• 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:
    Hydrogen and carbon oxides are reacted to form methane by passing an inlet stream of preheated methanation synthesis gas together with a recycle stream of product gas through a catalyst bed in an adiabatic methanation reactor. The inlet temperature is between 250 DEG and 350 DEG C, the outlet temperature between 500 DEG and 700 DEG C. The recycle stream is withdrawn from the outlet stream after the latter has been cooled to a temperature between 250 DEG and 350 DEG C and being, however, at least 50 DEG C above the dew point. A preferred means for withdrawing the recycle stream is an ejector driven by the inlet stream or by added steam.
    公开号:SU1215617A3
    申请号:SU752185807
    申请日:1975-11-04
    公开日:1986-02-28
    发明作者:Йерн Эрнест
    申请人:Халдор Топсое А.С. (Фирма)；
    IPC主号:
    专利说明:

    2. The method according to claim 1, characterized by the fact that the raw materials are fed to the adiabatic reactor at the same temperature to which the effluent from the first stage is cooled.
    Prioritize:
    by prize
    The invention relates to the production of methane-rich gases from carbon monoxide and hydrogen and can be used in the production of natural gas substitutes.
    The aim of the invention is to increase the efficiency of the process.
    FIG. Figure 1 shows the methane-containing gas breathing scheme, where the ejector is driven by the original synthesis gas; FIG. 2 is the same where the ejector is driven by water vapor.
    By, submitted to:. Fig. 1, a gas containing carbon monoxide and hydrogen-methane synthesis gas 1 supplied at elevated pressure, heated to the desired temperature in heat exchangers 2 and 3 by the resulting gas flows from the first methanation reactor 4 and the second methanation reactor 5, respectively in the ejector 6 combines with the recycle gas stream 7, separated from the stream flowing from the outlet of the first methanation reactor 4, in order to create the necessary driving force for the ejector 6 in order to divert the recycle gas stream 7, the synthesis stream -gas 1 is supplied at a pressure slightly higher than the pressure required at the inlet of the methanation reactor.
    The combined syngas and recycle gas flows 7 enter the first methanation reactor through line 8 with a temperature of 259-339 ° C and pass through the nickel catalyst bed in reactor 4, Stream 9, leaving the first methanation reactor 6, heated
    215617
    06.11.74- temperature of the effluent from the first stage, cooling temperature of the effluent, ejection of a part of the effluent using the raw material flow to the first stage, the amount ejected by. current ;;
    04.22.75- ejection using a stream of water vapor.
    five
    0
    0
    five
    0
    to 500-700 ° C as a result of exothermic reactions, cooled in the heat exchanger 10, which works as a high-pressure steam generator, to 250-350 ° C, and the condition that the dew point of the stream would be at least 51 ° C below the cooling temperature ) dress After diverting the recycle gas stream 7, the remaining gas stream obtained from the first reactor is further cooled in the heat exchanger 2 and passed to the second methane reactor 5 through a catalyst bed contained therein.
    The outlet stream 11 from the second methane reactor 5 is cooled in heat exchangers 3 and 12, fed to a separator 13 and the final stream of target gas 14 is obtained,
    The process circuit shown in Fig. 2 differs from the circuit in Fig. 1 in that the ejector 6 operates under the action of water vapor of high pressure. Water vapor for the ejection of the ejector is a high pressure steam generated in the heat exchanger 10, from where it is fed to the ejector via line 15. In this case, methane synthesis gas 1 enters directly into the first metering reactor through line 8 and does not require excessive pressure, in the scheme in FIG. 1,
    The method is illustrated by the following examples.
    The table presents the data for examples 1-13 of the method implementation on various samples of synthesis gas using ejectors driven by high-pressure water vapor (examples 4, 5, 7 and 8)
    or the original methane synthesis gas (examples 1-3.6 and 9-13).
    The final product gas obtained in the examples, for example, 2-4 contains some amount of hydrogen and carbon dioxide. Therefore, if not. It is necessary to obtain a methane concentration of more than 90 vol.%, the stream 11 exiting the second methanation reactor, after cooling to 250-300 ° C, should be further methanated in the third methanation reactor. In Examples 1 and 5.8, the concentration of methane, either higher than 90% by volume or oia, can be increased to more than 90% by simple removal of carbon dioxide. In particular, in examples 5 and 8, the removal of carbon dioxide leads to the formation of a gas containing 97.5 and 94.5% of methane, respectively.
    In this way, a gas, rich in methane, is obtained from synthesis gas according to those
    215617
    According to the known technology, the process, which excludes gas cooling to a low temperature, is accompanied by vapor condensation, leading to heat loss and a decrease in the process economy. Cooling the gas discharged to the reactor to 250-350 ° C saves energy, since no steam condensate is formed and the heat of 10 lAt removed during cooling can be effectively used, for example, to produce steam.
    (5 Minor cooling of the gas leaving the reactor makes it possible to use ejectors for gas recirculation. This eliminates energy costs for the operation of compressors. Recirculation of the gas leaving the reactor to the reactor inlet allows limiting the temperature at the reactor outlet.
    "S4
    u
    five
    &

    Editor M, Nedoluzhenko
    Compiled by N, Kirillova
    Tehred T. Tulik Corrector B, But ha
    Order 915/62 Circulation 379Subscription
    VNIIPI USSR State Committee
    for inventions and discoveries 113035, Moscow, Zh-35, Raushsk nab., 4/5
    Branch PPP Patent, Uzhgorod, st. Project, 4
    权利要求:
    Claims (2)
    [1]
    1. METHOD FOR PRODUCING A METAN-CONTAINING GAS by contacting a gas mixture containing carbon monoxide and hydrogen, preheated to 259339, with a nickel catalyst at an elevated temperature and pressure of 26-71 atm vadiabati-, sand reactor at the first stage of methanization, cooling the stream leaving the reactor and feeding it to the second stage of methanization, characterized in that, in order to increase the efficiency of the process, the stream from the first stage of methanization is withdrawn at 500-700 C, cooled to 250 ~ 350 ° C, provided that the dew point of the effluent at least 51 ° C below this temperature, and ejected using a stream of water vapor or raw materials to the first stage to combine with the raw material part of the cooled stream in an amount necessary to maintain the outlet stream temperature of the reactor 500-700 ° C.
    SU and, 1215617 _ftsg.1
    [2]
    2. The method according to p. ^ Characterized in that the feed to the adiabatic reactor is supplied at the same temperature to which the stream leaving the first stage is cooled.
    Priority by signs:
    06.11.74 - temperature of the effluent from the first stage of the flow, cooling temperature of the effluent, ejection of a part of the effluent using the feed stream to the first stage, the amount of ejected by. current ;;
    04/22/75 - ejection using a stream of water vapor.
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1215617A3|1986-02-28|Method of producing methane-containing gas
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    US4650814A|1987-03-17|Process for producing methanol from a feed gas
    US4309359A|1982-01-05|Energy process in methanol synthesis
    US3904389A|1975-09-09|Process for the production of high BTU methane-containing gas
    JP4053103B2|2008-02-27|Ammonia production using concentrated air reforming and nitrogen input to synthesis loop
    US4578214A|1986-03-25|Process for ammonia syngas manufacture
    AU633470B2|1993-02-04|Production of fuel gas
    US4618451A|1986-10-21|Synthesis gas
    US4065483A|1977-12-27|Methanol
    US4264567A|1981-04-28|Method for producing a hydrogen-containing gas
    US3940428A|1976-02-24|Methanol production
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    WO2000009441A2|2000-02-24|Steam reforming
    RU2110477C1|1998-05-10|Method for catalytic production of gas rich in carbon oxide
    US3705009A|1972-12-05|Heat recycling for ammonia preparation
    JP4065413B2|2008-03-26|Method for recovering krypton and xenon from air
    US5173513A|1992-12-22|Methanol synthesis
    CA1160844A|1984-01-24|Synthesis gas for ammonia production
    AU715987B2|2000-02-17|Process for ammonia and methanol co-production
    US4045960A|1977-09-06|Process for producing energy
    EP0291857A2|1988-11-23|Method of carbon monoxide production
    EP0047596B1|1983-11-30|Synthesis for producing carbon compounds from a carbon oxide/hydrogen synthesis gas
    US4218389A|1980-08-19|Process for making methanol
    同族专利:
    公开号 | 公开日
    DE2549439C2|1988-02-25|
    DK495675A|1976-05-07|
    DD122066A5|1976-09-12|
    JPS5953245B2|1984-12-24|
    AR205595A1|1976-05-14|
    BR7507253A|1976-08-03|
    US4130575A|1978-12-19|
    IN142700B|1977-08-13|
    CA1075906A|1980-04-22|
    FR2290410A1|1976-06-04|
    JPS5168502A|1976-06-14|
    FR2290410B1|1980-05-09|
    DE2549439A1|1976-05-13|
    DK142501B|1980-11-10|
    DK142501C|1981-06-29|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    GB47924/74A|GB1516319A|1974-11-06|1974-11-06|Process for preparing methane-rich gases|
    GB1664175|1975-04-22|
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