WO2003016250A1 - Production d'hydrocarbures - Google Patents

Production d'hydrocarbures Download PDF

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Publication number
WO2003016250A1
WO2003016250A1 PCT/GB2002/003311 GB0203311W WO03016250A1 WO 2003016250 A1 WO2003016250 A1 WO 2003016250A1 GB 0203311 W GB0203311 W GB 0203311W WO 03016250 A1 WO03016250 A1 WO 03016250A1
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Prior art keywords
gas
reformed gas
steam
reforming
hydrocarbons
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PCT/GB2002/003311
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English (en)
Inventor
Peter Edward James Abbott
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Johnson Matthey Plc
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Publication date
Application filed by Johnson Matthey Plc filed Critical Johnson Matthey Plc
Priority to EA200400320A priority Critical patent/EA005280B1/ru
Priority to AU2002317369A priority patent/AU2002317369B2/en
Publication of WO2003016250A1 publication Critical patent/WO2003016250A1/fr
Priority to NO20040665A priority patent/NO335117B1/no

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • 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
    • C01B3/382—Multi-step processes
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    • 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
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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    • 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
    • C01B2203/0238—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a carbon dioxide reforming step
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    • 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
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    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
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    • C01B2203/0405—Purification by membrane separation
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    • C01B2203/042—Purification by adsorption on solids
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    • C01B2203/0465—Composition of the impurity
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    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
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    • 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
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    • 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
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    • 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
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    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
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    • C01B2203/14—Details of the flowsheet
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
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    • C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus
    • 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
    • Y02P20/10—Process efficiency

Definitions

  • This invention relates to the production of hydrocarbons by the Fischer-Tropsch process and in particular to steam reforming and in particular to the production of the synthesis gas for use in that process.
  • the synthesis gas contains hydrogen and carbon oxides and is produced by the catalytic reaction of steam with a hydrocarbon feedstock.
  • a synthesis gas containing carbon monoxide and hydrogen is reacted in the presence of a catalyst, which is typically a cobalt- and/or iron- containing composition.
  • a catalyst typically a cobalt- and/or iron- containing composition.
  • the process may be effected using one or more fixed catalyst beds or using a moving catalyst, for example a slurry of the catalyst in a hydrocarbon liquid.
  • the product hydrocarbon liquid is separated from the residual gas.
  • the reaction may be carried out in a single pass or part of the residual gas may be combined with fresh synthesis gas and recycled to the Fischer-Tropsch reactor. Any residual gas which is not recycled to the Fischer- Tropsch reactor for further reaction is here termed tail gas. Since the reaction of the synthesis gas is incomplete, the tail gas will contain some hydrogen and carbon monoxide.
  • the tail gas may also contain some light hydrocarbons, e.g. paraffins including methane, ethane, butane, olefins such as propylene, alcohols such as ethanol, and traces of other minor components such as organic acids. It will generally also contain some carbon dioxide, which may be present in the synthesis gas fed to the Fischer-Tropsch reaction and/or is formed by side reactions. Possibly, as a result of incomplete separation of the liquid hydrocarbon product, the tail gas may also contain a small proportion of higher hydrocarbons, i.e. hydrocarbons containing 5 or more carbon atoms. These components of the tail gas represent a valuable source of carbon and hydrogen.
  • some light hydrocarbons e.g. paraffins including methane, ethane, butane, olefins such as propylene, alcohols such as ethanol, and traces of other minor components such as organic acids. It will generally also contain some carbon dioxide, which may be present in the synthesis gas fed to the Fischer-Tropsch
  • At least part of the tail gas is recycled and used as part of the feedstock employed to make the Fischer-Tropsch synthesis gas.
  • Steam reforming is widely practised and is used to produce hydrogen streams and synthesis gas for a number of processes such as ammonia, methanol as well as the Fischer- Tropsch process.
  • a desulphurised hydrocarbon feedstock e.g. natural gas or naphtha
  • a suitable catalyst generally a transition metal, especially nickel, on a suitable support, for example alumina, magnesia, zirconia, or a calcium aluminate cement.
  • any hydrocarbons containing two or more carbon atoms that are present are converted to carbon monoxide and hydrogen, and in addition, the reversible methane/steam reforming and shift reactions occur. The extent to which these reversible reactions proceed depends upon the reaction conditions, e.g. temperature and pressure, the feed composition and the activity of the reforming catalyst.
  • the methane/steam reforming reaction is highly endothermic and so the conversion of methane to carbon oxides is favoured by high temperatures. For this reason, steam reforming is usually effected at outlet temperatures above about 600°C, typically in the range 650°C to 950°C, by passing the feedstock/steam mixture over a primary steam reforming catalyst disposed in externally heated tubes.
  • the composition of the product gas depends on, inter alia, the proportions of the feedstock components, the pressure and temperature.
  • the product normally contains methane, hydrogen, carbon oxides, steam and any gas, such as nitrogen, that is present in the feed and which is inert under the conditions employed. For applications such as Fischer-Tropsch synthesis, it is desired that the molar ratio of hydrogen to carbon monoxide is about 2 and the amount of carbon dioxide present is small.
  • the primary reformed gas may be subjected to secondary reforming by partially combusting the primary reformed gas using a suitable oxidant, e.g. air or oxygen.
  • a suitable oxidant e.g. air or oxygen.
  • This increases the temperature of the reformed gas which is then passed adiabatically through a bed of a secondary reforming catalyst, again usually nickel on a suitable support, to bring the gas composition towards equilibrium.
  • Secondary reforming serves three purposes: the increased temperature resulting from the partial combustion and subsequent adiabatic reforming results in a greater amount of reforming so that the secondary reformed gas contains a decreased proportion of residual methane.
  • the increased temperature favours the reverse shift reaction so that the carbon monoxide to carbon dioxide ratio is increased.
  • the partial combustion effectively consumes some of the hydrogen present in the reformed gas, thus decreasing the hydrogen to carbon oxides ratio.
  • these factors render the secondary reformed gas formed from natural gas as a feedstock more suited for use as synthesis gas for applications such as Fischer-Tropsch synthesis than if the secondary reforming step was omitted.
  • more high grade heat can be recovered from the secondary reformed gas: in particular, the recovered heat can be used to heat the catalyst-containing tubes of the primary reformer.
  • the primary reforming may be effected in a heat exchange reformer in which the catalyst-containing reformer tubes are heated by the secondary reformed gas. Examples of such reformers and processes utilising the same are disclosed in for example US 4 690 690 and US 4 695 442.
  • the Fischer-Tropsch tail gas is liable to contain a significant amount of carbon monoxide. If this is added to the feedstock prior to primary reforming in a heat exchange reformer, the carbon monoxide undergoes the exothermic methanation reaction resulting in a faster increase in temperature of the gas undergoing reforming than if the tail gas had not been added. The temperature difference between the gas undergoing reforming and the heating medium is thus decreased and so more heat transfer area, e.g. more and/or longer heat exchange tubes, is required for a given reforming duty.
  • this problem may be overcome.
  • the present invention provides a process for the production of hydrocarbons by the Fischer-Tropsch reaction comprising a) subjecting a mixture of a hydrocarbon feedstock and steam to steam reforming by i) passing the mixture over a catalyst disposed in heated tubes in a heat exchange reformer to form a primary reformed gas, ii) subjecting the primary reformed gas to secondary reforming by partially combusting the primary reformed gas with an oxygen-containing gas and bringing the resultant partially combusted gas towards equilibrium over a secondary reforming catalyst, and iii) using the resultant secondary reformed gas to heat the tubes of the heat exchange reformer, thereby producing a partially cooled reformed gas, b) further cooling the partially cooled reformed gas to below the dew point of the steam therein to condense water and separating condensed water to give a de-watered synthesis gas, c) synthesising hydrocarbons from said de-watered synthesis gas, and separating at least some of the synthesise
  • the amount of oxygen required in the secondary reformer is determined by two main considerations, viz. the desired composition of the product gas, and the heat balance of the heat exchange reformer. In general, increasing the amount of oxygen causes the [H 2 ] / [CO] ratio to decrease and the proportion of carbon dioxide to decrease. Alternatively, if the conditions are arranged such that the product composition and temperature is kept constant, increasing the temperature at which the feedstock is fed to the heat exchange reformer decreases the amount of oxygen required (at a constant oxygen feed temperature). Decreasing the required amount of oxygen is advantageous as this means that a smaller, and hence cheaper, air separation plant can be employed to produce the oxygen.
  • the temperature of the feedstock can be increased by any suitable heat source, which may, if necessary, be a fired heater, which of course can use air, rather than oxygen, for the combustion.
  • carbon dioxide is separated from the synthesis gas prior to the Fischer-Tropsch synthesis stage and recycled to the synthesis gas production.
  • This recycled carbon dioxide stream may be added, as in the aforesaid WO 00/09441 , to the feedstock prior to feeding the latter to the heat exchange reformer or to the primary reformed gas before the latter is fed to the secondary reforming step.
  • some or all of the Fischer-Tropsch tail gas which will contain hydrogen, carbon monoxide and lower hydrocarbons such as methane and ethane, is added to the primary reformed gas before feeding the latter to the secondary reforming step.
  • the primary reforming process can be operated at a lower steam ratio.
  • steam ratio we mean the ratio of the number of moles of steam to the number of gram atoms of hydrocarbon carbon in the feed: thus a methane/steam mixture comprising 2 moles of steam per mole of methane has a steam ratio of 2.
  • the risk of carbon deposition is decreased by decreasing the proportion of carbon dioxide in the feed and also by increasing the steam ratio.
  • the process can be operated at a lower steam ratio.
  • the feedstock is methane and amount of recycled carbon dioxide is 0.2 moles per mole of methane feed, at a primary reforming exit temperature of 750°C, adding the recycled carbon dioxide after primary reforming, rather than before primary reforming, enables the steam ratio to be reduced by about 0.2, e.g. from about 0.9 to about 0.7, before there is a serious risk of carbon deposition.
  • a mixture of a desulphurised hydrocarbon feedstock, for example natural gas, and steam is fed, typically at a pressure in the range 10 to 50 bar abs., via line 10 to a heat exchanger 12 and thence, via line 14, to the catalyst-containing tubes 16 of a heat exchange reformer 18.
  • the mixture is typically heated to a temperature in the range 350 to 550°C prior to entry into the tubes 16.
  • a temperature in the range 350 to 550°C prior to entry into the tubes 16.
  • only one tube is shown in the drawing: in practice there may be several tens or hundreds of such tubes.
  • the feedstock/steam mixture undergoes primary steam reforming in the tubes 16 and the primary reformed gas leaves the heat exchange reformer 18 via line 20, typically at a temperature in the range 600 to 800°C.
  • the primary reformed gas is mixed with Fischer- Tropsch tail gas (to be described) fed via line 22 and the mixture is fed via line 24 to a secondary reformer 26, to which oxygen is supplied via line 28.
  • the primary reformed gas/tail gas mixture is partially combusted in the secondary reformer and brought towards equilibrium by passage over a secondary reforming catalyst.
  • the secondary reformed gas leaves secondary reformer via line 30, typically at a temperature in the range 850 to 1150°C.
  • Heat is recovered from the hot secondary reformed gas by passing the secondary reformed gas via line 30 to the shell side of the heat exchange reformer 18 so that the secondary reformed gas forms the heating medium of the heat exchange reformer.
  • the secondary reformed gas is thus cooled by heat exchange with the gas undergoing reforming in the tubes 16 and leaves the heat exchange reformer via line 32, typically at a temperature 50 to 150°C above the temperature at which the hydrocarbon feedstock/steam mixture is fed to the tubes 16.
  • the partially cooled secondary reformed gas is then cooled further with heat recovery in one or more heat exchangers 34 to a temperature below the dew point of the water in the secondary reformed gas.
  • the cooled secondary reformed gas is then fed via line 36 to a separator 38 wherein condensed water is separated as a liquid water stream 40. This water can be recycled by heating it and contacting the hydrocarbon feedstock with the resultant hot water in a saturator to provide the feedstock/steam mixture.
  • the remaining de-watered gas is then fed, via line 42, to an optional hydrogen separation unit 44, e.g. a membrane unit or a pressure swing adsorption stage, to separate part of the hydrogen in the de-watered gas as a hydrogen stream 46.
  • an optional hydrogen separation unit 44 e.g. a membrane unit or a pressure swing adsorption stage
  • the resultant gas is then fed via line 48 to a Fischer-Tropsch synthesis stage 50, wherein liquid hydrocarbons are synthesised and are separated, together with by-product water, as a product stream 52 leaving a tail gas stream 54.
  • Part of the tail gas is purged as stream 56 to avoid a build up of inerts, e.g. nitrogen which may be present in the hydrocarbon feedstock as a contaminant and/or is often present in small amounts as an impurity in the oxygen used for the partial combustion.
  • the purged tail gas may be used as fuel, for example in a fired heater heating the mixture of hydrocarbon and steam fed to the heat exchange reformer.
  • the remainder of the tail gas is fed to a compressor 58 and then to a heat exchanger 60 and then fed via line 22 to be mixed with the primary reformed gas.
  • the amount of oxygen required is 3360 kmol/h, i.e. an increase of 2.8%, or, if the amount of oxygen is not increased, the heat transfer area in the heat exchange reformer has to be increased in size by 25%.

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  • Inorganic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

Selon l'invention, on peut obtenir un gaz de synthèse destiné à être utilisé dans un procédé Fischer-Tropsch en soumettant une charge d'hydrocarbures à un reformage primaire à la vapeur dans des tubes d'un reformeur à échange thermique, en soumettant ensuite le gaz de reformage primaire à un reformage secondaire, puis en utilisant le gaz chaud de reformage secondaire pour chauffer les tubes dans le reformeur à échange thermique. Le gaz de reformage obtenu est refroidi, déshydraté et utilisé pour former des hydrocarbures selon un procédé Fischer-Tropsch. On recycle au moins une partie des gaz résiduaires issus du procédé Fischer-Tropsch en les ajoutant au gaz de reformage primaire avant le reformage secondaire.
PCT/GB2002/003311 2001-08-17 2002-07-19 Production d'hydrocarbures WO2003016250A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
EA200400320A EA005280B1 (ru) 2001-08-17 2002-07-19 Производство углеводородов
AU2002317369A AU2002317369B2 (en) 2001-08-17 2002-07-19 Production of hydrocarbons
NO20040665A NO335117B1 (no) 2001-08-17 2004-02-16 Fremgangsmåte for fremstilling av hydrokarboner ved Fischer-Tropsch reaksjon

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB0120071.6 2001-08-17
GBGB0120071.6A GB0120071D0 (en) 2001-08-17 2001-08-17 Steam reforming

Publications (1)

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WO2003016250A1 true WO2003016250A1 (fr) 2003-02-27

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AU (1) AU2002317369B2 (fr)
EA (1) EA005280B1 (fr)
GB (1) GB0120071D0 (fr)
MY (1) MY129743A (fr)
NO (1) NO335117B1 (fr)
WO (1) WO2003016250A1 (fr)
ZA (1) ZA200400794B (fr)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1413547A1 (fr) * 2002-09-26 2004-04-28 Haldor Topsoe A/S Procédé pour la production de gas de synthèse
WO2004041716A1 (fr) * 2002-11-07 2004-05-21 Johnson Matthey Plc Production d'hydrocarbures
WO2004096952A1 (fr) * 2003-05-02 2004-11-11 Johnson Matthey Plc Production d'hydrocarbures par reformage a la vapeur et reaction de fischer-tropsch
GB2407818A (en) * 2003-10-20 2005-05-11 Johnson Matthey Plc Steam reforming process
EP1698590A1 (fr) * 2005-03-04 2006-09-06 Ammonia Casale S.A. Procédé et installation de reformage pour la production de gaz de synthèse
WO2010105786A1 (fr) 2009-03-16 2010-09-23 Saudi Basic Industries Corporation Procédé de production d'un mélange d'hydrocarbures aliphatiques et aromatiques
WO2012084135A1 (fr) * 2010-12-22 2012-06-28 Haldor Topsøe A/S Procédé pour le reformage d'hydrocarbures
CN101709226B (zh) * 2009-12-02 2012-10-03 中国石油集团工程设计有限责任公司抚顺分公司 一种费托合成循环气脱二氧化碳及烃类回收工艺
GB2494751A (en) * 2011-09-15 2013-03-20 Johnson Matthey Plc Improved hydrocarbon production process
WO2017194427A1 (fr) * 2016-05-12 2017-11-16 Thyssenkrupp Industrial Solutions Ag Procédé pour former un gaz de synthèse
GB2551314A (en) * 2016-06-06 2017-12-20 Energy Tech Institute Llp Equilibium approach reactor
WO2018046590A1 (fr) * 2016-09-09 2018-03-15 Shell Internationale Research Maatschappij B.V. Procédé de préparation d'hydrogène

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DE739569C (de) * 1937-04-15 1943-10-04 Braunkohle Benzin Ag Verfahren zur Durchfuehrung der katalytischen Kohlenwasserstoffsynthese aus Co und Hnach Fischer-Tropsch
GB2168719A (en) * 1984-10-29 1986-06-25 Humphreys & Glasgow Ltd Producing synthesis gas
WO2000009441A2 (fr) * 1998-08-13 2000-02-24 Imperial Chemical Industries Plc Reformage a la vapeur
WO2001042175A1 (fr) * 1999-12-09 2001-06-14 Den Norske Stats Oljeselskap As Integration optimale de la synthese de fischer-tropsch et production de gaz de synthese

Patent Citations (4)

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Publication number Priority date Publication date Assignee Title
DE739569C (de) * 1937-04-15 1943-10-04 Braunkohle Benzin Ag Verfahren zur Durchfuehrung der katalytischen Kohlenwasserstoffsynthese aus Co und Hnach Fischer-Tropsch
GB2168719A (en) * 1984-10-29 1986-06-25 Humphreys & Glasgow Ltd Producing synthesis gas
WO2000009441A2 (fr) * 1998-08-13 2000-02-24 Imperial Chemical Industries Plc Reformage a la vapeur
WO2001042175A1 (fr) * 1999-12-09 2001-06-14 Den Norske Stats Oljeselskap As Integration optimale de la synthese de fischer-tropsch et production de gaz de synthese

Cited By (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1413547A1 (fr) * 2002-09-26 2004-04-28 Haldor Topsoe A/S Procédé pour la production de gas de synthèse
AU2003276396B2 (en) * 2002-11-07 2008-06-26 Johnson Matthey Plc Production of hydrocarbons
WO2004041716A1 (fr) * 2002-11-07 2004-05-21 Johnson Matthey Plc Production d'hydrocarbures
US7314891B2 (en) 2002-11-07 2008-01-01 Johnson Matthey Plc Production of hydrocarbons
WO2004096952A1 (fr) * 2003-05-02 2004-11-11 Johnson Matthey Plc Production d'hydrocarbures par reformage a la vapeur et reaction de fischer-tropsch
AU2004234588B2 (en) * 2003-05-02 2009-04-09 Johnson Matthey Plc Production of hydrocarbons by steam reforming and Fischer-Tropsch reaction
EA008048B1 (ru) * 2003-05-02 2007-02-27 Джонсон Мэтти Плс Получение углеводородов путём риформинга с водяным паром и реакции фишера-тропша
US7323497B2 (en) 2003-05-02 2008-01-29 Johnson Matthey Plc Production of hydrocarbons by steam reforming and Fischer-Tropsch reaction
GB2407818A (en) * 2003-10-20 2005-05-11 Johnson Matthey Plc Steam reforming process
GB2407818B (en) * 2003-10-20 2005-11-30 Johnson Matthey Plc Steam reforming process
US9039795B2 (en) 2005-03-04 2015-05-26 Casale Sa Reforming process for synthesis gas production and related plant
WO2006094618A1 (fr) * 2005-03-04 2006-09-14 Ammonia Casale S.A. Procede de reformage destine a la production d’un gaz de synthese et installation correspondante
EP1698590A1 (fr) * 2005-03-04 2006-09-06 Ammonia Casale S.A. Procédé et installation de reformage pour la production de gaz de synthèse
US8609738B2 (en) 2009-03-16 2013-12-17 Saudi Basic Industries Corporation Process for producing a mixture of aliphatic and aromatic hydrocarbons
WO2010105786A1 (fr) 2009-03-16 2010-09-23 Saudi Basic Industries Corporation Procédé de production d'un mélange d'hydrocarbures aliphatiques et aromatiques
CN101709226B (zh) * 2009-12-02 2012-10-03 中国石油集团工程设计有限责任公司抚顺分公司 一种费托合成循环气脱二氧化碳及烃类回收工艺
WO2012084135A1 (fr) * 2010-12-22 2012-06-28 Haldor Topsøe A/S Procédé pour le reformage d'hydrocarbures
US9067850B2 (en) 2011-09-15 2015-06-30 Johnson Matthey Public Limited Company Synthesis gas and Fischer Tropsch integrated process
WO2013038140A1 (fr) 2011-09-15 2013-03-21 Johnson Matthey Public Limited Company Gaz de synthèse et procédé intégré de fischer-tropsch
GB2494751A (en) * 2011-09-15 2013-03-20 Johnson Matthey Plc Improved hydrocarbon production process
GB2494751B (en) * 2011-09-15 2016-03-23 Johnson Matthey Plc Improved hydrocarbon production process
WO2017194427A1 (fr) * 2016-05-12 2017-11-16 Thyssenkrupp Industrial Solutions Ag Procédé pour former un gaz de synthèse
GB2551314A (en) * 2016-06-06 2017-12-20 Energy Tech Institute Llp Equilibium approach reactor
US10843163B2 (en) 2016-06-06 2020-11-24 Kew Technology Limited Equilibrium approach reactor
GB2551314B (en) * 2016-06-06 2021-03-17 Kew Tech Limited Equilibium approach reactor
WO2018046590A1 (fr) * 2016-09-09 2018-03-15 Shell Internationale Research Maatschappij B.V. Procédé de préparation d'hydrogène
US11161738B2 (en) 2016-09-09 2021-11-02 Shell Oil Company Process for the preparation of hydrogen

Also Published As

Publication number Publication date
EA005280B1 (ru) 2004-12-30
AU2002317369B2 (en) 2007-01-25
MY129743A (en) 2007-04-30
NO20040665L (no) 2004-02-16
NO335117B1 (no) 2014-09-15
ZA200400794B (en) 2004-10-13
GB0120071D0 (en) 2001-10-10
EA200400320A1 (ru) 2004-08-26

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