WO2009152895A1 - Verfahren zum betreiben einer fischer-tropsch-synthese - Google Patents

Verfahren zum betreiben einer fischer-tropsch-synthese Download PDF

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Publication number
WO2009152895A1
WO2009152895A1 PCT/EP2009/003250 EP2009003250W WO2009152895A1 WO 2009152895 A1 WO2009152895 A1 WO 2009152895A1 EP 2009003250 W EP2009003250 W EP 2009003250W WO 2009152895 A1 WO2009152895 A1 WO 2009152895A1
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WO
WIPO (PCT)
Prior art keywords
gas
fischer
tropsch synthesis
synthesis unit
gas stream
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/EP2009/003250
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German (de)
English (en)
French (fr)
Inventor
Johannes Menzel
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ThyssenKrupp Industrial Solutions AG
Original Assignee
Uhde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority to RU2010153594/04A priority Critical patent/RU2503706C2/ru
Priority to AU2009259740A priority patent/AU2009259740A1/en
Priority to DK09765475.0T priority patent/DK2294162T3/da
Priority to BRPI0913206A priority patent/BRPI0913206A2/pt
Priority to US12/992,090 priority patent/US8741971B2/en
Priority to PL09765475T priority patent/PL2294162T3/pl
Priority to CA2725898A priority patent/CA2725898A1/en
Priority to CN200980119588XA priority patent/CN102066526A/zh
Priority to EP09765475A priority patent/EP2294162B1/de
Priority to ES09765475T priority patent/ES2382173T3/es
Application filed by Uhde GmbH filed Critical Uhde GmbH
Priority to JP2011510860A priority patent/JP5607612B2/ja
Priority to AT09765475T priority patent/ATE541914T1/de
Publication of WO2009152895A1 publication Critical patent/WO2009152895A1/de
Anticipated expiration legal-status Critical
Priority to ZA2010/08544A priority patent/ZA201008544B/en
Ceased legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen; Reversible storage of hydrogen
    • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
    • C01B3/06—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen with inorganic reducing agents
    • C01B3/12—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • 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
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
    • C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
    • 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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415—Purification by absorption in liquids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—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
    • C01B2203/0465—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
    • C01B2203/04—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
    • 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
    • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
    • C01B2203/86—Carbon dioxide sequestration
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1618—Modification of synthesis gas composition, e.g. to meet some criteria
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1659—Conversion of synthesis gas to chemicals to liquid hydrocarbons
    • 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
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • 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
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • 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
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry

Definitions

  • the invention relates to a method for operating a Fischer-Tropsch synthesis.
  • FTS unit Fischer-Tropsch synthesis unit
  • H 2 : CO molar ratio of about 2: 1 in terms to strive for an optimal yield.
  • part of the FTS product gas is compressed and returned to the feed gas stream.
  • the recirculation ratio is chosen so that up to twice the amount of the feed gas are recirculated.
  • the recirculation ratio is limited by the fact that the proportion of inert gases, such as nitrogen, argon and carbon dioxide (CO 2 ), increases successively by repeated recycling, as a result of which further repatriation is not economically viable.
  • the H 2 : CO molar ratio of a synthesis gas obtained from the coal gasification is about 1: 3 and is thus in principle unsuitable for direct feeding into a Fischer-Tropsch synthesis reactor.
  • a partial stream of the raw gas is therefore processed before being fed to the AGVS, the process gas pretreatment essentially consisting of a desulfurization stage and a CO conversion stage.
  • sulfur-containing conversion sour shift
  • desulfurized conversion sweet shift
  • a partial flow of the FTS residual gas is usually supplied to an energy recovery stage to improve the energy balance.
  • electricity is generated by means of one or more gas turbines in combination with one or more generators, which is made available to the system during operation again.
  • the invention has for its object to provide a method by which the yield of the gas used from the coal gasification can be improved without the expenditure on equipment would be much higher than that required for the prior art.
  • the invention and solution to this problem is a method according to claim 1.
  • a crude gas containing CO and H 2 is desulfurized from a coal gasification and then fed directly as feed gas of a Fischer-Tropsch synthesis unit in which by catalytic reactions of carbon oxides and hydrogen hydrocarbons are formed.
  • the hydrocarbons are separated as liquid products.
  • a CO and CO 2 -containing gas stream leaving the FTS synthesis unit is compressed and fed to a conversion stage in which CO is converted with water vapor into H 2 and CO 2 .
  • the gas leaving the conversion stage is returned to the Fischer-Tropsch synthesis unit as H 2 -rich gas together with the desulfurized feed gas after a gas treatment in which CO 2 and / or further constituents apart from H 2 are removed. It proves to be advantageous in this case that the expense for the desulfurization is reduced by the direct supply of desulfurized raw gas, since only unconverted gas is to be desulfurized.
  • the CO content of the process gas when entering the conversion stage is below 20% due to the process. Therefore, it is sufficient to equip the conversion stage with only one reactor. In conventional methods, the CO content is more than 50% when entering the conversion stage, so that there for conversion a second reactor and a heat exchanger are required.
  • a partial stream of the desulfurized feed gas can be branched off and fed to the recirculated gas stream upstream of the compressor. In this way, the H 2 content in the gas stream that is fed to the FTS reactor can be increased.
  • a H 2 : CO molar ratio of at least 1, 5: 1 is set.
  • a 2: 1 ratio is preferred in terms of FTS product yield.
  • the gas treatment of the gas stream leaving the conversion stage can consist of a gas scrubber.
  • This procedure according to the invention enables a higher crude gas yield, since the CO2 produced in the FTS unit is almost completely removed from the FTS recycle gas, as a result of which the circulating gas stream is reduced.
  • This allows over previous process concepts, a higher concentration of inert gas constituents in the process gas, which then leads to the CO and H 2 concentrations in personallyschleusenden residual gas from the Fischer-Tropsch synthesis is significantly lower than previous concepts.
  • a partial stream is discharged from the gas stream, which leaves the synthesis unit, in order to avoid that slight hydrocarbons and inert gas components accumulate too much.
  • the discharged partial flow is fed to the energy recovery of a gas turbine.
  • the power generation with a steam turbine which is preceded by a waste heat boiler and a steam generator, has the further advantage that in case of failure of the coal gasification, the power supply through the energy recovery stage could be ensured by using an alternative fuel with high availability.
  • a small pressure swing adsorption plant required for conventional process concepts for producing H 2 for the hydrogenation of the heavy Fischer-Tropsch products is dispensed with. It may further be provided that the gas flow leaving the pressure swing adsorption is compressed and subsequently supplied to a gas turbine.
  • the subject of the invention is a plant for operating a Fischer-Tropsch synthesis.
  • Its basic design includes a Fischer-Tropsch synthesis unit comprising a Fischer-Tropsch synthesis reactor, a liquid product separation, and a heavy-end recovery unit.
  • To construct the system according to the invention also includes an upstream device for desulfurization of a gas generated by coal gasification, CO and H 2 containing raw gas and a recycling device for returning a Fischer Tropsch synthesis unit leaving the gas stream in the Fischer-Tropsch synthesis unit supplied, desulfurized feed gas.
  • the return device has to return the Gas stream a compressor, a steam-powered converter for converting CO into H 2 and CO 2 and a device for removing CO 2 from the recirculated gas stream on.
  • the device for returning the gas stream is connected by a branch line to a line carrying the desulfurized feed gas, wherein the branch line is connected upstream of the compressor to the return device. It allows, for example, when starting up the system to direct a small partial flow from the desulfurized raw gas directly into the conversion stage until sufficient FTS product gas is present.
  • the device for removing CO 2 has a gas scrubber, wherein the gas scrubber can optionally be operated with a physical solvent.
  • the device for removing CO 2 has an alternately operated adsorber for pressure swing adsorption. It can be provided that the pressure swing adsorption is preceded by a gas washing, whereby a separation of CO 2 for CO 2 sequestration is possible.
  • FIG. 2 shows a process diagram with an adsorber for a pressure swing adsorption.
  • the process according to the invention basically includes that a raw gas containing CO and H 2 first desulfurized from a coal gasification 1 in a desulfurization device 2 and then fed as feed gas with a H 2 : CO ratio of at least 1.5: 1 to a Fischer-Tropsch synthesis unit 3 in which hydrocarbons are formed by catalytic reactions which are separated as liquid products 4.
  • the CO- and CO 2 -containing gas stream leaving the Fischer-Tropsch synthesis unit 3 is compressed in a compressor 5 and then fed to a converter 6 in which CO is converted into H 2 and CO 2 with steam by a sweet-shift method , From there, the gas stream is fed to a gas treatment in which CO 2 is removed.
  • the H 2 -rich process gas is recycled together with the desulfurized feed gas into the Fischer-Tropsch synthesis unit 3.
  • a branch line equipped with a valve 8 8 a partial stream of the desulfurized feed gas is branched off and fed to the compressor 5 in the circulated gas stream.
  • the gas treatment of the gas stream leaving the conversion stage consists of a scrubber 9.
  • the CO 2 is removed from the process as waste gas 10.
  • a partial stream is discharged and supplied to the energy of a gas turbine 11, which is connected to a generator module 12.
  • this gas turbine can also be preceded by a heavy-end recovery unit.
  • the remaining in the energy recovery gas is discharged as process exhaust gas 13.
  • the process illustrated in FIG. 2 shows that the gas treatment of the gas stream leaving the conversion stage 6 consists of a pressure swing adsorption, wherein essentially pure hydrogen is obtained on the pressure side of an adsorber 14, which mixture is mixed with the feed gas and recycled to the Fischer-Tropsch synthesis unit 3. In this case also falls on a lower pressure level, a gas mixture, which is used to generate steam in a waste heat boiler, with the power generation, a steam turbine is driven, which is connected to a generator module 12. The process exhaust gas 13 is removed from the energy recovery stage.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Industrial Gases (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Fats And Perfumes (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Detergent Compositions (AREA)
PCT/EP2009/003250 2008-05-28 2009-05-07 Verfahren zum betreiben einer fischer-tropsch-synthese Ceased WO2009152895A1 (de)

Priority Applications (13)

Application Number Priority Date Filing Date Title
EP09765475A EP2294162B1 (de) 2008-05-28 2009-05-07 Verfahren zum betreiben einer fischer-tropsch-synthese
DK09765475.0T DK2294162T3 (da) 2008-05-28 2009-05-07 Fremgangsmåde til brug af en fischer-tropsch-syntese
BRPI0913206A BRPI0913206A2 (pt) 2008-05-28 2009-05-07 método para operação de uma síntese de fischer-tropsch
US12/992,090 US8741971B2 (en) 2008-05-28 2009-05-07 Method for operating a Fischer-Tropsch synthesis
PL09765475T PL2294162T3 (pl) 2008-05-28 2009-05-07 Sposób wykonywania syntezy Fischera-Tropscha
CA2725898A CA2725898A1 (en) 2008-05-28 2009-05-07 Method of running a fischer-tropsch synthesis
CN200980119588XA CN102066526A (zh) 2008-05-28 2009-05-07 运行费托合成的方法
RU2010153594/04A RU2503706C2 (ru) 2008-05-28 2009-05-07 Способ осуществления синтеза фишера-тропша
AU2009259740A AU2009259740A1 (en) 2008-05-28 2009-05-07 Method for operating a Fischer-Tropsch synthesis
ES09765475T ES2382173T3 (es) 2008-05-28 2009-05-07 Procedimiento para realizar una síntesis de Fischer-Tropsch
JP2011510860A JP5607612B2 (ja) 2008-05-28 2009-05-07 フィッシャー−トロプシュ合成を操業する方法
AT09765475T ATE541914T1 (de) 2008-05-28 2009-05-07 Verfahren zum betreiben einer fischer-tropsch- synthese
ZA2010/08544A ZA201008544B (en) 2008-05-28 2010-11-29 Method for operating a fischer-tropsch synthesis

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102008025577.7 2008-05-28
DE102008025577A DE102008025577A1 (de) 2008-05-28 2008-05-28 Verfahren zum Betreiben einer Fischer-Tropsch-Synthese

Publications (1)

Publication Number Publication Date
WO2009152895A1 true WO2009152895A1 (de) 2009-12-23

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Country Status (16)

Country Link
US (1) US8741971B2 (https=)
EP (1) EP2294162B1 (https=)
JP (1) JP5607612B2 (https=)
KR (1) KR20110021940A (https=)
CN (1) CN102066526A (https=)
AT (1) ATE541914T1 (https=)
AU (1) AU2009259740A1 (https=)
BR (1) BRPI0913206A2 (https=)
CA (1) CA2725898A1 (https=)
DE (1) DE102008025577A1 (https=)
DK (1) DK2294162T3 (https=)
ES (1) ES2382173T3 (https=)
PL (1) PL2294162T3 (https=)
RU (1) RU2503706C2 (https=)
WO (1) WO2009152895A1 (https=)
ZA (1) ZA201008544B (https=)

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CN102746870A (zh) * 2012-06-19 2012-10-24 中国石油化工股份有限公司 一种费托合成工艺

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EP2530136B1 (en) * 2011-05-30 2020-04-01 Neste Oyj Method of producing a hydrocarbon composition
CN105460890B (zh) * 2015-12-03 2018-03-13 东华工程科技股份有限公司 一种煤制油项目油洗干气经膜分离后的膜分离非渗透气转化制氢的方法
CN112410078A (zh) * 2020-11-04 2021-02-26 山东义丰环保机械股份有限公司 一种用于煤气的脱硫设备
JP7361142B2 (ja) * 2022-01-12 2023-10-13 本田技研工業株式会社 燃料合成装置
CN117339487A (zh) * 2023-09-26 2024-01-05 清华大学 一种将合成气高效转化的反应装置与方法

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CA2725898A1 (en) 2009-12-23
US20110118366A1 (en) 2011-05-19
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ZA201008544B (en) 2012-03-28
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