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RU2008102414A - METHOD FOR CONVERTING SYNTHESIS GAS TO HYDROCARBONS IN THE PRESENCE OF FOAM SIC - Google Patents

METHOD FOR CONVERTING SYNTHESIS GAS TO HYDROCARBONS IN THE PRESENCE OF FOAM SIC Download PDF

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Publication number
RU2008102414A
RU2008102414A RU2008102414/04A RU2008102414A RU2008102414A RU 2008102414 A RU2008102414 A RU 2008102414A RU 2008102414/04 A RU2008102414/04 A RU 2008102414/04A RU 2008102414 A RU2008102414 A RU 2008102414A RU 2008102414 A RU2008102414 A RU 2008102414A
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carried out
varies
silicon carbide
catalyst
operating conditions
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RU2008102414/04A
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RU2437918C2 (en
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Куонг ФАМ-ХУУ (FR)
Куонг Фам-Хуу
Беранж МАДАНИ (FR)
Беранж МАДАНИ
Максим ЛЯКРУА (FR)
Максим ЛЯКРУА
Ламиа ДРЭБИН (FR)
Ламиа ДРЭБИН
Марк-Жак ЛЕДУ (FR)
Марк-Жак Леду
Сабин САВИН-ПОНСЕ (FR)
Сабин САВИН-ПОНСЕ
Жак БУСКЕ (FR)
Жак Буске
Даниель ШВЕЙХ (FR)
Даниель ШВЕЙХ
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Тоталь С.А. (FR)
Тоталь С.А.
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74—Iron group metals
    • B01J23/75—Cobalt
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/20—Carbon compounds
    • B01J27/22—Carbides
    • B01J27/224—Silicon carbide
    • 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
    • C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Catalysts (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

1. Способ превращения монооксида углерода в углеводороды С2 + в присутствии водорода и металлсодержащего катализатора в реакторе, содержащем указанный катализатор, нанесенный на носитель на основе вспененного карбида кремния, осуществляемый в следующих рабочих условиях: ! WH (GHSV) изменяется от 100 до 5000 час-1 и ! WHSV изменяется от 1 до 100 час-1. ! 2. Способ превращения монооксида углерода в углеводороды C2 + в присутствии водорода и металлсодержащего катализатора в многотрубчатом реакторе, содержащем указанный катализатор, нанесенный на носитель, содержащий вспененный карбид кремния. ! 3. Способ по п.2, осуществляемый в следующих рабочих условиях: ! WH (GHSV) изменяется от 100 до 5000 час-1 и ! WHSV изменяется от 1 до 100 час-1. ! 4. Способ по п.1, в котором вспененный карбид кремния содержит более 50% мас. карбида кремния модификации бета. ! 5. Способ по п.1, в котором носитель катализатора содержит от 50 до практически 100% мас. карбида кремния модификации бета, предпочтительно, практически 100% мас. указанного карбида кремния. ! 6. Способ по п.1, в котором пена имеет отверстия пор в диапазоне 300-5000 мкм, преимущественно, 1000-3000 мкм. ! 7. Способ по п.1, в котором пена является твердой. ! 8. Способ по п.1, в котором открытая пористость вспененного SiC изменяется от 30 до 90%, в частности, от 50 до 85%. ! 9. Способ по п.1, осуществляемый в следующих рабочих условиях: ! WH (GHSV) изменяется от 150 до 2000 час-1 и ! WHSV изменяется от 1, преимущественно, от 5 до 50 час-1. ! 10. Способ по п.1, осуществляемый в следующих рабочих условиях: ! производительность по углеводородам выше 3 час-1 и ! производительность по углеводороду С4+ выше 3 час-1. ! 11. Способ по п.1, осуществляемый в следующих рабочих условиях: ! произ1. The method of converting carbon monoxide to C2 + hydrocarbons in the presence of hydrogen and a metal-containing catalyst in a reactor containing the specified catalyst deposited on a carrier based on foamed silicon carbide, carried out under the following operating conditions:! WH (GHSV) varies from 100 to 5000 h-1 and! WHSV varies from 1 to 100 hr-1. ! 2. A method for converting carbon monoxide to C2 + hydrocarbons in the presence of hydrogen and a metal-containing catalyst in a multi-tube reactor containing said catalyst supported on a carrier containing foamed silicon carbide. ! 3. The method according to claim 2, carried out in the following operating conditions:! WH (GHSV) varies from 100 to 5000 h-1 and! WHSV varies from 1 to 100 hr-1. ! 4. The method according to claim 1, in which the foamed silicon carbide contains more than 50% wt. silicon carbide modification beta. ! 5. The method according to claim 1, in which the catalyst carrier contains from 50 to almost 100% wt. silicon carbide modification beta, preferably almost 100% wt. specified silicon carbide. ! 6. The method according to claim 1, in which the foam has pore openings in the range of 300-5000 microns, preferably 1000-3000 microns. ! 7. The method according to claim 1, in which the foam is solid. ! 8. The method according to claim 1, in which the open porosity of the foamed SiC varies from 30 to 90%, in particular from 50 to 85%. ! 9. The method according to claim 1, carried out in the following operating conditions:! WH (GHSV) varies from 150 to 2,000 h-1 and! WHSV varies from 1, mainly from 5 to 50 hr-1. ! 10. The method according to claim 1, carried out in the following operating conditions:! hydrocarbon productivity is above 3 h-1 and! C4 + hydrocarbon productivity is higher than 3 h-1. ! 11. The method according to claim 1, carried out in the following operating conditions:! production

Claims (23)

1. Способ превращения монооксида углерода в углеводороды С2 + в присутствии водорода и металлсодержащего катализатора в реакторе, содержащем указанный катализатор, нанесенный на носитель на основе вспененного карбида кремния, осуществляемый в следующих рабочих условиях:1. The method of converting carbon monoxide to C 2 + hydrocarbons in the presence of hydrogen and a metal-containing catalyst in a reactor containing the specified catalyst deposited on a carrier based on foamed silicon carbide, carried out under the following operating conditions: WH (GHSV) изменяется от 100 до 5000 час-1 иWH (GHSV) varies from 100 to 5000 hour -1 and WHSV изменяется от 1 до 100 час-1.WHSV varies from 1 to 100 hour -1 . 2. Способ превращения монооксида углерода в углеводороды C2 + в присутствии водорода и металлсодержащего катализатора в многотрубчатом реакторе, содержащем указанный катализатор, нанесенный на носитель, содержащий вспененный карбид кремния.2. A method for converting carbon monoxide to C 2 + hydrocarbons in the presence of hydrogen and a metal-containing catalyst in a multi-tube reactor containing said catalyst supported on a carrier containing foamed silicon carbide. 3. Способ по п.2, осуществляемый в следующих рабочих условиях:3. The method according to claim 2, carried out in the following operating conditions: WH (GHSV) изменяется от 100 до 5000 час-1 иWH (GHSV) varies from 100 to 5000 hour -1 and WHSV изменяется от 1 до 100 час-1.WHSV varies from 1 to 100 hour -1 . 4. Способ по п.1, в котором вспененный карбид кремния содержит более 50% мас. карбида кремния модификации бета.4. The method according to claim 1, in which the foamed silicon carbide contains more than 50% wt. silicon carbide modification beta. 5. Способ по п.1, в котором носитель катализатора содержит от 50 до практически 100% мас. карбида кремния модификации бета, предпочтительно, практически 100% мас. указанного карбида кремния.5. The method according to claim 1, in which the catalyst carrier contains from 50 to almost 100% wt. silicon carbide modification beta, preferably almost 100% wt. specified silicon carbide. 6. Способ по п.1, в котором пена имеет отверстия пор в диапазоне 300-5000 мкм, преимущественно, 1000-3000 мкм.6. The method according to claim 1, in which the foam has pore openings in the range of 300-5000 microns, preferably 1000-3000 microns. 7. Способ по п.1, в котором пена является твердой.7. The method according to claim 1, in which the foam is solid. 8. Способ по п.1, в котором открытая пористость вспененного SiC изменяется от 30 до 90%, в частности, от 50 до 85%.8. The method according to claim 1, in which the open porosity of the foamed SiC varies from 30 to 90%, in particular from 50 to 85%. 9. Способ по п.1, осуществляемый в следующих рабочих условиях:9. The method according to claim 1, carried out in the following operating conditions: WH (GHSV) изменяется от 150 до 2000 час-1 иWH (GHSV) varies from 150 to 2000 hour -1 and WHSV изменяется от 1, преимущественно, от 5 до 50 час-1.WHSV varies from 1, mainly from 5 to 50 hour -1 . 10. Способ по п.1, осуществляемый в следующих рабочих условиях:10. The method according to claim 1, carried out in the following operating conditions: производительность по углеводородам выше 3 час-1 иhydrocarbon production is greater than 3 hour -1 and производительность по углеводороду С4+ выше 3 час-1.performance of a C 4 + hydrocarbon above 3 h -1. 11. Способ по п.1, осуществляемый в следующих рабочих условиях:11. The method according to claim 1, carried out in the following operating conditions: производительность по углеводородам от 5 до 100 час-1 иhydrocarbon productivity from 5 to 100 hour -1 and производительность по углеводороду С4+ от 5 до 50 час-1.hydrocarbon production C 4 + from 5 to 50 hour -1 . 12. Способ по п.1, осуществляемый в следующих рабочих условиях:12. The method according to claim 1, carried out in the following operating conditions: общее давление: 10-100 атмосфер;total pressure: 10-100 atmospheres; температура реакции: 160-260°С, предпочтительно, 160-250°С;reaction temperature: 160-260 ° C, preferably 160-250 ° C; отношение Н2/СО в исходном синтез-газе составляет 1,2-2,8.the ratio of H 2 / CO in the original synthesis gas is 1.2-2.8. 13. Способ по п.1, осуществляемый в следующих рабочих условиях:13. The method according to claim 1, carried out in the following operating conditions: общее давление: 20-50 атмосфер;total pressure: 20-50 atmospheres; температура реакции: 180-230°С;reaction temperature: 180-230 ° C; отношение Н2/СО в исходном синтез-газе составляет 1,7-2,3.the ratio of H 2 / CO in the feed synthesis gas is 1.7-2.3. 14. Способ по п.1, в котором реактор содержит часть, в которой катализатор нанесен на носитель на основе твердой пены карбида кремния, и часть, в которой катализатор нанесен на носитель в форме зерен или гранул.14. The method according to claim 1, in which the reactor contains a part in which the catalyst is supported on a carrier based on solid silicon carbide foam, and a part in which the catalyst is supported on the carrier in the form of grains or granules. 15. Способ по п.1, осуществляемый в реакторе с восходящим потоком.15. The method according to claim 1, carried out in an upflow reactor. 16. Способ по п.1, осуществляемый в реакторе с нисходящим потоком.16. The method according to claim 1, carried out in a downflow reactor. 17. Способ по п.1, в котором катализатор содержит 1-50%, более конкретно, 3-30% мас., преимущественно, 3-20% мас. одного или нескольких металлов группы, состоящей из кобальта, железа или рутения.17. The method according to claim 1, in which the catalyst contains 1-50%, more specifically, 3-30% wt., Mainly 3-20% wt. one or more metals of the group consisting of cobalt, iron or ruthenium. 18. Способ по п.1, в котором катализатор содержит дополнительно промотор, выбираемый из группы, состоящей из Zr, К, Na, Mn, Sr, Сu, Cr, W, Re, Pt, Ir, Ph, Pd, Ru, Та, V, Mo и их смесей, предпочтительны Mo и Zr.18. The method according to claim 1, in which the catalyst further comprises a promoter selected from the group consisting of Zr, K, Na, Mn, Sr, Cu, Cr, W, Re, Pt, Ir, Ph, Pd, Ru, Ta , V, Mo, and mixtures thereof, Mo and Zr are preferred. 19. Способ по п.1, в котором реактор представляет собой многотрубчатый реактор, содержащий более 10, предпочтительно, более 100 трубок, в частности, 1000-100000 трубок.19. The method according to claim 1, in which the reactor is a multi-tube reactor containing more than 10, preferably more than 100 tubes, in particular, 1000-100000 tubes. 20. Способ по п.1, в котором пена имеет градиент размера пор.20. The method according to claim 1, in which the foam has a pore size gradient. 21. Способ по п.1, в котором пена измельчена.21. The method according to claim 1, in which the foam is crushed. 22. Способ по п.1, в котором реактор снабжен интегрированным теплообменником.22. The method according to claim 1, in which the reactor is equipped with an integrated heat exchanger. 23. Способ по п.1, включающий этап обогащения для производства топлива. 23. The method according to claim 1, comprising an enrichment step for producing fuel.
RU2008102414/04A 2005-06-27 2006-06-22 PROCEDURE FOR CONVERSION OF SYNTHESIS GAS INTO HYDROCARBONS AT PRESENCE OF FOAMED SiC RU2437918C2 (en)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
FR0506523 2005-06-27
FR0506523A FR2887545B1 (en) 2005-06-27 2005-06-27 PROCESS FOR PROCESSING HYDROCARBON SYNTHESIS GAS IN THE PRESENCE OF SIC FOAM
FRPCT/FR2006/001422 2006-06-22
PCT/FR2006/001422 WO2007000506A1 (en) 2005-06-27 2006-06-22 Method of converting a synthesis gas into hydrocarbons in the presence of sic foam

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RU2008102414A true RU2008102414A (en) 2009-08-10
RU2437918C2 RU2437918C2 (en) 2011-12-27

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EP (1) EP1907506A1 (en)
JP (1) JP5139277B2 (en)
CN (1) CN101208408B (en)
AR (1) AR055065A1 (en)
AU (1) AU2006263782B2 (en)
BR (1) BRPI0613019B1 (en)
CA (1) CA2611890C (en)
FR (1) FR2887545B1 (en)
NO (1) NO20076608L (en)
RU (1) RU2437918C2 (en)
WO (1) WO2007000506A1 (en)
ZA (1) ZA200710987B (en)

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2934174B1 (en) * 2008-07-25 2010-09-17 Total Sa METHOD OF FISCHER-TROPSCH SYNTHESIS ON CATALYTIC PLATES COMPRISING A SIC FOAM SUPPORT
JP2012512011A (en) * 2008-12-15 2012-05-31 サソール テクノロジー（プロプライエタリー）リミテッド catalyst
FR2965191A1 (en) 2010-09-23 2012-03-30 Centre Nat Rech Scient PLATE REACTOR FOR THE FISCHER-TROPSCH SYNTHESIS
FR2992236A1 (en) * 2012-06-26 2013-12-27 Sicat Llc Preparing catalyst support used in Fischer-Tropsch reaction, comprises providing beta-silicon carbide support, preparing titanium dioxide precursor solution, impregnating support in solution, and drying and calcining impregnated support
AU2013283037B2 (en) * 2012-06-26 2017-05-25 Centre National De La Recherche Scientifique Catalyst supports made from silicon carbide covered with TiO2 for fischer-tropsch synthesis
CN103816904A (en) * 2012-11-16 2014-05-28 亚申科技研发中心（上海）有限公司 Fischer-Tropsch catalyst, preparation method and application thereof, and Fischer-Tropsch synthesis method using same
WO2014140973A1 (en) 2013-03-14 2014-09-18 Sasol Technology (Pty) Limited A hydrocarbon synthesis process using a cobalt-based catalyst supported on a silicon carbide comprising support
WO2014207096A1 (en) 2013-06-27 2014-12-31 Sicat Method for manufacturing shaped beta-sic mesoporous products and products obtained by this method
ITMI20131439A1 (en) 2013-09-03 2015-03-04 Eni Spa BED TUBULAR REACTOR, PACKED FOR EXOTHERMIC OR ENDOTHERMAL CATHALTIC REACTIONS
EP3532567B1 (en) * 2016-10-27 2024-08-28 Shell Internationale Research Maatschappij B.V. A process for producing hydrocarbons

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4914070A (en) * 1987-10-19 1990-04-03 Pechiney Electrometallurgie Process for the production of silicon carbide with a large specific surface area and use for high-temperature catalytic reactions
GB9114314D0 (en) * 1991-07-02 1991-08-21 British Petroleum Co Plc Catalyst treatment for fisher-tropsch process
FR2684092B1 (en) * 1991-11-21 1994-03-04 Pechiney Recherche PROCESS FOR THE PREPARATION OF LARGE SPECIFIC METAL CARBIDES FROM ACTIVATED CARBON FOAMS.
US5648312A (en) * 1994-12-29 1997-07-15 Intevep, S.A. Hydrogenation catalyst with improved attrition resistance and heat dissipation
DZ2370A1 (en) * 1996-12-13 2002-12-28 Shell Int Research Process for the preparation of hydrocarbons
US6440895B1 (en) * 1998-07-27 2002-08-27 Battelle Memorial Institute Catalyst, method of making, and reactions using the catalyst
JP2003507161A (en) * 1999-08-17 2003-02-25 バッテル・メモリアル・インスティチュート Catalyst structure and method for Fischer-Tropsch synthesis
FR2832415B1 (en) * 2001-11-20 2005-09-23 Inst Francais Du Petrole PROCESS FOR CONVERTING SYNTHESIS GAS IN SERIES REACTORS
FR2864532B1 (en) * 2003-12-31 2007-04-13 Total France PROCESS FOR TRANSFORMING A SYNTHETIC GAS TO HYDROCARBONS IN THE PRESENCE OF SIC BETA AND EFFLUTING THE SAME

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ZA200710987B (en) 2008-11-26
JP5139277B2 (en) 2013-02-06
WO2007000506A1 (en) 2007-01-04
NO20076608L (en) 2007-12-27
CA2611890A1 (en) 2007-01-04
FR2887545A1 (en) 2006-12-29
CA2611890C (en) 2012-05-08
FR2887545B1 (en) 2007-08-10
BRPI0613019B1 (en) 2016-03-15
EP1907506A1 (en) 2008-04-09
BRPI0613019A2 (en) 2010-12-14
CN101208408A (en) 2008-06-25
RU2437918C2 (en) 2011-12-27
AU2006263782B2 (en) 2011-05-12
AU2006263782A1 (en) 2007-01-04
CN101208408B (en) 2012-08-22
JP2008544060A (en) 2008-12-04
AR055065A1 (en) 2007-08-01

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