from the catalyst surface and condenses in a condenser located immediately after the catalytic layer and cooled to O 0 C. 20 minutes after the start of the catalyst regeneration, the supply of regenerating gas is stopped and again serves the source of hydrogen sulfide gas. The process is carried out in batch mode repeatedly without reducing 100% hydrogen sulfide conversion and without reducing the chemisorption capacity of the catalyst. Example 7. Processing is subjected to natural gas containing methane, 5 vol. % hydrogen sulfide and 0.3 vol.
  • the specified gas is passed at room temperature through a layer of sulfide catalyst composition Co x Mo y S z deposited on a porous carrier - alumina.
  • the processed gas contains methane and hydrogen, hydrogen sulfide and methyl mercaptan are absent. 90 minutes after the start of transmission, hydrogen sulfide and methyl marcaptan appear in the exhaust gas; therefore, the supply of the initial gas is stopped and reactive gas, nitrogen, begins to be supplied at a temperature of 5 ° C. After 20 minutes, the reactivation is completed and the initial gas mixture is again fed at room temperature.
  • the chemisorption - reactivation cycles are repeated many times until the surface of the catalyst is filled with solid sulfur. Then, the catalyst catalyst layer is isolated and heated at a temperature of 12 0 0 C, liquid sulfur flows off the catalyst surface and condenses in a condenser located immediately after the catalytic layer and cooled to 0 0 C. 50 min after the start of catalyst regeneration, the starting hydrogen sulfide and methyl mercaptan containing material are again fed gas. The process is carried out in batch mode repeatedly without reducing 100% hydrogen sulfide conversion and without reducing the chemisorption capacity of the catalyst.
  • Example 8 Processing is subjected to gas containing ethane and 5 vol. % ethyl mercaptan (ethanethiol).
  • the specified gas is passed at room temperature through a layer of sulfide catalyst composition Ni x MOyS 2 , deposited on a porous carrier - silica gel.
  • the processed gas contains ethane, ethyl mercaptan is absent.
  • 90 minutes after the start of transmission ethyl mercaptan appears in the exhaust gas; therefore, the supply of the source gas is stopped and reactive gas, nitrogen, is supplied at a temperature of 60 ° C. After 30 minutes, the reactivation is completed and the feed gas mixture is again fed at room temperature.
  • Chemisorption - reactivation cycles are repeated many times until filling the surface of the catalyst with solid sulfur. Then, the catalyst bed is isolated and heated at a temperature of 12 0 0 C, liquid sulfur flows off the catalyst surface and condenses in a condenser located immediately after the catalytic layer and cooled to 0 0 C. 50 min after the start of catalyst regeneration, the starting ethane and ethyl mercaptan are again fed. The process is carried out in batch mode repeatedly without reducing 100% ethyl mercaptan conversion and without reducing the chemisorption capacity of the catalyst.
  • the proposed method allows the decomposition of hydrogen sulfide and / or mercaptans at a low temperature, for example room temperature, and there is no need for frequent catalyst regeneration after each chemisorption step.

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  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
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  • Environmental & Geological Engineering (AREA)
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  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention relève du domaine de la transformation du gaz et du pétrole, et se rapporte plus précisément à des procédés de décomposition et d'utilisation de sulfure d'hydrogène et/ou de thiols, et peut être utilisée pour produire de l'hydrogène et du soufre à partir de sulfure d'hydrogène, ainsi que pour éliminer le sulfure d'hydrogène et les thiols de mélanges gazeux. Le procédé de décomposition de sulfure d'hydrogène et/ou de thiols selon l'invention, qui permet d'obtenir de l'hydrogène (hydrocarbures) et du soufre, consiste à mettre en contact un gaz contenant du sulfure d'hydrogène et/ou des thiols à travers une couche de matière dure pouvant décomposer le sulfure d'hydrogène en hydrogène et/ou en un gaz contenant des hydrocarbures, et à former des composés contenant du soufre à la surface de ladite matière, l'étape de décomposition étant réalisée par chimisorption-catalyse à une température inférieure au point de fusion du soufre, de façon que l'on obtienne de l'hydrogène et/ou des hydrocarbures et des composés contenant du soufre superficiels de chimisorption. La réactivation est effectuée à une température inférieure au point de fusion du soufre, et la régénération est effectuée à une température supérieure au point de fusion du soufre. L'invention permet d'exécuter un processus de décomposition à faible température, par exemple à température ambiante, sans qu'il soit nécessaire de procéder à la régénération fréquente du catalyseur après chaque étape de chimisorption.
PCT/RU2004/000447 2004-11-03 2004-11-03 Procede de decomposition de sulfure d'hydrogene et/ou de thiols WO2006049526A1 (fr)

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4399112A (en) * 1980-04-23 1983-08-16 Societe Nationale Elf Aquitaine Process for the catalytic incineration of residual gases containing a low content of at least one sulfur compound selected from COS, CS2 and the mercaptans and possibility at least one member of the group
US4439412A (en) * 1981-07-06 1984-03-27 Behie Leo A Process for producing hydrogen from hydrogen sulphide in a gas fluidized bed reactor
RU2088516C1 (ru) * 1993-03-25 1997-08-27 Говоров Геннадий Васильевич Способ разложения газообразного сероводорода
RU2131396C1 (ru) * 1998-02-02 1999-06-10 Быстрова Татьяна Владимировна Способ получения серы и водорода из сероводорода

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4399112A (en) * 1980-04-23 1983-08-16 Societe Nationale Elf Aquitaine Process for the catalytic incineration of residual gases containing a low content of at least one sulfur compound selected from COS, CS2 and the mercaptans and possibility at least one member of the group
US4439412A (en) * 1981-07-06 1984-03-27 Behie Leo A Process for producing hydrogen from hydrogen sulphide in a gas fluidized bed reactor
RU2088516C1 (ru) * 1993-03-25 1997-08-27 Говоров Геннадий Васильевич Способ разложения газообразного сероводорода
RU2131396C1 (ru) * 1998-02-02 1999-06-10 Быстрова Татьяна Владимировна Способ получения серы и водорода из сероводорода

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