RU2007125703A - METHOD AND DEVICE FOR PRODUCING LIQUID NATURAL GAS FLOW - Google Patents

METHOD AND DEVICE FOR PRODUCING LIQUID NATURAL GAS FLOW Download PDF

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RU2007125703A
RU2007125703A RU2007125703/04A RU2007125703A RU2007125703A RU 2007125703 A RU2007125703 A RU 2007125703A RU 2007125703/04 A RU2007125703/04 A RU 2007125703/04A RU 2007125703 A RU2007125703 A RU 2007125703A RU 2007125703 A RU2007125703 A RU 2007125703A
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stream
substream
distillation column
supply point
washing
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RU2007125703/04A
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Russian (ru)
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RU2402592C2 (en
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Марко Дик ЯГЕР (NL)
Марко Дик Ягер
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Шелл Интернэшнл Рисерч Маатсхаппий Б.В. (NL)
Шелл Интернэшнл Рисерч Маатсхаппий Б.В.
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    • 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
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0247—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 4 carbon atoms or more
    • 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
    • C10G2300/10—Feedstock materials
    • C10G2300/1025—Natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/50—Processes or apparatus using other separation and/or other processing means using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/20—Integration in an installation for liquefying or solidifying a fluid stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Claims (17)

1. Способ производства потока сжиженного природного газа, в котором перед сжижением природного газа из его потока удаляют тяжелые углеводородные компоненты с молекулярным весом, большим молекулярного веса бутана, включающий следующие этапы, на которых создают в основном парообразный поток (1) природного газа с давлением и температурой потока подаваемого газа; подают поток подаваемого газа (1) в дистилляционную колонну (10), имеющую две или больше ступени (11) сепарации; отбирают нижний поток (17) из нижней части дистилляционной колонны (10) и верхний поток (16) из верхней части дистилляционной колонны (10), причем верхний поток (16) содержит относительно меньшее количество компонентов тяжелых углеводородов, чем нижний поток (17); и сжижают по меньшей мере часть верхнего потока (16), в результате чего получают поток сжиженного природного газа; отличающийся тем, что перед подачей потока (1) газа в дистилляционную колонну (10) разделяют поток (1) подаваемого газа на первый и второй подпотоки (3а, 3b) с выбранным соотношением разделения; подают первый подпоток (3а) в дистилляционную колонну (10) через первую точку (7а) подачи в нижней части дистилляционной колонны (10) под давлением не ниже давления подаваемого потока (1) за вычетом падения давления от указанного разделения подаваемого потока (1), причем первый подпоток (3а) не подвергают нагреву между точкой разделения подаваемого потока (1) и первой точкой (7а) подачи первого подпотока (3а) в дистилляционную колонну(10); охлаждают второй подпоток (3b) в теплообменнике (6) до температуры более низкой, чем температура потока подаваемого газа; подают охлажденный второй подпоток (7) в дистилляционную колонну (10) во второй точке (7b) подачи, расположенной выше первой точки (7а) подачи, при этом ни в первом, ни во втором подпотоках (3а, 3b) давление специально не понижают в устройстве понижения давления.1. A method of producing a stream of liquefied natural gas, in which heavy hydrocarbon components with a molecular weight greater than the molecular weight of butane are removed from the stream prior to liquefying natural gas, the process comprising the following steps, which create a substantially vaporous stream (1) of natural gas with pressure and gas flow temperature; supplying a feed gas stream (1) to a distillation column (10) having two or more separation stages (11); the lower stream (17) from the lower part of the distillation column (10) and the upper stream (16) from the upper part of the distillation column (10) are selected, the upper stream (16) containing a relatively lower amount of heavy hydrocarbon components than the lower stream (17); and liquefying at least a portion of the overhead stream (16), resulting in a liquefied natural gas stream; characterized in that before supplying the gas stream (1) to the distillation column (10), the supplied gas stream (1) is divided into first and second substreams (3a, 3b) with a selected separation ratio; the first substream (3a) is supplied to the distillation column (10) through the first supply point (7a) at the bottom of the distillation column (10) under a pressure not lower than the pressure of the feed stream (1) minus the pressure drop from the specified separation of the feed stream (1), moreover, the first substream (3A) is not subjected to heating between the separation point of the feed stream (1) and the first point (7a) of the supply of the first substream (3a) to the distillation column (10); cooling the second substream (3b) in the heat exchanger (6) to a temperature lower than the temperature of the feed gas stream; a cooled second substream (7) is supplied to the distillation column (10) at a second supply point (7b) located above the first supply point (7a), while the pressure in either the first or second substreams (3a, 3b) is not specially reduced pressure reducing device. 2. Способ по п.1, отличающийся тем, что в основном парообразный подаваемый поток (1) газа содержит больше 90 об.% пара, предпочтительно, больше 95 об.%.2. The method according to claim 1, characterized in that basically the vaporous feed stream (1) of the gas contains more than 90 vol.% Steam, preferably more than 95 vol.%. 3. Способ по любому из пп.1 или 2, отличающийся тем, что падение давления в первом подпотоке (3а) между узлом разделения подаваемого потока (1) и первой точкой (7а) подачи меньше 6 бар, предпочтительно, меньше 3 бар.3. A method according to any one of claims 1 or 2, characterized in that the pressure drop in the first subflow (3a) between the separation unit of the feed stream (1) and the first supply point (7a) is less than 6 bar, preferably less than 3 bar. 4. Способ по любому из пп.1 или 2, отличающийся тем, что выбранное отношение разделения поддерживают меньше 1, предпочтительно меньше 1/5, более предпочтительно, меньше, чем 1/10, при этом отношение разделения представляет собой массовую скорость потока первого подпотока (3а), деленную на массовую скорость потока второго подпотока (3b).4. The method according to any one of claims 1 or 2, characterized in that the selected separation ratio is maintained less than 1, preferably less than 1/5, more preferably less than 1/10, wherein the separation ratio is the mass flow rate of the first substream (3a) divided by the mass flow rate of the second substream (3b). 5. Способ по п.4, отличающийся тем, что выбранное отношение разделения поддерживают большим 1/100, предпочтительно, больше 1/50.5. The method according to claim 4, characterized in that the selected separation ratio is maintained greater than 1/100, preferably greater than 1/50. 6. Способ по любому из пп.1 или 2, отличающийся тем, что второй подпоток (3b) охлаждают в теплообменнике (6) с использованием внешнего хладагента.6. The method according to any one of claims 1 or 2, characterized in that the second substream (3b) is cooled in the heat exchanger (6) using an external refrigerant. 7. Способ по п.1, отличающийся тем, что дистилляционная колонна (10) выполнена в виде промывной колонны, в которую промывной поток (18) подают через третью точку (7с) подачи, расположенную выше второй точки (7b) подачи, при температуре ниже, чем температура охлажденного второго подпотока (7).7. The method according to claim 1, characterized in that the distillation column (10) is made in the form of a washing column into which the washing stream (18) is supplied through a third supply point (7c) located above the second supply point (7b) at a temperature lower than the temperature of the cooled second substream (7). 8. Способ по п.7, отличающийся тем, что промывной поток (18) является по существу жидким.8. The method according to claim 7, characterized in that the wash stream (18) is essentially liquid. 9. Способ по любому из пп.7 или 8, отличающийся тем, что промывной поток (18) получают путем отбора фракции из второго подпотока (3b) для формирования третьего подпотока (22) и охлаждения третьего подпотока (22) во втором теплообменнике (26) для формирования промывного потока (18).9. The method according to any one of claims 7 or 8, characterized in that the washing stream (18) is obtained by taking a fraction from the second substream (3b) to form a third substream (22) and cooling the third substream (22) in the second heat exchanger (26 ) to form a wash flow (18). 10. Способ по любому из пп.7 или 8, отличающийся тем, что промывной поток получают путем частичной конденсации верхнего потока (16) с формированием потока со смешанной фазой паров и конденсата и отбора конденсата из сформированного потока со смешанной фазой для получения промывного потока (18).10. The method according to any one of claims 7 or 8, characterized in that the washing stream is obtained by partially condensing the overhead stream (16) to form a mixed-vapor stream and condensate and taking condensate from the formed mixed-phase stream to obtain a washing stream ( eighteen). 11. Способ по п.10, отличающийся тем, что часть верхнего потока (16), которую используют как промывной поток (18), не расширяют между промывной колонной и третьей точкой (7с) подачи.11. The method according to claim 10, characterized in that the part of the upper stream (16), which is used as a washing stream (18), is not expanded between the washing column and the third supply point (7c). 12. Способ по любому из пп.7 или 8, отличающийся тем, что температура промывного потока (18) является достаточно низкой для формирования конденсата из тяжелых углеводородов.12. The method according to any one of claims 7 or 8, characterized in that the temperature of the washing stream (18) is low enough to form condensate from heavy hydrocarbons. 13. Устройство для производства потока сжиженного природного газа, в котором перед сжижением природного газа из его потока удаляют тяжелые углеводородные компоненты с молекулярным весом, большим молекулярного веса бутана, содержащее линию (1) потока для подачи в основном парообразного потока (1) природного газа с давлением и температурой потока подаваемого газа, дистилляционную колонну (10) с двумя или более ступенями (11) сепарации для отделения компонентов тяжелых углеводородов от природного газа, причем в дистилляционной колонне (10) имеются отверстие (8) в нижней части для выпуска нижнего потока (17) и отверстие (12) в верхней части для выпуска верхнего потока (16) с меньшим относительным содержанием компонентов тяжелых углеводородов, чем в нижнем потоке (17); и низкотемпературную зону, в которой по меньшей мере часть верхнего потока (16) может быть сжижена с получением в результате потока сжиженного природного газа, отличающееся тем, что линия (1) подаваемого потока содержит узел (2) разветвления, соединяющий по текучей среде основную ветвь с первым и вторым ответвлениями с образованием первого и второго подпотоков (3а, 3b) с выбранным отношением разделения, при этом первое ответвление (3а) соединяет узел (2) разветвления подаваемого потока с первой точкой (7а) подачи в нижней части дистилляционной колонны (10) под давлением не ниже давления подаваемого потока за вычетом падения давления от указанного разделения подаваемого потока, а второе ответвление (3b) соединяет узел (2) разветвления подаваемого потока со второй точкой (7b) подачи в дистилляционной колонне (10), причем вторая точка (7b) подачи расположена выше первой точки (7а) подачи, и во втором ответвлении (3b) имеется теплообменник (6), при этом первая точка (7а) подачи расположена ниже самой нижней ступени (11) сепарации дистилляционной колонны (10), в первом подпотоке (3а) не предусмотрен теплообменник для его нагрева, а в первом и во втором подпотоках не предусмотрены отдельные средства для понижения давления.13. A device for producing a liquefied natural gas stream, in which, before liquefying natural gas, heavy hydrocarbon components with a molecular weight greater than the molecular weight of butane are removed from the stream, comprising a stream line (1) for supplying a substantially vaporous stream (1) of natural gas with pressure and temperature of the feed gas stream, a distillation column (10) with two or more stages (11) of separation to separate the components of heavy hydrocarbons from natural gas, and in the distillation column (10) have I opening (8) in the lower part for discharging a bottom stream (17) and an opening (12) at the top for release of the upper thread (16) with a lower relative content of heavy hydrocarbon components than the bottom stream (17); and a low-temperature zone in which at least a portion of the overhead stream (16) can be liquefied to produce a liquefied natural gas stream, characterized in that the feed stream line (1) comprises a branching unit (2) fluidly connecting the main branch with the first and second branches with the formation of the first and second substreams (3a, 3b) with the selected separation ratio, while the first branch (3a) connects the node (2) branching of the feed stream with the first point (7a) of the supply at the bottom of the distillation data (10) at a pressure not lower than the pressure of the feed stream minus the pressure drop from the specified separation of the feed stream, and the second branch (3b) connects the node (2) for branching the feed stream to the second point (7b) of the feed in the distillation column (10), and the second supply point (7b) is located above the first supply point (7a), and in the second branch (3b) there is a heat exchanger (6), while the first supply point (7a) is located below the lowest separation stage (11) of the distillation column (10) , the first substream (3a) does not provide heat exchanger to heat it, and in the first and second substreams no separate means are provided for reducing the pressure. 14. Устройство по п.13, отличающееся тем, что дистилляционная колонна (10) выполнена в виде промывной колонны, при этом устройство снабжено источником промывного потока, соединенным с промывной колонной через третью точку (7с) подачи в промывной колонне выше второй точки (7b) подачи.14. The device according to item 13, wherein the distillation column (10) is made in the form of a wash column, the device is provided with a wash flow source connected to the wash column through a third supply point (7c) in the wash column above the second point (7b ) filing. 15. Устройство по п.14, отличающееся тем, что источник промывного потока включает второй узел (20) разветвления, выполненный во втором ответвлении (3b) перед второй точкой подачи для образования третьего ответвление (22), отходящего от второго ответвления (3b), при этом в третьем ответвлении (22) имеется второй теплообменник (26).15. The device according to 14, characterized in that the source of the washing stream includes a second branch node (20) made in the second branch (3b) in front of the second supply point to form a third branch (22), extending from the second branch (3b), in the third branch (22) there is a second heat exchanger (26). 16. Устройство по любому из пп.14 или 15, отличающееся тем, что источник промывного потока содержит конденсатор (14) для получения выходящего из промывной колонны верхнего потока (16) и сепаратор (27), имеющий выходное отверстие (33) для конденсата и выходное отверстие (35) для паров, причем выходное отверстие (33) для конденсата соединено с промывной колонной через третью точку (7с) подачи.16. Device according to any one of paragraphs.14 or 15, characterized in that the source of the washing stream contains a condenser (14) for receiving the upper stream leaving the washing column (16) and a separator (27) having an outlet (33) for condensate and an outlet (35) for vapors, the outlet (33) for condensate being connected to the wash column through a third supply point (7c). 17. Устройство по любому из пп.14 или 15, отличающееся тем, что между выходным отверстием (12) выпуска верхнего потока и третьей точкой (7с) подачи не имеется расширителя. 17. Device according to any one of paragraphs.14 or 15, characterized in that between the outlet (12) of the upper flow outlet and the third supply point (7c) there is no expander.
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