• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    A process and apparatus for the auto-thermal production of hydrogen rich synthesis gas wherein a mixture of steam and a hydrocarbon feed gas is reacted by passing through a catalyst counter-currently to the flow of the combustion reaction effluent of the process. Reaction tubes are mounted within a heat exchange chamber of the reactor and are adapted to contain catalyst to effect the reaction of the mixture. Oxygen or oxygen-enriched air is introduced into a combustion chamber within the reactor to effect combustion, and the combustion reaction effluent is passed through a second catalyst zone to provide additional reaction and is thereafter passed about the exterior of the reaction tubes to effect heat exchange with the mixture passing through the tubes. The exothermic heat of reaction from combustion thus provides the heat for the endothermic reaction occurring within the reaction tubes and within the second catalyst zone.
    公开号:SU1713420A3
    申请号:SU853856865
    申请日:1985-01-29
    公开日:1992-02-15
    发明作者:Ли Льюис Джерри
    申请人:Флуор Корпорейшн (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a reactor design for producing synthesis gas.
    The aim of the invention is to increase the efficiency of the process.
    The drawing shows the autothermal reactor, vertical section.
    The reactor includes a housing 1, a heat exchange chamber 2, a nozzle 3 for introducing a mixture of water vapor with the original hydrocarbon gas, reaction tubes 4 fixed in tube sheets 5 and 6. The first fixed bed of catalyst 1 is located in the reaction tubes. This catalyst can be any suitable for reforming a catalyst, for example nickel. The wall of the housing 1 has an inside lining 8, for example, of reinforcing ceramics, which minimizes heat transfer through the casing. The reactor contains a device for directing the flow, made in the form of a conical reflector 9 with tube 10, which corresponds to the reaction tubes directly near the tube sheet 6, allowing passage of the reacted, partially reformed gases from the reaction tubes 4 to the combustion chamber 11, which is in the lower part of the reactor. Although the represented reflector 9 has a cone shape, other reflector configurations may be used.
    A second inlet is provided at the bottom of the reactor to introduce oxygen or oxygen-enriched air into the combustion chamber. Adjacent to the end of the vertically passing pipe 10, a partition 12 is installed to separate the combustion chamber 11 from the heat exchange chamber 2. In the partition 12, openings 13 are provided through which the reaction product passes. formed during combustion and enters the second catalyst zone 14. The product formed during combustion can pass through this catalyst zone and undergo additional or secondary reforming to form the required synthesis gas. In this case, any well-known catalyst selected by a person skilled in the art can be a reforming catalyst.
    As the resulting synthesis gas passes upward from the second catalyst zone, it is directed through the flow reflectors 15 to the outside of the reaction tubes 4, so that direct contact between the reaction tubes and the hot product flow is ensured. This, in turn, provides effective utilization of the exothermic heat of combustion for the endothermic reaction occurring inside the reaction tubes 4.
    In the vicinity of the inlet 3, an outlet 16 is provided through which the synthesis gas is removed for purification and further processing in order to produce ammonia (or some other product depending on the type of reaction process).
    The reactor includes manholes 17 and 18 serving for maintenance and preventive maintenance. The reactor can be equipped with additional inlet and outlet connections for flow distribution, addition of additional flue gas or water vapor to the combustion chamber.
    The reactor operates as follows.
    The source hydrocarbon gas is introduced into reactor vessel 1 through inlet 3 at a temperature of 482-704 ° C. The mixture passes through the holes in the tube sheet 5 and through the reaction tube 4, exits the reaction tube through the conical reflector 9, passes through the tube 10 and exits into the lower part of the reactor and into the reaction chamber 11 at a temperature of 593-760 ° C. Oxygen or oxygen-enriched air at a temperature ranging from room temperature to 38 ° C is introduced into the combustion chamber through the inlet pipe 19 to carry out the combustion process. The product obtained as a result of combustion has a temperature of 1374-1926 ° C and passes upwards through the openings 13 in the partition 12 and the second catalyst zone 14, as a result of which secondary reforming occurs,
    The mixture of synthesis gas produced during secondary reforming has a temperature of 815-1149 ° C and is directed upwards, the arrival of
    in direct contact with the reaction tubes 4, as a result of which heat exchange takes place, providing heating of the water vapor mixture with the original hydrocarbon gas inside the tubes 4. The temperature of the cooled synthesis gas mixture is 538-704 ° C.
    The reaction tubes 4 in tube sheets 5 and 6 are suspended inside the reactor to its
    0 wall on hangers 20. This allows the use of thin-walled pipes, which are less expensive and have better heat transfer characteristics than large pipes. Since thin-walled pipes
    5 have a higher tensile strength than compression, they are mounted inside the reaction vessel by hanging, otherwise they may be deformed or even destroyed.
    权利要求:
    Claims (2)
    [1]
    1.Athermal reactor to produce synthesis gas, containing a heat exchange chamber, a nozzle for inlet water
    5 vapor and feed gas into the heat exchange chamber, reaction tubes filled with catalyst and installed in the heat exchange chamber to perform the first reforming stage, the device for
    0 flow direction, made in the form of a conical reflector with a tube, in the lower part of which there is a partition for directing the flow from the reaction tubes to the combustion chamber, having a nozzle
    5 for the incoming gas, a synthesis gas outlet nozzle located in the upper part of the heat exchange chamber, and a lining, in that, in order to increase the efficiency of the process, the combustion chamber is located under the partition having openings for the exit of the combustion products, and on the partition, located between the combustion chamber and the heat exchange chamber, a second layer is installed
    5 catalyst to perform the second reforming step.
    [2]
    2. Reactor pop. 1, characterized in that. the lining is located inside the reactor.
    0 3, Reactor on PP. 1 and 2, characterized in that the reaction tubes are mounted on hangers.
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1713420A3|1992-02-15|Autothermic reactor for producing synthesis gas
    CA2081170C|2002-12-24|Fluidized bed reaction system for steam/hydrocarbon gas reforming to produce hydrogen
    US4650651A|1987-03-17|Integrated process and apparatus for the primary and secondary catalytic steam reforming of hydrocarbons
    US7297169B2|2007-11-20|Apparatus and method for hydrocarbon reforming process
    US4822521A|1989-04-18|Integrated process and apparatus for the primary and secondary catalytic steam reforming of hydrocarbons
    US5112578A|1992-05-12|Reactor for reforming hydrocarbon and process for reforming hydrocarbon
    DK167864B1|1993-12-27|PROCEDURE AND REACTOR SYSTEM FOR REFORMING CARBON HYDROIDS DURING HEAT EXCHANGE
    US4909809A|1990-03-20|Apparatus for the production of gas
    KR20040027457A|2004-04-01|Process and apparatus for the preparation of synthesis gas
    US4113441A|1978-09-12|Steam reforming reactor
    CA2428548A1|2003-11-14|Methanol-steam reformer
    EA000777B1|2000-04-24|Process and process unit for the preparation of ammonia synthesis gas
    US3262758A|1966-07-26|Apparatus for reforming synthesis gas
    US4378336A|1983-03-29|Monolith reactor
    IE43795B1|1981-06-03|Reactor
    US5019356A|1991-05-28|Steam reformer with internal heat recovery
    US20080247942A1|2008-10-09|Method and Reactor for Carrying Out Endothermic Catalytic Reactions
    US5362453A|1994-11-08|Reformer for the generation of synthesis gas
    US3190730A|1965-06-22|Integrated hydrocarbon conversion column
    WO2004112954A1|2004-12-29|Cooled gas injection device
    US4336229A|1982-06-22|Apparatus for the production of ammonia synthesis gas from purified coke oven gas
    AU598074B2|1990-06-14|Apparatus and use thereof in the production of synthesis gas
    GB1254364A|1971-11-24|Catalytic reformer
    RU2002131458A|2004-03-27|CATALYTIC REACTOR FOR EXOTHERMAL PROCESSES PROCESSING IN A GAS-SOLID PHASE WITH A DIFFERENT TEMPERATURE DIFFERENCE
    US3450507A|1969-06-17|Integrated reforming of hydrocarbons
    同族专利:
    公开号 | 公开日
    GB2153382A|1985-08-21|
    GB2153382B|1987-06-24|
    JPS60186401A|1985-09-21|
    ATA24185A|1990-10-15|
    NL192572B|1997-06-02|
    AU3813585A|1985-08-08|
    NZ210933A|1987-07-31|
    NL192572C|1997-10-03|
    BR8500393A|1985-09-10|
    DK38385D0|1985-01-28|
    US4666680A|1987-05-19|
    GB8501758D0|1985-02-27|
    NO170921C|1992-12-30|
    DK38385A|1985-07-31|
    JPH0522641B2|1993-03-30|
    DK166770B1|1993-07-12|
    IN163324B|1988-09-10|
    NO850329L|1985-07-31|
    CA1327271C|1994-03-01|
    ZA85527B|1995-04-06|
    AT392628B|1991-05-10|
    AU576214B2|1988-08-18|
    NO170921B|1992-09-21|
    MY101681A|1991-12-31|
    NL8500238A|1985-08-16|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2459857C2|2007-07-20|2012-08-27|Юпм-Киммене Ойй|Method and apparatus for producing biofuel from solid biomass|
    RU2480400C1|2011-12-02|2013-04-27|Общество с ограниченной ответственностью "Газохим Техно"|Process system for producing synthesis gas|
    RU2574464C1|2014-07-10|2016-02-10|Федеральное государственное бюджетное учреждение науки Институт проблем химической физики Российской академии наук |Method for obtaining synthesis-gas from hydrogen-containing raw material in revere flow reactor and reactor for realisation thereof|FR512655A|1919-09-08|1921-01-28|Air Liquide|Method for the direct synthesis of ammonia|
    US2472254A|1944-08-22|1949-06-07|Shell Dev|Apparatus and method for carrying out catalytic reactions|
    US2887365A|1955-02-21|1959-05-19|Belge Produits Chimiques Sa|Catalytic reactor|
    DE1143295B|1961-05-06|1963-02-07|Metallgesellschaft Ag|Device for the autothermal, catalytic cracking of hydrocarbons under pressure|
    GB1093943A|1963-10-07|1967-12-06|Ici Ltd|Reforming hydrocarbons|
    DE1442594A1|1965-06-24|1968-11-28|Badische Anilin & Soda Fakrik|High pressure synthesis furnace for exothermic gas reactions|
    US3516800A|1965-08-25|1970-06-23|Hisao Yamamoto|Synthesis reaction apparatus equipped with means for temperature control of catalyst bed|
    US3442613A|1965-10-22|1969-05-06|Braun & Co C F|Hydrocarbon reforming for production of a synthesis gas from which ammonia can be prepared|
    GB1247338A|1967-10-13|1971-09-22|Power Gas Ltd|Steam reforming of hydrocarbons|
    US3607125A|1968-12-30|1971-09-21|Gen Electric|Reformer tube construction|
    US3658498A|1969-06-03|1972-04-25|Siegener Ag Geisweid|Method and apparatus for producing ethylene and synthesis gas by thermal cracking|
    US3909299A|1973-10-01|1975-09-30|United Technologies Corp|Fuel cell system including reform reactor|
    US4079017A|1976-11-19|1978-03-14|Pullman Incorporated|Parallel steam reformers to provide low energy process|
    US4071330A|1976-12-22|1978-01-31|United Technologies Corporation|Steam reforming process and apparatus therefor|
    US4221763A|1978-08-29|1980-09-09|Cities Service Company|Multi tube high pressure, high temperature reactor|
    AU511381B2|1978-09-12|1980-08-14|Midrex International B.V. Rotterdam|Vertical shaft furnace forthe reduction of iron ore to sponge iron|
    DE3244252C2|1982-11-30|1990-10-31|Uhde Gmbh, 4600 Dortmund, De|US4650651A|1983-06-09|1987-03-17|Union Carbide Corporation|Integrated process and apparatus for the primary and secondary catalytic steam reforming of hydrocarbons|
    US5181937A|1985-06-27|1993-01-26|Stone & Webster Engineering Corp.|Apparatus for production of synthesis gas using convective reforming|
    US5006131A|1985-06-27|1991-04-09|Stone & Webster Engineering Corporation|Apparatus for production of synthesis gas using convective reforming|
    DE3532413C2|1985-09-11|1990-02-08|Uhde Gmbh, 4600 Dortmund, De|
    GB8609099D0|1986-04-15|1986-05-21|British Petroleum Co Plc|Production of synthesis gas|
    EP0281600B1|1986-09-15|1994-06-08|L. & C. Steinmüller GmbH|Reformer for catalytic cracking of gaseous hydrocarbons|
    GB8629497D0|1986-12-10|1987-01-21|British Petroleum Co Plc|Apparatus|
    DE3719780A1|1987-06-13|1988-12-22|Uhde Gmbh|METHOD FOR PRODUCING AMMONIA FROM NATURAL GAS|
    IT1211957B|1987-12-07|1989-11-08|Kinetics Technology|PROCEDURE, APPARATUS AND RELATED OPERATING METHOD FOR STEAM GENERATION AND HEAT RECOVERY IN HYDROGEN AND SYNTHESIS GAS PRODUCTION PLANTS|
    DE3803082A1|1988-02-03|1989-08-17|Uhde Gmbh|MULTI-STAGE PROCESS FOR GENERATING H2AND CO-CONTAINING SYNTHESIS GAS|
    DE3803081A1|1988-02-03|1989-08-10|Uhde Gmbh|Apparatus for carrying out a multistage generation of synthesis gas|
    JPH01261201A|1988-04-12|1989-10-18|Mitsubishi Gas Chem Co Inc|Hydrocarbon reforming reactor|
    GB2222533A|1988-04-20|1990-03-14|Humphreys & Glasgow Ltd|Combined tubular primary and secondary reformer|
    DE3813863A1|1988-04-23|1989-11-02|Uhde Gmbh|DEVICE FOR RECEIVING CATALYSTS, ESPECIALLY IN THE PRODUCTION OF SYNTHESIS GAS|
    GB2217728B|1988-04-28|1992-02-26|Humphreys & Glasgow Ltd|Combined reformer|
    JPH0218303A|1988-07-07|1990-01-22|Mitsubishi Gas Chem Co Inc|Reactor and process for reforming hydrocarbon|
    US5011625A|1989-12-11|1991-04-30|The M. W. Kellogg Company|Autothermal steam reforming process|
    US5122299A|1989-12-11|1992-06-16|The M. W. Kellogg Company|Autothermal steam reforming process|
    US5382271A|1991-12-26|1995-01-17|Industrial Technology Research Institute|Hydrogen generator|
    JPH07126201A|1993-10-27|1995-05-16|Mitsubishi Gas Chem Co Inc|Methanol production process|
    US5980840A|1997-04-25|1999-11-09|Bp Amoco Corporation|Autothermic reactor and process using oxygen ion--conducting dense ceramic membrane|
    DE19727841A1|1997-06-24|1999-01-07|Fraunhofer Ges Forschung|Method and device for the autothermal reforming of hydrocarbons|
    EP0936183B1|1998-02-17|2006-10-04|Haldor Topsoe A/S|Process for the autothermal reforming of a hydrocarbon feedstock|
    AU754632B2|1998-07-02|2002-11-21|Haldor Topsoe A/S|Process for autothermal reforming of a hydrocarbon feedstock|
    DK173745B1|1998-08-27|2001-09-03|Topsoe Haldor As|Process for Autothermal Reform of Hydrocarbon Material|
    US6180846B1|1998-09-08|2001-01-30|Uop Llc|Process and apparatus using plate arrangement for combustive reactant heating|
    US6641625B1|1999-05-03|2003-11-04|Nuvera Fuel Cells, Inc.|Integrated hydrocarbon reforming system and controls|
    AU774093B2|1999-07-29|2004-06-17|Sasol TechnologyLtd.|Natural gas conversion to hydrocarbons and ammonia|
    DE10119083C1|2001-04-19|2002-11-28|Joachim Alfred Wuenning|Compact steam reformer|
    GB2421246A|2003-08-21|2006-06-21|Syntroleum Corp|Two-stage auto thermal reforming process system|
    US7892511B2|2004-07-02|2011-02-22|Kellogg Brown & Root Llc|Pseudoisothermal ammonia process|
    US7435401B2|2004-07-02|2008-10-14|Kellogg Brown & Root Llc|Pseudoisothermal ammonia process|
    KR101301710B1|2004-12-23|2013-08-30|킹 에프에이에이치디 유니벌시티 오브 패트로레움 앤 미네랄스|Thermo-neutral reforming of petroleum-based liquid hydrocarbons|
    US20070000173A1|2005-06-28|2007-01-04|Michael Boe|Compact reforming reactor|
    US7700005B2|2006-12-26|2010-04-20|Saudi Arabian Oil Company|Oil-based thermo-neutral reforming with a multi-component catalyst|
    EP2065337A1|2007-11-27|2009-06-03|Ammonia Casale S.A.|Process for producing ammonia synthesis gas|
    JPWO2009069220A1|2007-11-29|2011-04-07|日揮株式会社|Production method and production apparatus for elementary gas for ammonia synthesis|
    US9034208B1|2011-02-11|2015-05-19|Emerging Fuels Technology, Inc.|Process to convert natural gas into liquid fuels and chemicals|
    US9321641B1|2011-02-11|2016-04-26|Emerging Fuels Technology, Inc.|Process to convert natural gas into liquid fuels and chemicals|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/574,921|US4666680A|1984-01-30|1984-01-30|Autothermal production of synthesis gas|
    [返回顶部]