WO2010150063A1 - Procédé de valorisation de gaz naturel à teneur élevée en sulfure d’hydrogène - Google Patents

Procédé de valorisation de gaz naturel à teneur élevée en sulfure d’hydrogène Download PDF

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Publication number
WO2010150063A1
WO2010150063A1 PCT/IB2010/001344 IB2010001344W WO2010150063A1 WO 2010150063 A1 WO2010150063 A1 WO 2010150063A1 IB 2010001344 W IB2010001344 W IB 2010001344W WO 2010150063 A1 WO2010150063 A1 WO 2010150063A1
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hydrogen
carbon disulfide
natural gas
reaction
reforming
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PCT/IB2010/001344
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English (en)
Inventor
Alberto De Angelis
Paolo Pollesel
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Eni S.P.A.
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Priority to RU2011153109/04A priority Critical patent/RU2522443C2/ru
Priority to CA2766037A priority patent/CA2766037A1/fr
Publication of WO2010150063A1 publication Critical patent/WO2010150063A1/fr

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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
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • 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
    • C01B17/48—Sulfur dioxide; Sulfurous acid
    • C01B17/50—Preparation of sulfur dioxide
    • C01B17/508—Preparation of sulfur dioxide by oxidation of sulfur compounds
    • 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
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • 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
    • C01B2203/0211—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step
    • 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
    • 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
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • 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
    • C01B2203/0455—Purification by non-catalytic desulfurisation
    • 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
    • C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
    • 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
    • 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
    • C01B2203/08—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
    • 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
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • 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
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • 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
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • C01B2203/1052—Nickel or cobalt catalysts
    • 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
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • C01B2203/1052—Nickel or cobalt catalysts
    • C01B2203/1058—Nickel catalysts
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane
    • 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
    • C01B2203/146—At least two purification steps in series

Definitions

  • the present invention relates to a process for the upgrading of natural gas with a high hydrogen sulfide content .
  • the present invention relates to a process for the upgrading of natural gas containing hydrogen sulfide in concentrations higher than or equal to 60% by volume.
  • the present invention relates to a process for the upgrading of natural gas containing hydrogen sulfide in concentrations higher than or equal to 60% by volume by the recovery of hydrogen from both the sulfurized compound and hydrocarbon phase present.
  • natural gas essentially consists of methane, but, in addition to significant traces of higher C 2 -C 7 + hydrocarbons, it can also contain variable quantities of inert gases or pollutants, for example carbon dioxide or nitrogen, whose presence must be eliminated or reduced to satisfy the specifications of use.
  • Fields/reservoirs of natural gas with a high hydrogen sulfide content can be found all over the world, for example Bearberry fields or Panther River in Canada are natural gas reservoirs containing approximately 90% by volume and 68% by volume of H 2 S, respectively. In the United States there are fields such as Black Creek and Cox (Missisipi) which contain approximately 78% and 65% of H 2 S, respectively. "Super- sour" gas fields having large dimensions also exist, such as the Zhaolazhuang-Hebei field in China which comprises 19 wells which produce a natural gas whose concentration of H 2 S varies from 60 to 90% by volume.
  • superacid gas reservoirs also known as "super-sour” gas reservoirs
  • These superacid gas reservoirs either remain unused, as the recovery of natural gas (methane) is too onerous, or, as in the case of the Zholazhuang field, they are used for the production of sulphur by means of the Claus process, sending the gaseous stream, substantially as it leaves the production well, directly to the combustion reactor where the partial oxidation of the hydrogen sulfide to SO 2 , takes place.
  • the methane present is burnt and this is an economic loss which becomes increasingly more significant, the higher the methane content in the natural gas .
  • Hydrogen is a raw material which is extremely requested in refineries, for example, for all hydrotreatment processes such as hydrocracking and hydrodesulfurization, and it would therefore be extremely desirable to be able to obtain it from a source with zero value such as current "super-sour" natural gas reservoirs .
  • a method which allows hydrogen to be recovered from natural gas, strongly acid due to hydrogen sulfide, is the reforming reaction with methane according to the reaction:
  • the Applicant has also found that it is possible to use the CS 2 , produced by the reforming reaction between methane and H 2 S, as fuel for sustaining the reaction
  • the previous endothermic reforming reaction of H 2 S with methane can be sustained without having to burn any high-quality fuel.
  • the SO 2 produced by the combustion can be upgraded downstream as intermediate for specific synthesis reactions, for example to produce sulfuric acid, or it can be disposed of by injection into the subsoil.
  • a further preferred aspect of this reaction is the use of the mixture thus formed of carbon monoxide and hydrogen, after the separation of the water, for the production of methanol according to:
  • An object of the present invention therefore relates to a process for upgrading superacid natural gas, with a content of hydrogen sulfide higher than or equal to 60% by volume, with the production of hydrogen, which comprises. a. feeding the superacid natural gas to a reforming reactor operating at a temperature ranging from 900 to 1500 0 C and at atmospheric pressure, or slightly lower than atmospheric pressure, for example ranging from 0.08 to 0.1 MPa, to produce a mixture essentially consisting of carbon disulfide (CS 2 ) and hydrogen (H 2 ) ; b. cooling the reaction products, separating the carbon disulfide from the remaining reaction mixture containing hydrogen and recovering the hydrogen; c.
  • step (d) burning the carbon disulfide with a gas containing oxygen to produce a gaseous mixture, essentially consisting of CO 2 and SO 2/ at a high temperature; d. feeding at least a part of the hot gases of the combustion of carbon disulfide to the reforming step, as heat source for maintaining the endothermic reaction of step (a) ; and e. providing the combustion gases of carbon disulfide, also coming from step (d) , as intermediates for chemical syntheses downstream or for their disposal by injection into specific geological structures.
  • the reaction products can be cooled to a temperature which is optimum for the subsequent operations, for example to a temperature lower than 50 0 C, in order to recover the carbon disulfide, which is liquid at those temperatures, from the gaseous phase essentially consisting of hydrogen, residual H 2 S and possible reaction by-products and/or hydrocarbons.
  • the gaseous phase can then be treated with conventional methods, for example by means of the selective adsorption technology of the PSA type or treatment with membranes, for the recovery of the hydrogen.
  • the possible H 2 S in excess can be recovered by the traditional techniques, for example by absorption with amines .
  • the cooling phase preferably takes place in heat exchangers where the cooling liquid is water, which can be transformed into vapour at a temperature of 100- 150 0 C and a pressure of 0.2-10 MPa.
  • the vapour can then be used to produce electric energy or as a heat source to be destined for the running of other plants .
  • the reaction products can pre-heat the reagents which are to be fed to the reforming reactor.
  • the carbon disulfide recovered in the liquid state is burnt in a specific reactor, with air or air enriched in oxygen as comburent .
  • the combustion gases leaving the reactor at a temperature of 1000-2500 0 C are fed, either partially or totally, to a further system of heat exchangers to bring the reagents, possibly pre-heated, to the correct temperature, before being introduced into the reforming reactor.
  • a further system of heat exchangers to bring the reagents, possibly pre-heated, to the correct temperature, before being introduced into the reforming reactor.
  • the production of hydrogen can be obtained from a stream containing hydrogen sulfide without having to use any external high-quality fuel and a stream containing SO 2 is also obtained as by-product, which can be advantageously used as raw material for chemical syntheses such as, for example, the production of sulfuric acid.
  • the stream containing SO 2 can be injected into adequate geological structures.
  • An alternative embodiment of the process, object of the present invention envisages that only a part of the CS 2 produced is burnt as energy source, whereas the remaining part is separated and destined for commercialization.
  • the balance between the aliquot of burnt CS 2 and that separated and destined for sale depends on the quantity of heat which is to be produced to sustain the endothermic reforming reaction of methane with H 2 S.
  • the sufficient quantity of CS 2 to be destined for combustion to sustain the reforming of methane with H 2 S is equal to at least 55% by weight of the total CS 2 produced.
  • the remaining part of CS 2 can be separated and sold or burnt to provide heat energy for also sustaining other process equipment, for example for producing high-pressure vapour which can be used in this or other plants .
  • Another innovative aspect of the process, object of the present invention consists of the fact that the sulfur present in the H 2 S molecule is transformed directly into SO 2 , which can in turn be transformed, by reactions and processes well-known in literature, for example, to sulfuric acid, requested by the chemical industry, rather than into elemental sulfur as in the conventional Claus process. Elemental sulfur does in fact have considerable environmental storage problems and many nations in which there are natural gas reservoirs impose heavy economic sanctions for the storage of sulfur. By transforming sulfur to sulfuric acid, on the other hand, a liquid product is obtained, which can be easily transported and sold as such.
  • A is a conventional plant using amines for the recovery of hydrogen sulfide in excess with respect to the stoichiometric value of the reforming reaction
  • B is a heat exchanger system for heat recovery
  • C is a heat exchanger system which can be used for providing the energy necessary for the reforming
  • Rl is the methane/H 2 S reforming reactor and can be, for example, a fixed bed or fluid bed catalytic reactor
  • E is a condensation and collection system of the CS 2 produced in the reactor Rl
  • R2 is the combustion reactor of CS 2 .
  • the stream (1) is preheated in B, brought to the reforming reaction temperature in C and then fed to the reactor Rl.
  • the hot reaction products (2) are recovered from the reactor Rl, at a temperature of about 900-1500 0 C. These hot gases are fed to B, for preheating the reagents, and are then fed to the condenser E where the carbon disulfide CS 2 , in the liquid state, stream (3) , is separated from the gaseous phase essentially consisting of H 2 , non-reacted H 2 S/in excess and possibly methane and/or other hydrocarbons and/or reaction byproducts, stream (4) .
  • a part of the carbon disulfide produced, stream (5) can be deviated from the cycle, object of the present invention, and destined for other purposes.
  • the carbon disulfide (3) and comburent air (6) are fed to the combustion reactor R2.
  • the combustion gases, stream (7) which comprise CO 2 and SO 2 , leave the reactor at a temperature of about 1000-2500 0 C and are fed directly to the heat exchanger C where they heat the reagent gases (CH 4 e H 2 S) bringing them to a temperature of about 900-1500 0 C, or slightly higher.
  • the stream of heated reagent gases (8) is fed to the reactor Rl, in which the catalyst is positioned, consisting for example of one or more sulfides of - metals of groups VIB, VIIB and VIIIB of the periodic system.
  • chromium, tungsten, molybdenum, iron, cobalt and nickel sulfides are particularly preferred, used alone or in a mixture with each other.
  • the temperature inside Rl is kept uniform at about 900-1500 0 C.
  • the combustion gases of carbon disulfide can be further cooled, in specific equipment not illustrated in the scheme of the enclosed figure, and then used for further chemical processes, for example the synthesis of sulfuric acid, or they can be disposed of by injecting them into the subsoil or into deep seawater.
  • the products of the reforming reaction which, after cooling in E, are in gas phase, stream (4) , are fed to the plant A for recovery of the hydrogen sulfide.
  • the stream (9) essentially consisting of hydrogen, is discharged from the plant A.
  • the outgoing fumes essentially consisting of CS 2 , hydrogen and non-reacted H 2 S, are sent to a condenser from which the CS 2 is separated as liquid, whereas the gaseous stream comprising hydrogen and H 2 S, is sent to an amine plant .
  • This stream is used for heating the reagents to be fed to the reforming reactor. After transferring its heat to the reagents of the reforming reaction, it can then be subsequently fed to a plant for the production of sulfuric acid or disposed of by injection into the subsoil.

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

Abstract

L’invention concerne un procédé de valorisation de gaz naturel superacide présentant une teneur en sulfure d’hydrogène supérieure ou égale à 60% en volume, avec production d’hydrogène. Le procédé comprend les étapes consistant à : a) traiter le sulfure d’hydrogène au méthane (reformage) selon la réaction endothermique 2 H2S + CH4 = CS2 + 4H2 (1) ; 2) refroidir les produits de réaction, séparer le disulfure de carbone (CS2) et récupérer l’hydrogène; c) brûler le disulfure de carbone; d) charger au moins une partie des gaz chauds résultant de la combustion du disulfure de carbone vers l’étape de reformage, comme source de chaleur destinée à maintenir la réaction endothermique (1); e) éliminer les gaz de combustion refroidis de sulfure de carbone.
PCT/IB2010/001344 2009-06-24 2010-06-02 Procédé de valorisation de gaz naturel à teneur élevée en sulfure d’hydrogène WO2010150063A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
RU2011153109/04A RU2522443C2 (ru) 2009-06-24 2010-06-02 Способ повышения качества природного газа с высоким содержанием сероводорода
CA2766037A CA2766037A1 (fr) 2009-06-24 2010-06-02 Procede de valorisation de gaz naturel a teneur elevee en sulfure d'hydrogene

Applications Claiming Priority (2)

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ITMI2009A001115 2009-06-24
ITMI2009A001115A IT1394568B1 (it) 2009-06-24 2009-06-24 Procedimento per la valorizzazione di gas naturale ad alto contenuto di idrogeno solforato

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WO2010150063A1 true WO2010150063A1 (fr) 2010-12-29

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IT (1) IT1394568B1 (fr)
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109721028A (zh) * 2017-10-27 2019-05-07 中国石油化工股份有限公司 甲烷硫化氢重整制氢的方法
WO2022023365A1 (fr) * 2020-07-28 2022-02-03 Totalenergies Se Procédé de conduite d'une réaction de thio-reformage endothermique d'hydrocarbures dans une installation comprenant un réacteur à lit fluidisé électrifié

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB293172A (en) * 1927-05-26 1928-07-05 Ig Farbenindustrie Ag Improvements in the manufacture and production of carbon disulphide
US2788262A (en) * 1953-05-01 1957-04-09 Pan American Petroleum Corp Process for preparation of carbon disulfide
US3388971A (en) * 1965-06-07 1968-06-18 Seymour C. Schuman Production of hydrogen
GB1126465A (en) * 1964-09-14 1968-09-05 Ivor Gray Nixon Manufacture of hydrogen and carbon disulphide
US4695443A (en) * 1985-02-14 1987-09-22 Stauffer Chemical Company Autothermal process for the production of carbon disulfide and hydrogen sulfide
DE102004013283A1 (de) * 2004-03-18 2005-10-13 Guennadi, Berner Das Verfahren der gemeinsamen Schwefelkohlenstoff und Schwefelsäureproduktion ohne Treibstoffverwendung
US20060254769A1 (en) * 2005-04-21 2006-11-16 Wang Dean C Systems and methods for producing oil and/or gas
WO2010102653A1 (fr) * 2009-03-13 2010-09-16 Eni S.P.A. Procédé pour l'abattement de sulfure d'hydrogène à partir de compositions le contenant avec production simultanée d'hydrogène

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2216506C1 (ru) * 2002-02-26 2003-11-20 Институт катализа им. Г.К.Борескова СО РАН Способ получения водорода и элементарной серы из сероводорода

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB293172A (en) * 1927-05-26 1928-07-05 Ig Farbenindustrie Ag Improvements in the manufacture and production of carbon disulphide
US2788262A (en) * 1953-05-01 1957-04-09 Pan American Petroleum Corp Process for preparation of carbon disulfide
GB1126465A (en) * 1964-09-14 1968-09-05 Ivor Gray Nixon Manufacture of hydrogen and carbon disulphide
US3388971A (en) * 1965-06-07 1968-06-18 Seymour C. Schuman Production of hydrogen
US4695443A (en) * 1985-02-14 1987-09-22 Stauffer Chemical Company Autothermal process for the production of carbon disulfide and hydrogen sulfide
DE102004013283A1 (de) * 2004-03-18 2005-10-13 Guennadi, Berner Das Verfahren der gemeinsamen Schwefelkohlenstoff und Schwefelsäureproduktion ohne Treibstoffverwendung
US20060254769A1 (en) * 2005-04-21 2006-11-16 Wang Dean C Systems and methods for producing oil and/or gas
WO2010102653A1 (fr) * 2009-03-13 2010-09-16 Eni S.P.A. Procédé pour l'abattement de sulfure d'hydrogène à partir de compositions le contenant avec production simultanée d'hydrogène

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
HUANG ET AL: "Liquid hydrogen production via hydrogen sulfide methane reformation", JOURNAL OF POWER SOURCES, ELSEVIER SA, CH, vol. 175, no. 1, 26 November 2007 (2007-11-26), pages 464 - 472, XP022361662, ISSN: 0378-7753 *
M.L.POUTSMA & ALL.: "Selective Formation of Methanol from Synthesis Gas over Palladium Catalysts", JOURNAL OF CATALYSIS, vol. 52, 1 May 1978 (1978-05-01) - 1 May 1978 (1978-05-01), pages 157 - 168, XP002604671 *

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109721028A (zh) * 2017-10-27 2019-05-07 中国石油化工股份有限公司 甲烷硫化氢重整制氢的方法
CN109721028B (zh) * 2017-10-27 2020-09-11 中国石油化工股份有限公司 甲烷硫化氢重整制氢的方法
WO2022023365A1 (fr) * 2020-07-28 2022-02-03 Totalenergies Se Procédé de conduite d'une réaction de thio-reformage endothermique d'hydrocarbures dans une installation comprenant un réacteur à lit fluidisé électrifié

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RU2522443C2 (ru) 2014-07-10
RU2011153109A (ru) 2013-07-27

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