• 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 for separation of a high pressure gas stream (10) such as light refinery gases in which the gas mixture is expanded, preferably through a turbine (28), and separated into first vapor and liquid portions. The first vapor portion (31) may be recovered as, for example, methane-rich product gas. The first liquid portion (33) is raised to an intermediate pressure, revaporized, and introduced to a fractionator (36) from which an ethane-containing stream is recov­ered. The ethane-containing stream (37) is then cooled and separated (in 39) into a second vapor portion (40) and a second liquid portion (42) which is then expanded (in 43) and combined with the expanded starting gas mixture (29) to increase the amount of refrigeration that may be recovered from the first liquid stream prior to its fractionation.
    公开号:SU1553018A3
    申请号:SU874203807
    申请日:1987-12-18
    公开日:1990-03-23
    发明作者:Шарма Шанмук；К.Хилл Донни；А.Дурр Чарльз
    申请人:Дзе М.В.Келлог Компани (Фирма)；
    IPC主号:
    专利说明:


    cm
    The invention relates to a cryogenic technique, and more specifically to methods for -cryogenic separation of hydrocarbon / gases under high pressure.
    The purpose of the invention is to increase efficiency.
    The drawing shows an installation diagram which makes it possible to realize a method for the separation of gases.
    The installation includes a processing gas supply line 1, a double-flow heat exchanger 2, evaporators 3-5, a turbine 6 installed on the same shaft as the compressor 7, a pump 8, heat exchangers 9-11, valves 12 and 13, column 14 and line 15 for gas production.
    The installation works as follows.
    Light gas, such as refinery gas, predominantly containing methane, C-hydrocarbons and hydrogen with small amounts of nitrogen and Ce-hydrocarbons, is fed into the system once
    dividing in line 1, is cooled in heat exchanger 2 and separated in evaporator 3. The vapor stream exiting the evaporator 3 is a high pressure gas stream containing a mixture of light hydrocarbons, with a composition similar to the original light gas, but with reduced C3-hydrocarbon content. In the production of light gas from natural gas that is produced by improving oil recovery by introducing nitrogen or carbon dioxide, a substantial component of the high-pressure gas stream can be nitrogen or carbon dioxide, respectively, depending on the nature of the oil recovery. Nitrogen is associated with methane, and carbon dioxide is associated with ethane. If the presence of such binary mixtures is undesirable, they can be divided into special separation systems located downstream.
    The initial gaseous mixture should be under a sufficiently high pressure to provide at least one expansion stage to produce cold, and, with the release of the target gas from the expanded gas fraction, under a pressure of 3-28 kg / cm2. High pressure is in the range of 5 to 55 Kg / cm2.
    High pressure gas flow pre-cooled to heat
    30184
    The mannik 2 expands on the turbine 6 to a first intermediate pressure of 3 to 35 kg / cm2 and is introduced into the evaporator 4, which is the first separation zone.
    The operation of the turbine shaft 6 is used to recompress the first steam flow from the evaporator 4 to KOMI: spring 7 to supply pressure after removing cold from the steam flow in the heat exchanger 11.
    ten
    five
    0
    five
    five
    0 5
    0 5
    The first fluid flow is removed from the evaporator 4 separately from the steam flow and compressed to a second intermediate pressure by the pump 8. The second intermediate pressure is also between 3 and 35 kg / cm2, but it must be higher than the first intermediate pressure. Then, the cold in the heat exchanger 2 is extracted from the first liquid stream and the resulting partially re-evaporated stream is introduced into the top of the column 14, which is a separation zone with multiple equilibrium levels. When the first liquid stream is combined with the descending liquid from the evaporator 3, the raw material of the column 14 (deethanizer) is mainly Cr-C3 hydrocarbons, but the C component is only a small fraction of the Cj content in the light gas in line 10.
    When treating refined gas, a certain amount of heavier flows (not shown) from other gas separation stages also enter the column. The head stream from column 14 contains mainly ethane and ethylene with small amounts of methane and C3 hydrocarbons. When this process is applied in case of enhanced oil recovery with nitrogen, this stream, as well as the first stream, is mainly nitrogen. The overhead stream leaving the column is cooled to -54 ° C in heat exchanger 9, and then evaporated in a second separation zone (in evaporator 5). Cold is recovered from the second vapor stream exiting the evaporator and this second vapor stream is combined with the first vapor stream exiting compressor 7 to form methane-rich gas in the case of refining gas which is diverted via line 15.
    Since the overhead stream from column 14 is under the second intermediate pressure, which in this case is 1.5 kg / cm2 higher than the first intermediate pressure, the effect of the second separation zone is to obtain a second liquid stream, which is expanded at valve 12 and combined into flow expanded in the turbine 6. A mixture of these cold flows increases the amount of cold compared to the amount obtained only with expansion in the turbine, and thereby increases the recovery of cold in the heat exchanger 2.
    权利要求:
    Claims (1)
    [1]
    1. A high pressure gas separation method containing a mixture of light hydrocarbons by expanding the high pressure gas stream to the value of the first intermediate pressure and supplying the obtained expanded stream to the first separation zone with one equilibrium step, removing the first steam from the first separation zone flow and separation of the first liquid stream, supplying the first liquid stream to the separation zone with several equilibrium steps, with high pressure gas flow it is cooled before expansion, and expansion is carried out on a turbine, which is distinguished by the fact that,
    five
    0
    five
    in order to increase efficiency, the pressure of the first liquid stream is increased to the second intermediate pressure and the cold is removed from this stream until complete evaporation before being fed into the separation zone with several equilibrium steps, the gas mixture containing ethane is separated from this zone, it is cooled and directed In the second separation zone with one stage-1-equilibrium, from where the second vapor stream and the second liquid stream are diverted, the second liquid stream in the first separation zone with one equilibrium step is distributed.
    2, the method according to claim 1, wherein cooling the gas stream under high pressure is carried out by heat exchange through the wall with the first liquid stream under the second intermediate pressure.
    i
    3, the method according to claim 1, differing from that by the fact that the high-pressure gas stream contains in the rest. hydrogen, methane and ethane, the values of the first and second intermediate pressures are within 3 and
    35 kgf / cm2, and the pressure of the gas stream under high pressure is between 5 and 55 kgf / cm2,
    4, the method according to claim 1, characterized in that the high-pressure gas stream contains 10 -.
    5 90 vol.% Of nitrogen, and the first and second vapor streams contain mostly nitrogen.
    0
    类似技术:
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    RU2190169C2|2002-09-27|Method of cooling gas in the course of production of ethylene from starting gas
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    US20020189443A1|2002-12-19|Method of removing carbon dioxide or hydrogen sulfide from a gas
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    US5421167A|1995-06-06|Enhanced olefin recovery method
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    RU2000120539A|2002-07-20|COOLING SYSTEM FOR ETHYLENE PRODUCTION
    US5253479A|1993-10-19|Method and apparatus for recovery of ethylene and propylene from gas produced by the pyrolysis of hydrocarbons
    US3932156A|1976-01-13|Recovery of heavier hydrocarbons from natural gas
    GB2304401A|1997-03-19|Recompression cycle for recovery of natural gas liquids
    US20020174679A1|2002-11-28|Ethylene plant refrigeration system
    US4436540A|1984-03-13|Low pressure separation for light hydrocarbon recovery
    同族专利:
    公开号 | 公开日
    EP0272391A3|1988-10-19|
    US4710214A|1987-12-01|
    EP0272391B1|1990-07-11|
    MX169237B|1993-06-25|
    AU584576B2|1989-05-25|
    NO875315D0|1987-12-18|
    NO875315L|1988-06-20|
    EP0272391A2|1988-06-29|
    NO167549C|1991-11-20|
    IN171634B|1992-11-28|
    AU8006187A|1988-06-23|
    CA1298540C|1992-04-07|
    NO167549B|1991-08-12|
    JPS63161381A|1988-07-05|
    DE3763653D1|1990-08-16|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/944,272|US4710214A|1986-12-19|1986-12-19|Process for separation of hydrocarbon gases|
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