WO2006117499A1 - Procede de fabrication d'un gaz de synthese - Google Patents

Procede de fabrication d'un gaz de synthese Download PDF

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Publication number
WO2006117499A1
WO2006117499A1 PCT/GB2005/001672 GB2005001672W WO2006117499A1 WO 2006117499 A1 WO2006117499 A1 WO 2006117499A1 GB 2005001672 W GB2005001672 W GB 2005001672W WO 2006117499 A1 WO2006117499 A1 WO 2006117499A1
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Prior art keywords
synthesis gas
reformer
gas
production
synthesis
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PCT/GB2005/001672
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English (en)
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Alexander H. Quartey-Papafio
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Quartey-Papafio Alexander H
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Priority to PCT/GB2005/001672 priority Critical patent/WO2006117499A1/fr
Publication of WO2006117499A1 publication Critical patent/WO2006117499A1/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
    • C01B3/382—Multi-step 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
    • C01B2203/0205—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
    • 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
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift 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
    • C01B2203/0435—Catalytic purification
    • C01B2203/0445—Selective methanation
    • 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
    • C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
    • 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
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling
    • C01B2203/0883—Methods of cooling by indirect heat exchange
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1258—Pre-treatment of the feed
    • C01B2203/1264—Catalytic pre-treatment of the feed
    • C01B2203/127—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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/141—At least two reforming, decomposition or partial oxidation steps in parallel
    • 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

  • This invention relates to a method of producing synthesis gas which when used as feedstock to the synthesis section of synthesis gas based plants such as Fischer-Tropsch, Methanol or Ammonia plants will enable significant increases in plant capacities coupled with improved plant efficiencies than currently achieved with present processes.
  • the synthesis gas production process employs three reforming technologies, arranged in a unique configuration to produce synthesis gas with the optimum composition for Fischer-Tropsch liquids, Methanol or Ammonia production.
  • Figure 1 outlines a simplified block flow diagram of producing synthesis gas using a Single Reforming Process (Prior Act).
  • Figure 2 outlines a simplified block flow diagram of producing synthesis gas using a Combined Reforming Process (Prior Act).
  • Figure 3 outlines a simplified block flow diagram of producing synthesis gas using the present invention.
  • the feedstock to the synthesis section of any synthesis gas based plant such as Fischer-Tropsch, Methanol or Ammonia plant is a gas containing H 2 , CO 2 , CO, CH 4 , N 2 and H 2 O.
  • This is coined synthesis gas or "syngas" and is produced by catalytic or non-catalytic processing a hydrocarbon based feedstock such as natural gas.
  • the reformer where the hydrocarbon based feedstock is chemically broken down into the said components using water vapour, oxygen, enriched air or atmospheric air. Examples of reforming technologies used presently in synthesis gas production processes include:
  • Hydrogen, hydrogen rich containing gas from the synthesis section of the plant in question or imported from an external source 102 is added to natural gas feedstock 101 and the mixture 103 is heated up and desulphurised in a typical Desulphurisation Unit 201 to remove any sulphur compounds present in the natural gas.
  • the desulphurised gas 104 is then fed to the Saturator 202 where it is contacted with hot water (not shown) and leaves saturated with water vapour 105.
  • Supplementary water vapour 106 is added to the saturated gas 105 to achieve a desired steam to carbon ratio.
  • the mixture 107 is heated up and routed to the Reformer 203 were the hydrocarbons present in the natural gas reforms to produce hydrogen, carbon monoxide and carbon dioxide in the presents of water vapour or oxygen from an oxygen containing stream 108 such as pure oxygen, enriched air or atmospheric air.
  • the reformed gas 109 is cooled down by generating high pressure water vapour and depending on the plant in question, conditioned by shifting carbon monoxide, removing carbon dioxide and/or methanating carbon oxides in 204.
  • the conditioned gas coined syngas 110 is cooled down further to remove water vapour in 205.
  • the conditioned gas is fed to a Desaturator 205 where it is contacted with cold water (not shown) to remove the water vapour 112 present in it.
  • the resulting dry gas 111 is fed to the synthesis section of a Fischer-Tropsch, Methanol or Ammonia Plant for further processing.
  • the mixture 107 is heated up and routed to the first of two reformers 203 where part of the hydrocarbons present in the natural gas reforms to produce hydrogen, carbon monoxide and carbon dioxide.
  • the partly reformed gas 108 is then fed to a second reformer 204 where the reforming process is completed using oxygen, enriched air or atmospheric air 109.
  • a portion of the desulphurised gas 104 or saturated gas 105 is mixed with the effluents from the first reformer 203 and introduced to the second reformer 204 where the mixture is processed to completion 110 using oxygen, enriched air or atmospheric air 109 as described earlier.
  • This alternative route has not been shown on Figure 2.
  • the reformed gas 110 from the second reformer 204 is routed to the first reformer 203 to provide the heat required for reforming and leaves colder as 111.
  • the cooled reformed gas or the reformed gas from the secondary reformer 112 is cooled down by generating high pressure water vapour and depending on the plant in question, conditioned by shifting carbon monoxide, removing carbon dioxide and or methanating carbon oxides in 205.
  • the conditioned gas coined syngas 113 is cooled down further to remove water vapour 115 in 206.
  • the resulting dry gas 114 is fed to the synthesis section of a Fischer-Tropsch, Methanol or Ammonia Plant for further processing.
  • the conditioned gas is fed to a Desaturator 206 where it is contacted with cold water (not shown) to remove the water vapour present in it.
  • the resulting dry gas 114 is fed to the synthesis section of the plants as described in the preceding paragraph for further processing.
  • the steam-methane, autothermal and partial oxidation reformers can be used in this reforming process with each other or with either the gas heated reformer or pre-reformer.
  • the maximum synthesis gas production from a single train of partial oxidation reformer will enable maximum plant production capacity (i.e. C 5 and above hydrocarbon) of about 8,000 BPD. This increases to 10,000 BPD for a steam-methane reformer scheme and to between 15,000 -17,000 BPD when an autothermal reformer is employed.
  • the pre-reformer and steam-methane reformer or autothermal combination route increases the methanol plant's production capacity to between 4500 - 5,000 MTPD. Plant's production capacity can be increased further to around 7,000 MTPD by employing the autothermal and gas heated reformer combination.
  • the synthesis production section of most of today's ammonia plants consists of a primary and secondary reformer arranged in series with the primary being a steam methane reformer and the secondary an autothermal reformer.
  • the steam methane reformers are smaller than those on methanol plants and thus not limiting, the size of the autothermal reformer limits the production of synthesis gas to that equivalent to a maximum ammonia plant capacity of between 2500 - 2800 MTPD.
  • the capacity of the biggest ammonia plant currently on stream is of the order of 2200 - 2500 MTPD.
  • Adiabatic Pre-Reformers are catalytic reactors which use part of the energy in the feed (i.e. hydrocarbon and steam mixture) introduced into it and the heat of any exothermic reaction of the reactants in the feed to reform heavier hydrocarbons and part of the methane present in the feed. No heat is added to or extracted from the reaction and hence the name adiabatic.
  • SMR Steam-Methane Reformers
  • the feed i.e. hydrocarbon and steam mixture
  • the heat required by the endothermic reforming reaction is supplied by orderly-arranged burners located either in the roof, floor or sidewalls of the furnace box.
  • Autothermal Reformers are catalytic reactors which use the heat from the highly exothermic hydrocarbon-oxygen combustion reaction to supply heat for the endothermic reforming reaction without the need for external heat.
  • the oxygen for the reaction is supplied either as pure oxygen, enriched air or as normal atmospheric air.
  • Partial Oxidation Reformers are either catalytic or non-catalytic reactors which use the heat from the highly exothermic hydrocarbon-oxygen combustion reaction to supply heat for the endothermic reforming reaction without the need for external heat.
  • the oxygen for the reaction is supplied either as pure oxygen, enriched air or as normal atmospheric air.
  • the present invention arranges the three reforming technologies namely APR, SMR and ATR (or POX) in a unique configuration, selects key process parameters such as steam to carbon ratios, flows and flow splits and fixes operating conditions of the reforming technologies to produce synthesis gas with the optimum composition for either Fischer- Tropsch Liquid, Methanol or Ammonia Production.
  • Hydrogen or hydrogen rich containing gas from the synthesis section of the plant in question or imported from an external source 102 is added to natural gas feedstock 101 from the plant's battery limit and the mixture 103 is heated up and desulphurised in a typical Desulphurisation Unit 201 on said plants to remove any sulphur compounds present in the natural gas.
  • the desulphurised gas 104 is sent to the Saturator 202 where it is contacted with hot water heated from other parts of the plant and leaves saturated 105 with water vapour.
  • Supplementary water vapour 106 is added to the saturated natural gas 105 to attain a desired steam to carbon ratio.
  • vapourised oxygenates from the synthesis section of the plant is added to the saturated gas prior to adding the supplementary steam.
  • the Saturator 202 can be omitted for all three plants and sufficient water vapour is added to the desulphurised gas to attain the same desired steam to carbon ratio as before.
  • the natural gas mixture with the desired steam to carbon ratio 107 is heated up and fed to the APR 203 where all the ethane and heavier hydrocarbons present are reformed together with some methane to hydrogen, carbon monoxide and carbon dioxide.
  • the resulting APR products 108 is split into two streams 110 and 116 and one stream 110 is fed to the SMR train.
  • the second stream 116 is fed to the ATR (or POX) train.
  • the SMR train consists of a heating train 204, a steam-methane reformer (SMR) 205 and a cooling train 206.
  • SMR steam-methane reformer
  • water vapour 111 is added to the portion of APR products 110 to obtain a desired steam to carbon ratio.
  • the mixture is heated up in the heating train 204 and fed to the SMR 205 for further reforming.
  • the effluents from the SMR 113 is cooled down in a series of heat exchangers in 206 by generating high pressure water vapour and heating up other parts of the process.
  • the resulting cooled gas 114 is added to the effluents from the ATR (or POX) train.
  • a fraction of the cooled SMR effluent 126 is cooled down further in 212 and the cooled gas 127 is fed to a Hydrogen Recovery Unit 213 together with purge gas 128 from the synthesis section of the plant in question to recover hydrogen gas 129.
  • the hydrogen gas 129 is added to the synthesis gas for conditioning.
  • the ATR (or POX ) train consists of a cooling/heating train 207, an Autothermal (ATR) or Partial Oxidation (POX) Reactor 208 and another cooling train 209.
  • the portion of the APR effluent fed to the ATR (or POX) train 116, if desired is heated up (or cooled down to recover water vapour and reheated) in 207.
  • the heated or reheated stream 117 is added to the tail gas from the synthesis section of the plant 118 and the mixture 119 is fed to the ATR or POX Reactor 208 where it is reformed further with oxygen or enriched air 120.
  • the heated or reheated stream 117 is fed to the ATR or POX Reactor 208 where it is reformed further with oxygen or enriched air 120.
  • the heated or reheated stream 117 is fed to the ATR or POX Reactor 208 where it is reformed further with atmospheric air or enriched air.
  • the effluents from the ATR or POX Reactor 208 is cooled down by generating high pressure water vapour before it is added to the effluents from the SMR as mentioned before.
  • the resulting mixture 123 is fed to the Syngas Conditioning Unit 210 where the gas is cooled down by generating high pressure water vapour, interchanging heat with other parts of the synthesis process in a series of exchangers to a desired temperature and depending on the type of Fischer-Tropsch technology being employed, removing part of the carbon dioxide in the reformed gas using a typical carbon dioxide removal unit.
  • Carbon dioxide removal units are proprietary technology and are commercially available from a number of companies world-wide.
  • the resulting mixture 123 is fed to the Syngas Conditioning Unit 210 where the gas is cooled down by generating high pressure water vapour and interchanging heat with other parts of the synthesis process in a series of exchangers to a desired temperature.
  • the resulting mixture 123 is fed to the Syngas Conditioning Unit 210 where the gas is cooled down by generating high pressure water vapour and processed further by Carbon Monoxide Shifting, Carbon Dioxide Removal and Methanation to eliminate all carbon oxides from the reformed gas.
  • the processed gas is then cooled down to a desired temperature by interchanging heat with other parts of the synthesis process in a series of exchangers. All these processing techniques are common on most ammonia plants.
  • the synthesis gas is fed to a Desaturator 211 where it is contacted with cooled water to cool the gas down and remove any condensate produced.
  • the resulting dry gas 125 from the Desaturator or K.O. Drum if required is conditioned further by added hydrogen gas 129 recovered from the small portion of synthesis gas and purge gas sent to the Hydrogen Recovery Unit 213 as described earlier.
  • the conditioned mixture 129 is fed to the synthesis section of the Fischer-Tropsch, Methanol or Ammonia Plant for processing.
  • the configuration of the reformers provides better control of the quantity of H 2 , CO, CO 2 and N 2 in the syngas thus permitting the production of syngas with the optimum composition for the particular synthesis gas based plant in question.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

L'invention concerne un procédé de fabrication d'un gaz de synthèse, employant trois technologies de reformage, à savoir le pré-reformage adiabatique (APR), le reformage à vapeur de méthane (SMR) et le reformage à oxydation partielle ou autotherme (POX ou ATR), disposées en une configuration unique, dans des conditions opératoires sélectionnées pour chaque reformeur et avec des paramètres clés fixés de manière à fabriquer un gaz de synthèse avec une composition optimisée pour la fabrication d'ammoniac, de méthanol ou de liquides Fischer-Tropsch.
PCT/GB2005/001672 2005-05-03 2005-05-03 Procede de fabrication d'un gaz de synthese WO2006117499A1 (fr)

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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010067077A1 (fr) * 2008-12-11 2010-06-17 Bp P.L.C. Raffinerie de gaz intégrée
CN102498060A (zh) * 2009-08-14 2012-06-13 沙特基础工业公司 用于生产甲醇的联合转化方法
WO2013015687A1 (fr) * 2011-07-26 2013-01-31 Stamicarbon B.V. Acting Under The Name Of Mt Innovation Center Procédé et système pour la production de mélanges de gaz riches en hydrogène
WO2013013895A1 (fr) * 2011-07-25 2013-01-31 Haldor Topsøe A/S Procédé de production de gaz de synthèse
WO2013062415A1 (fr) * 2011-10-26 2013-05-02 Stamicarbon B.V. Acting Under The Name Of Mt Innovation Center Procédé de production de syngaz pour la production de méthanol
WO2013095130A1 (fr) * 2011-12-19 2013-06-27 Stamicarbon B.V. Acting Under The Name Of Mt Innovation Center Procédé de production d'ammoniac et d'urée
US8889037B2 (en) 2011-02-01 2014-11-18 Kellogg Brown & Root Llc Systems and methods for producing syngas and products therefrom
US9132402B2 (en) 2009-08-20 2015-09-15 Kellogg Brown & Root Llc Apparatus, systems, and processes for producing syngas and products therefrom
WO2015177051A1 (fr) * 2014-05-21 2015-11-26 Thyssenkrupp Industrial Solutions Ag Production de gaz de synthèse avec deux reformeurs autothermes
US9321655B2 (en) 2009-08-20 2016-04-26 Kellogg Brown & Root Llc Systems and methods for producing syngas and products therefrom
DE102016002728A1 (de) 2016-03-08 2017-09-14 Linde Aktiengesellschaft Verfahren zur Erzeugung von Synthesegas

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0504471A1 (fr) * 1989-12-11 1992-09-23 The M. W. Kellogg Company Procédé de réformage à la vapeur autotherme
EP0522744A2 (fr) * 1991-07-09 1993-01-13 Imperial Chemical Industries Plc Production de gaz de synthese
US20010006615A1 (en) * 1998-11-03 2001-07-05 Marco Badano Process for the production of synthesis gas
WO2001060773A1 (fr) * 2000-02-15 2001-08-23 Syntroleum Corporation Systeme et procede de preparation d'un flux de gaz de synthese et de conversion d'hydrocarbures
US20010047040A1 (en) * 1999-03-30 2001-11-29 Syntroleum Corporation, Delaware Corporation System and method for converting light hydrocarbons into heavier hydrocarbons with a plurality of synthesis gas subsystems
EP1219566A1 (fr) * 2000-12-27 2002-07-03 L'air Liquide, S.A. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et dispositif intégré pour la production de gaz de synthèse
US6444712B1 (en) * 2000-09-28 2002-09-03 Exxonmobil Chemical Patents, Inc. Methanol, olefin, and hydrocarbon synthesis process
EP1403216A1 (fr) * 2002-09-26 2004-03-31 Haldor Topsoe A/S Procédé pour la préparation de gaz de synthèse

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0504471A1 (fr) * 1989-12-11 1992-09-23 The M. W. Kellogg Company Procédé de réformage à la vapeur autotherme
EP0522744A2 (fr) * 1991-07-09 1993-01-13 Imperial Chemical Industries Plc Production de gaz de synthese
US20010006615A1 (en) * 1998-11-03 2001-07-05 Marco Badano Process for the production of synthesis gas
US20010047040A1 (en) * 1999-03-30 2001-11-29 Syntroleum Corporation, Delaware Corporation System and method for converting light hydrocarbons into heavier hydrocarbons with a plurality of synthesis gas subsystems
WO2001060773A1 (fr) * 2000-02-15 2001-08-23 Syntroleum Corporation Systeme et procede de preparation d'un flux de gaz de synthese et de conversion d'hydrocarbures
US6444712B1 (en) * 2000-09-28 2002-09-03 Exxonmobil Chemical Patents, Inc. Methanol, olefin, and hydrocarbon synthesis process
EP1219566A1 (fr) * 2000-12-27 2002-07-03 L'air Liquide, S.A. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et dispositif intégré pour la production de gaz de synthèse
EP1403216A1 (fr) * 2002-09-26 2004-03-31 Haldor Topsoe A/S Procédé pour la préparation de gaz de synthèse

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WO2010067077A1 (fr) * 2008-12-11 2010-06-17 Bp P.L.C. Raffinerie de gaz intégrée
RU2524720C2 (ru) * 2008-12-11 2014-08-10 Бп П.Л.К. Комплексная установка для переработки газа
US9079770B2 (en) 2009-08-14 2015-07-14 Saudi Basic Industries Corporation Combined reforming process for methanol production
CN102498060A (zh) * 2009-08-14 2012-06-13 沙特基础工业公司 用于生产甲醇的联合转化方法
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US9321655B2 (en) 2009-08-20 2016-04-26 Kellogg Brown & Root Llc Systems and methods for producing syngas and products therefrom
US9132402B2 (en) 2009-08-20 2015-09-15 Kellogg Brown & Root Llc Apparatus, systems, and processes for producing syngas and products therefrom
US8889037B2 (en) 2011-02-01 2014-11-18 Kellogg Brown & Root Llc Systems and methods for producing syngas and products therefrom
WO2013013895A1 (fr) * 2011-07-25 2013-01-31 Haldor Topsøe A/S Procédé de production de gaz de synthèse
EA030740B1 (ru) * 2011-07-26 2018-09-28 СТАМИКАРБОН Б.В. ЭКТИНГ АНДЕР ДЗЕ НЕЙМ ОФ ЭмТи ИННОВЕЙШН СЕНТЕР Способ для производства богатых водородом газовых смесей
US9932229B2 (en) 2011-07-26 2018-04-03 Stamicarbon B.V. Method and system for production of hydrogen rich gas mixtures
WO2013015687A1 (fr) * 2011-07-26 2013-01-31 Stamicarbon B.V. Acting Under The Name Of Mt Innovation Center Procédé et système pour la production de mélanges de gaz riches en hydrogène
US9102532B2 (en) 2011-10-26 2015-08-11 Stamicarbon B.V. Method for producing synthesis gas for methanol production
WO2013062415A1 (fr) * 2011-10-26 2013-05-02 Stamicarbon B.V. Acting Under The Name Of Mt Innovation Center Procédé de production de syngaz pour la production de méthanol
EA026825B1 (ru) * 2011-10-26 2017-05-31 Стамикарбон Б.В. Эктин Андер Те Нейм Оф Мт Инновейшн Сентр Способ получения синтез-газа для производства метанола
WO2013095130A1 (fr) * 2011-12-19 2013-06-27 Stamicarbon B.V. Acting Under The Name Of Mt Innovation Center Procédé de production d'ammoniac et d'urée
US9340494B2 (en) 2011-12-19 2016-05-17 Stamicarbon B.V. Acting Under The Name Of Mt Innovation Center Process for producing ammonia and urea
CN104105657B (zh) * 2011-12-19 2017-05-10 代表Mt创新中心的斯塔米卡邦有限公司 用于制备氨和尿素的方法
EA027871B1 (ru) * 2011-12-19 2017-09-29 Стамикарбон Б.В. Эктин Андер Те Нейм Оф Мт Инновейшн Сентр Способ получения аммиака и мочевины
US20140364647A1 (en) * 2011-12-19 2014-12-11 Stamicarbon B.V. Acting Under The Name Of Mt Innovation Center Process for producing ammonia and urea
CN104105657A (zh) * 2011-12-19 2014-10-15 代表Mt创新中心的斯塔米卡邦有限公司 用于制备氨和尿素的方法
EP3378832B1 (fr) * 2011-12-19 2024-05-08 Stamicarbon B.V. acting under the name of MT Innovation Center Procédé amélioré de production d'urée
WO2015177051A1 (fr) * 2014-05-21 2015-11-26 Thyssenkrupp Industrial Solutions Ag Production de gaz de synthèse avec deux reformeurs autothermes
DE102016002728A1 (de) 2016-03-08 2017-09-14 Linde Aktiengesellschaft Verfahren zur Erzeugung von Synthesegas
US9790433B2 (en) 2016-03-08 2017-10-17 Linde Aktiengesellschaft Process for producing synthesis gas

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