• 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:
    Process for treating a gaseous mixture under pressure to remove unwanted components from a gas, including methane, ethane, hydrogen, nitrogen, such components as C3, C4 and C5 higher hydrocarbons, hydrogen sulphide and carbon dioxide. The gaseous mixture is fractionated under pressure to remove in bottoms product portions of higher hydrocarbons, hydrogen sulphide and carbon dioxide. The overhead product is scrubbed to remove in a suitable solvent a substantial portion of or all of the remaining higher hydrocarbons, hydrogen sulphide and carbon dioxide.
    公开号:SU1085515A3
    申请号:SU782648211
    申请日:1978-08-08
    公开日:1984-04-07
    发明作者:Бекер Ганс；Гримм Петер；Ранке Герхард；Рот Дитер
    申请人:Линде Аг (Фирма)；
    IPC主号:
    专利说明:

    2. The method according to claim 1 is also distinguished by the fact that the rectification of the overhead product is carried out at a pressure between the critical pressure of the individual hydrocarbons and the lowest critical pressure of the liquid mixtures formed during rectification.
    3. The method according to claim 1, wherein the rectification of the overhead product is carried out at a temperature in the upper part of the column.
    180-325 K, and in the lower part - 230450 K.
    4. Method pop. 1, characterized in that the washing is carried out at a lower temperature.
    5. Method pop. 1 and DECLINED c. in that the washing is carried out at a rectification temperature.
    6. The method according to claim 1, is also distinguished by the fact that the washing is carried out at a rectification pressure.
    The invention relates to the technology of separation of the gas mixture, in particular to the method of separation of a gas mixture under pressure containing methane, ethane, propane, hydrocarbons and C, hydrogen sulfide, carbon dioxide 1 nitrogen, I There is a known method of separation of gas mixture under pressure containing coal hydrogen and inorganic impurities, which consists in the fact that the initial gas mixture is subjected to cooling followed by feeding to the first stage of distillation, from which the mixture of methane and nitrogen is removed as a head product, as a bottom product and a mixture of hydrocarbons C as a side stream, which are fed to the second stage of distillation with removal of methane and carbon dioxide as the main product fed to the carbon dioxide purification stage by treatment with a polar organic solvent such as methanol and hydrocarbon C24 B as of the bottom product, wherein the head products of the first and second stages of distillation are subjected to condensation fl. ° The disadvantage of this method is its multistage stage and the fact that hydrochloric product of the second step comprises recto fication C ,, hydrocarbons that complicated purification step by methane from carbon dioxide due to the formation of azeotropic mixture with methanol. The closest to the invention in its technical essence and the achieved result is a method for separating a gas mixture under pressure containing methane, ethane, propane, hydrocarbons C (j and Cg, hydrogen sulfide, carbon dioxide and nitrogen, including cooling with washing to remove hydrogen sulfide and part of the dioxide carbon, partial condensation of the gas mixture, separation and separate distillation of the liquid and vapor phases formed 2. The disadvantage of this method is that the one-stage washing of the gas mixture in the presence of a large amount of Higher hydrocarbons ensure complete removal of inorganic impurities, in particular carbon dioxide and hydrogen sulfide. In addition, part of the hydrocarbons is separated by the formation of an azeotrope with a washing agent. The aim of the invention is to increase the degree of separation of the gas mixture. a pressurized gas mixture containing methane, ethane, propane, C4 and C5 hydrocarbons, hydrogen sulfide, hydrocarbon dioxide and nitrogen, including cooling with flushing for hydrogen sulfide and parts of carbon dioxide, partial condensation of the gas mixture, separation and separate rectification of the liquid and vapor phases formed, condensation is carried out before the Cz-C5 hydrocarbons liquefy and, at the liquid rectification stage, methane and ethane are separated, this washing is subjected to the head product of rectification with separate removal of carbon dioxide and hydrogen sulfide residues. Moreover, the washing is carried out at a temperature of less than 0 ° C and at a rectification pressure. At the same time, the rectification of the overhead product is carried out at a temperature in the upper part of the column of 180-325 K, and in the lower part - 230-450 K and at a pressure between the critical pressure of individual hydrocarbons and the lowest critical pressure of the liquid mixtures formed during the rectification, and rinsing i conduct; at negative temperatures, in particular at the temperature of rectification, and at the pressure of rectification. In addition, the washing is carried out at a rectification temperature. The drawing shows an installation that implements the proposed method. The method is carried out as follows. Example. Pipeline 1 p yields 40,000 kmol of gas having a temperature of 316 K, a pressure of 63 bar and the following composition, mol.%: Hydrocarbons DiC Hydrocarbons At 25 hours / mil in heat exchanger 2, the gas is cooled to 196 K with two gas streams and then gas is fed separator 3, where the liquid is separated, which, in comparison with the raw gas, is enriched in higher hydrocarbons. Liquid (1200 kmol / h; composition, mol.%: 25.5, 11.6, 17.3, 19.2 carbon of SL, 22.1 hydrocarbons C 4.3 CO-2 and 35 ppm: .) discharged through line 4. Gas from the separator 3 is removed through line 5, which basically corresponds to raw gas depleted in higher hydrocarbons. The gas is divided into two streams, which are cooled in heat exchangers 6 and 7. Both streams are combined and at 265 K are fed to the distillation column 8, the upper part of which is equipped with a cooler, and the lower part with a heater. The temperature in the upper part is 244 K, and in a cube 319 K. The rectification is carried out at a pressure of 61.6 bar. The critical pressure of the liquids to be rectified in each place of the column is more than 70 bar, so that there is enough difference between the working and critical pressures, but the critical pressures of individual hydrocarbons lie below the working pressure. The gas discharged from the upper part of the pipeline 9 has the following composition, mol%: Hydrocarbons C Hydrocarbons C., 6.42 21 ppm / mill The mixture withdrawn from the bottom of the rectification column 8 has the following composition, mol%: CH420.07 18.50 27.43 20.97 Hydrocarbons C, 6.97 Hydrocarbons C 6.06 CO 7 55 ppm. The gas withdrawn from the top of the distillation column 8 is fed via conduit 9 to the heat exchanger 7, in which it is heated. It then enters the bottom of the wash column 10, equipped with a coolant. In this column, the gas is irrigated with methanol at 238 K, supplied in the amount of 2000 t / h. In this case, the higher hydrocarbons, hydrogen sulfide and carbon dioxide are completely removed from the gas. A gas at 238 K is withdrawn from the top of the wash column through line 11, which is heated to 268-273 K in heat exchanger 6. Then the gas is fed to heat exchanger 2, in which it gives the residual cold to the raw gas. Pipe 12 is used to withdraw gas of the composition, mol%: 92.61 CH, 7.32 N and 0.17 N. It can be used, for example, for gas supply to remote consumers. The washing liquid is discharged from the bottom of the column 10, the valve 13 is adjusted to e) a pressure of 21 bar and then fed to the separator 14. The gas discharged from the separator has the composition, mol%: 72.50 CH, 14.64 CjH, 9.82 CO2, the rest -. higher hydrocarbons. Gas is fed to compressor 15, in which it is brought to washing pressure and then recycled to wash column 10. Liquid discharged from separator 14 is fed to valve 16, in which the pressure is reduced to 2 bar. Then the liquid is fed to the regeneration in the column 17, in which the liquid is washed with methanol by irrigation. With etrm, the temperature in the top column is 243 K, and the bottom of the column is heated. From the upper part of the column 17, gas 18 is withdrawn through line 18, which gives off its cold in heat exchangers 6 and 2. Gas 19 of the composition, mol.%: 22.20 CH, 27.23, 6.94 and 43, 63 CO2, which is (CAN BE used as fuel. Cubic liquid of the column 17 in the pump 20 is compressed to a pressure of 4 bar and after heating in the heat exchanger 21 it is supplied for regeneration to the upper part of the column 22, the temperature in the upper part of which is maintained at 298 K, and in a cube, 381 K. In this column, almost all dissolved substances are removed from the washing liquid; pump 23, the washing liquid is brought to the washing pressure and fed into the pipe 24 through the heat exchanger 21, then in the heat exchanger 25 it is brought to the washing temperature conducted in the column 10. Before being supplied to the heat exchanger .25, the pipeline 24 is taken to regenerate the column 17, the amount of wash liquid that is expanded in the valve 26. The gas withdrawn from the upper part of the column 22 is free of C2 hydrocarbons and consists mainly of C hydrocarbons, carbon dioxide and hydrogen sulfide. This gas is compressed to a pressure of 24 bar in the compressor 27, is pre-cooled in the cooler 28, then cooled in the coil of the cube of the column 17 and fed through a duct 29 to the distillation column 30, the upper part of which is supplied with a cooler, and the lower part - with a heater. The temperature in the upper part is 240 K. In this distillation column, pipeline 4 also supplies liquid from separator 3, which is preliminarily expanded into valve 31, and pipeline 32, liquid from distillation column 8, which is pre-expanded in valve 33. Rectification in column 30 leads to the separation of the gas mixture into the head fraction ((composition, mol.%: 41.56 Cri, 34.34, 0.59 C, Hg, 23.51 COj and 20 h, / mil. ), which is withdrawn through conduit 34 and added to the gas from separator 14, which is fed through compressor 15 to washing column 10, and the bottom fraction (composition, mol,%: 54.62 C, Nd, 32.62 C-hydrocarbons, 12.70 Ci-hydrocarbons, 0.03 COg and 0.03), which is fed to unit 35, in which the mixture hydrocarbons can be divided into individual fractions by known methods. Thus, the proposed method allows for a more complete separation of the mixture and its purification from inorganic impurities.
    权利要求:
    Claims (6)
    [1]
    157) 1. METHOD FOR SEPARATING A GAS MIXTURE UNDER PRESSURE containing
    35 ΕΣΞΞ} methane, ethane, propane, C4 and C hydrocarbons , hydrogen sulfide, carbon dioxide and nitrogen, including cooling with washing to remove hydrogen sulfide and part of the carbon dioxide, a partial concentration of the gas mixture, separation and separate rectification of the formed liquid and vapor phases, characterized in that, in order to increase the degree of separation, the condensation is carried out before liquefaction C3-C5 · hydrocarbons and methane and ethane are isolated at the stage of rectification of the liquid phase, while the head of the rectification product is subjected to washing with separate removal of carbon dioxide and hydrogen sulfide residues.
    SU .. "1085515
    [2]
    2. The method according to π.1, is distinguished by the fact that the rectification of the head product is carried out at a pressure between the critical pressure of the individual hydrocarbons and the lowest critical pressure of the liquid mixtures formed during rectification.
    [3]
    3. The method of pop. 1, characterized in that the distillation of the head product is carried out at a temperature in the upper part of the column
    180-3.25 K, and at the bottom - 230450 K.
    [4]
    4. The way to pop. 1, characterized in that the washing is carried out at a temperature of less than 0 9 C.
    [5]
    5. The way popp. 1 and 3, distinguishing with. I that washing is carried out at a temperature of distillation.
    [6]
    6. The method of pop. 1, characterized in that the washing is carried out at a distillation pressure.
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    同族专利:
    公开号 | 公开日
    FR2429981B1|1983-02-18|
    US4276057A|1981-06-30|
    FR2429981A1|1980-01-25|
    DE2828498A1|1980-01-17|
    CA1087086A|1980-10-07|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2026265A|1933-08-09|1935-12-31|Mid Continent Petroleum Corp|Process of recovering olefine hydrocarbons from gases|
    US2596785A|1946-07-08|1952-05-13|Pritchard & Co J F|Method of enriching natural gas|
    US2849371A|1954-09-27|1958-08-26|Phillips Petroleum Co|Separation and recovery of hydrocarbons from gaseous mixtures thereof|
    US2815650A|1955-07-01|1957-12-10|Phillips Petroleum Co|Reboiled absorber operation|
    DE1095866B|1959-09-30|1960-12-29|Linde S Eismaschinen Ag Zweign|Process and device for the separation of carbon dioxide from compressed gases|
    US3213154A|1962-05-28|1965-10-19|Phillips Petroleum Co|Hydrocarbon treating|
    US3242682A|1963-09-23|1966-03-29|Eastman Kodak Co|Method for separation of hydrocarbons|
    US3595782A|1968-12-05|1971-07-27|Fluor Corp|Method for separating crabon dioxide from hydrocarbons|
    US3977203A|1974-03-25|1976-08-31|Kansas University Endowment Association|Purification of natural gas by liquid/liquid extraction with a polar solvent|
    US4012212A|1975-07-07|1977-03-15|The Lummus Company|Process and apparatus for liquefying natural gas|US4526594A|1982-05-03|1985-07-02|El Paso Hydrocarbons Company|Process for flexibly rejecting selected components obtained from natural gas streams|
    CA1215217A|1983-06-24|1986-12-16|Yuv R. Mehra|Process for extracting natural gas streams withphysical solvents|
    US4511381A|1982-05-03|1985-04-16|El Paso Hydrocarbons Company|Process for extracting natural gas liquids from natural gas streams with physical solvents|
    US4578094A|1983-09-14|1986-03-25|El Paso Hydrocarbons|Hydrocarbon separation with a physical solvent|
    US4623371A|1984-08-03|1986-11-18|El Paso Hydrocarbons Company|Utilizing the Mehra process for processing and BTU upgrading of nitrogen-rich natural gas streams|
    GB8411686D0|1984-05-08|1984-06-13|Stothers W R|Recovery of ethane and natural gas liquids|
    US6793712B2|2002-11-01|2004-09-21|Conocophillips Company|Heat integration system for natural gas liquefaction|
    ITMI20022709A1|2002-12-20|2004-06-21|Enitecnologie Spa|PROCEDURE FOR THE REMOVAL OF THE SULFUR HYDROGEN CONTAINED IN NATURAL GAS.|
    DE102005025958A1|2005-06-03|2006-12-07|Uhde Gmbh|Process for the depletion of hydrogen sulphide in natural gas|
    US7430858B2|2006-01-11|2008-10-07|Hoff Jr Robert A|System to generate inert gas from exhaust gas|
    EP2029949A2|2006-06-16|2009-03-04|Shell Internationale Research Maatschappij B.V.|Method and apparatus for treating a hydrocarbon stream|
    US7909913B2|2008-07-17|2011-03-22|Air Products And Chemicals, Inc.|Gas purification by adsorption of hydrogen sulfide|
    FR2947185B1|2009-06-26|2011-07-01|Total Sa|PROCESS FOR TREATING ACIDIC GASES|
    FR2990878B1|2012-05-25|2014-05-16|Total Sa|PROCESS FOR THE PURIFICATION OF GASEOUS MIXTURES CONTAINING ACIDIC GASES|
    DE102016200565A1|2016-01-18|2017-07-20|Linde Aktiengesellschaft|Process for the separation process of a gas mixture|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE19782828498|DE2828498A1|1978-06-29|1978-06-29|METHOD AND DEVICE FOR DISASSEMBLING A GAS MIXTURE|
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