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RU2770523C2 - Unit for c3+ hydrocarbon recovery from natural gas by low-temperature condensation - Google Patents

Unit for c3+ hydrocarbon recovery from natural gas by low-temperature condensation Download PDF

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RU2770523C2
RU2770523C2 RU2020133268A RU2020133268A RU2770523C2 RU 2770523 C2 RU2770523 C2 RU 2770523C2 RU 2020133268 A RU2020133268 A RU 2020133268A RU 2020133268 A RU2020133268 A RU 2020133268A RU 2770523 C2 RU2770523 C2 RU 2770523C2
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supply line
demethanizer
line
heat exchanger
gas
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RU2020133268A
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Russian (ru)
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RU2020133268A (en
RU2020133268A3 (en
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Сергей Васильевич Акулов
Андрей Владиславович Курочкин
Алена Геннадиевна Чиркова
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Общество С Ограниченной Ответственностью "Пегаз Инжиниринг"
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Priority to RU2020133268A priority Critical patent/RU2770523C2/en
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    • 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
    • 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
    • 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
    • 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
    • F25J3/0238—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 2 carbon atoms 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
    • F25J3/0242—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 3 carbon atoms 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
    • 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
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/02—Mixing or blending of fluids to yield a certain product
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/32—Compression of the product 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • 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
    • 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)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

FIELD: gas industry.SUBSTANCE: invention relates to equipment for the extraction of heavy hydrocarbons from natural gas, it can be used in the gas industry. The invention relates to an installation for extracting C3+hydrocarbons from natural gas by means of low-temperature condensation, including a first recuperative heat exchanger equipped with a compression refrigeration machine located on the natural gas supply line, and a separator equipped with a separation gas supply line with a second recuperative heat exchanger connected to a demethanizer by a separation residue supply line with a reducing device. The top of the demethanizer is equipped with a line for the withdrawal of topped gas, on which the second and first recuperative heat exchangers are located, and the bottom of the demethanizer is equipped with a heater located on the bypass line of the first recuperative heat exchanger, and is also connected by a line for the supply of demethanized condensate with a fractionation unit equipped with lines for the withdrawal of hydrocarbon fractions and connected by a line for the withdrawal of methane-containing gas with a line for the withdrawal of topped gas. On the separation gas supply line to the demethanizer, after the second recuperative heat exchanger, an additional separator is installed, connected to the demethanizer by a separation residue supply line with a reducing device and an additional separation gas supply line with an expander connected by kinematic, and/or electric, and/or magnetic, and/or hydraulic devices with a drive(s) of the compression refrigeration machine and/or other cooling devices of the fractionation unit and a refrigeration machine connected to the first recuperative heat exchanger.EFFECT: increased energy efficiency.1 cl, 1 ex, 1 dwg

Description

Изобретение относится к оборудованию для извлечения тяжелых углеводородов из природного гам и может быть использовано в газовой промышленности.The invention relates to equipment for the extraction of heavy hydrocarbons from natural gas and can be used in the gas industry.

Известна установка низкотемпературного разделения углеводородного газа [RU 2382301, опубл. 20.02.2010 г., МПК F25J 3/00], которая включает расположенный на линии подачи углеводородного газа узел охлаждения в составе теплообменников и пропанового холодильника (холодильной машины), а также сепаратор, соединенный с фракционирующей колонной (деметанизатором) линиями подачи газа и остатка с редуцирующими устройствами (редуцирующим вентилем и детандерной секцией детандер-компрессорного агрегата, соответственно), при этом низ деметанизатора соединен с деэтанизатором (блоком фракционирования) линией подачи деметанизированного конденсата с насосом и нагревателем, расположенным на байпасе узла охлаждения, и ос нашей нагревателем низа деметанизатора, расположенным на линии подачи газа деэтанизации (этановой фракции), соединяющей блок фракционирования с верхом демеханизатора, на шторой затем расположены нагреватель отбензиненного газа и редуцирующий вентиль, при этом верх деметанизатора оснащен линией вывода отбензиненного газа с нагревателем, узлом охлаждения и компрессорной секцией детандер-компрессорного агрегата.Known installation of low-temperature separation of hydrocarbon gas [RU 2382301, publ. February 20, 2010, IPC F25J 3/00], which includes a cooling unit located on the hydrocarbon gas supply line, consisting of heat exchangers and a propane refrigerator (refrigerator), as well as a separator connected to the fractionating column (demethanizer) by gas and residue supply lines with reducing devices (reducing valve and expander section of the expander-compressor unit, respectively), while the bottom of the demethanizer is connected to the demethanizer (fractionation unit) by a demethanizer condensate supply line with a pump and a heater located on the bypass of the cooling unit, and with our heater at the bottom of the demethanizer, located on the deethanization gas (ethane fraction) supply line connecting the fractionation unit with the top of the demechanizer, then the top gas heater and the reducing valve are located on the curtain, while the top of the demethanizer is equipped with a top gas outlet line with a heater, a cooling unit and a compressor section thunder compressor unit.

Недостатками данной установки являются низкая степень извлечения тяжелых компонентов газа и высокие энергозатраты.The disadvantages of this installation are the low degree of extraction of heavy gas components and high energy consumption.

Наиболее близка к предлагаемому изобретению установка низкотемпературного разделения углеводородного газа [RU 2724739, опубл. 25.05.2020 г., МПК F25J 3/00], которая включает расположенные на линии подачи углеводородного газа первый рекуперативный теплообменник и сепаратор, соединенный с деметанизатором линией подачи газа сепарации со вторым рекуперативным теплообменником и редуцирующим устройством и линией подачи остатка сепарации с редуцирующим устройством, при этом верх демеганизатора оснащен линией вывода отбензиненного газа, на которой расположены первый и второй рекуперативные теплообменники, а низ деметанизатора оснащен нагревателем, расположенным на байпасной линии первого рекуперативного теплообменника, а также соединен линией подачи деметанизированного конденсата с блоком фракционирования, оснащенным линиями вывода углеводородных фракций и соединенным линией вывода этановой фракции (метансодержащего газа) с линией вывода отбензиненного газа, кроме того первый рекуперативный теплообменник соединен с холодильной машиной линиями ввода/вывода хладоагента.Closest to the proposed invention installation low-temperature separation of hydrocarbon gas [RU 2724739, publ. 05/25/2020, IPC F25J 3/00], which includes the first recuperative heat exchanger and separator located on the hydrocarbon gas supply line, connected to the demethanizer by a separation gas supply line with a second recuperative heat exchanger and a reducing device and a separation residue supply line with a reducing device, at the same time, the top of the demethanizer is equipped with a stripped gas outlet line, on which the first and second recuperative heat exchangers are located, and the bottom of the demethanizer is equipped with a heater located on the bypass line of the first recuperative heat exchanger, and is also connected by a demethanized condensate supply line to a fractionation unit equipped with hydrocarbon fractions and connected by an ethane fraction (methane-containing gas) output line to a stripped gas output line, in addition, the first recuperative heat exchanger is connected to the refrigeration machine by refrigerant input/output lines.

Недостатками данной установки является низкая энергоэффективность из-за затрат сторонней энергии при фракционировании деметанизированного конденсата в блоке фракционирования на охлаждение верха колонн (например, деэтанизатора).The disadvantages of this installation is low energy efficiency due to the cost of third-party energy in the fractionation of demethanized condensate in the fractionation unit for cooling the top of the columns (for example, deethanizer).

Задачей предлагаемого изобретения является повышение эпергоэффективности.The objective of the invention is to improve energy efficiency.

Техническим результатом является повышение энергоэффективности за счет исключения использования энергии со стороны на охлаждение верха колонн блока фракционирования путем установки на линии подачи газа сепарации в деметанизатор дополнительного сепаратора, а на линии подачи газа дополнительной сепарации - детандера, соединенного с приводом(ами) компрессионной холодильной машины и/или иных охлаждающих устройств блока фракционирования.The technical result is to increase energy efficiency by eliminating the use of energy from the side for cooling the top of the fractionation unit columns by installing an additional separator on the separation gas supply line to the demethanizer, and on the additional separation gas supply line - an expander connected to the drive(s) of the compression refrigeration machine and /or other cooling devices of the fractionation unit.

Указанный технический результат достигается тем, что в предлагаемой установке, включающей расположенные на линии подачи природного газа первый рекуперативный теплообменник, оснащенный компрессионной холодильной машиной, и сепаратор, оснащенный линией подачи газа сепарации со вторым рекуперативным теплообменником, соединенный с деметанизатором линией подачи остатка сепарации с редуцирующим устройством» при этом верх демеганизатора оснащен линией вывода отбензиненного газа» на которой расположены второй и первый рекуперативные теплообменники, а низ демеганизатора оснащен нагревателем, расположенным на байпасной линии первого рекуперативного теплообменника, а также соединен линией подачи деметанизированного конденсата с блоком: фракционирования, оснащенным линиями вывода углеводородных фракций и соединенным линией вывода метансодержащего газа с линией вывода отбензиненного газа, особенностью является то, что на. линии подачи газа сепарации в деметанизатор после второго рекуперативного теплообменника установлен дополнительный сепаратор, соединенный с деметанизатором линией подачи остатка сепарации с редуцирующим устройством и линией подачи газа дополнительной сепарации, с детандером, соединенным посредством кинематических, и/или электрических и/или магнитных и/или гидравлических устройств с приводом(ами) компрессионной холодильной и/или иных охлаждающих устройств блока фракционирования и холодильной машиной соединенной с первым рекуперативным теплообменником.The specified technical result is achieved by the fact that in the proposed installation, which includes the first recuperative heat exchanger located on the natural gas supply line, equipped with a compression refrigeration machine, and a separator equipped with a separation gas supply line with a second recuperative heat exchanger, connected to the demethanizer by a separation residue supply line with a reducing device "at the same time, the top of the demeganizer is equipped with a stripped gas outlet line" on which the second and first recuperative heat exchangers are located, and the bottom of the demeganizer is equipped with a heater located on the bypass line of the first recuperative heat exchanger, and is also connected by a demethanized condensate supply line to the fractionation unit equipped with hydrocarbon outlet lines fractions and connected by a methane-containing gas outlet line to a stripped gas outlet line, the feature is that on. separation gas supply line to the demethanizer after the second recuperative heat exchanger, an additional separator is installed, connected to the demethanizer by a separation residue supply line with a reducing device and an additional separation gas supply line, with an expander connected by means of kinematic and/or electric and/or magnetic and/or hydraulic devices with a drive(s) for compression refrigeration and/or other cooling devices of the fractionation unit and a refrigeration machine connected to the first recuperative heat exchanger.

Блок фракционирования включает, например, ректификационные колонны в количестве и с характеристиками, обусловленными заданным ассортиментом жидких продуктов. В качестве охлаждающих устройств блока фракционирования использованы, например, компрессионные холодильные машины или аппараты воздушного охлаждения с вентиляторами. Редуцирующие устройства выполнены в виде дроссельного вентиля, газодинамического устройства mm детандера. В качестве остальных элементов установки могут быть размещены любые устройства соответствующего назначения, известные из уровня техники.The fractionation unit includes, for example, distillation columns in quantity and with characteristics due to a given range of liquid products. As cooling devices for the fractionation unit, for example, compression chillers or air coolers with fans are used. The reducing devices are made in the form of a throttle valve, a gas-dynamic device mm expander. As other elements of the installation, any devices of the appropriate purpose, known from the prior art, can be placed.

Для увеличения выхода тяжелых компонентов установка может быть дополнена редуцирующим устройством, расположенным на линии вывода отбензиненного газа из деметанизатора. На линии вывода отбензиненного газа после первого рекуперативного теплообменника может быть расположен дожимной компрессор. Приводы охлаждающих устройств и/или дожимной компрессор могут быть соединены с детандером (ами) посредством кинематических и/или электрических и/или магнитных и/или гидравлических устройств.In order to increase the output of heavy components, the plant can be supplemented with a reducing device located on the line for the removal of stripped gas from the demethanizer. A booster compressor may be located in the line of off-gas outlet after the first recuperative heat exchanger. The drives of the cooling devices and/or the booster compressor may be connected to the expander(s) by means of kinematic and/or electrical and/or magnetic and/or hydraulic devices.

Установка дополнительного сепаратора на линии подачи газа сепарации в деметанизатор, детандера, соединенного с приводом(ами) компрессионной холодильной и/или иных охлаждающих устройств блока фракционирования, на линии подачи газа дополнительной сепарации позволяет осуществить фракционирование в блоке фракционирования за счет собственного энергоресурса - энергии, подаваемой детандером на приводы охлаждающих устройств. Это позволяет исключить использование энергии со стороны для привода охлаждающих устройств и за счет большей удельной холодопроизводительности последних (относительно варианта непосредственного использования холода технологических потоков) повысить энергоэффективность установки, а также несколько увеличить глубину отбора тяжелых углеводородов.Installation of an additional separator on the separation gas supply line to the demethanizer, an expander connected to the drive(s) of the compression refrigeration and/or other cooling devices of the fractionation unit, on the additional separation gas supply line allows fractionation to be carried out in the fractionation unit at the expense of its own energy resource - the energy supplied expander for drives of cooling devices. This makes it possible to exclude the use of energy from outside to drive the cooling devices and, due to the greater specific cooling capacity of the latter (relative to the option of direct use of the cold of process streams), to increase the energy efficiency of the installation, as well as to slightly increase the depth of heavy hydrocarbon extraction.

Установка показана на прилагаемом чертеже и включает первый и второй сепараторы 1 и 2, первый и второй рекуперативный теплообменники 3 и 4, деметанизатор 5, редуцирующие устройства 6 и 7, детандер 8, блок фракционирования в составе фракционирующих колонн 9 и охлаждающих устройств 10 (условно показано одна холодильная машина), компрессионная холодильная машина 11. Установка может быть дополнена редуцирующим устройством 12 и компрессором 13 (показано пунктиром).The installation is shown in the attached drawing and includes the first and second separators 1 and 2, the first and second recuperative heat exchangers 3 and 4, the demethanizer 5, the reducing devices 6 and 7, the expander 8, the fractionation unit as part of the fractionation columns 9 and the cooling devices 10 (conditionally shown one refrigerating machine), compression refrigerating machine 11. The installation can be supplemented with a reducing device 12 and a compressor 13 (shown in dotted line).

При работе установки природный газ, поступающий по линии 14, разделяют на два потока, первый по байпасной (по отношению к теплообменнику 3) линии 15 подают в качестве теплоносителя в нагреватель демеганизатора 5, смешивают со вторым потоком, охлажденным в теплообменнике 3, и разделяют в сепараторе I на остаток, выводимый но линии 16, и газ, охлаждаемый в теплообменнике 4, который разделяют в сепараторе 2 на остаток, выводимый по линии 17, и газ. Остатки сепарации и газ и редуцируют устройствах 6, 7 и в детандере 8, соответственно, и подают в деметанизатор 5, с низа которого по линии 18 деметанизированный конденсат подают в блок 9, из которого по линиям 19 выводят углеводородные фракции в заданном ассортименте. При фракционировании в блоке 9 для охлаждения верха колонн используют холод, генерируемый охлаждающими устройствами 10, которые соединены с детандером(ами) (показано штрих-пунктиром), Отбензиненный газ, выводимый с верха деметанизатора 5 по линии 20, нагревают и теплообменнике 4, смешивают с метансодержащим газом, подаваемым из блока 9 по линии 21, нагревают в теплообменнике 3 и выводят по линии 22. Первый рекуперативный теплообменник 3 дополнительно охлаждают е помощью компрессионной холодильной машины. 11, также соединенной с детандером(ами).During operation of the plant, natural gas supplied through line 14 is divided into two streams, the first one is fed through the bypass (with respect to heat exchanger 3) line 15 as a heat carrier to the heater of demeganizer 5, mixed with the second stream cooled in heat exchanger 3, and separated into separator I into the residue discharged through line 16 and the gas cooled in the heat exchanger 4, which is separated in the separator 2 into the residue discharged through line 17 and the gas. Separation residues and gas are reduced in devices 6, 7 and in expander 8, respectively, and fed into demethanizer 5, from the bottom of which, via line 18, demethanized condensate is fed to unit 9, from which hydrocarbon fractions are removed via lines 19 in a given range. In the fractionation in unit 9, the cold generated by the cooling devices 10, which are connected to the expander(s) (shown in dash-dotted line), is used to cool the tops of the columns. methane-containing gas supplied from block 9 through line 21 is heated in heat exchanger 3 and removed through line 22. The first recuperative heat exchanger 3 is additionally cooled by means of a compression refrigeration machine. 11 also connected to the expander(s).

При необходимости (показано пунктиром) отбензиненный газ до рекуперационного холодильника 4 редуцируют с помощью устройства 12 и сжимают компрессором 13, а метансодержащий газ из блока 9 перед подачей в линию 20 нагревают в теплообменнике 3.If necessary (shown by the dotted line), the stripped gas is reduced to the recovery cooler 4 using the device 12 and compressed by the compressor 13, and the methane-containing gas from the unit 9 is heated in the heat exchanger 3 before being supplied to the line 20.

Работоспособность установки подтверждается следующим примером: сырой природный газ, содержащий 59,1 г/нм3 углеводородов C3+, в объеме 119,0 тыс. нм3/ч при 6,25 МПа и 45°С разделяют на два потока, 25,6 тыс, нм3/ч первого потока подают на охлаждение в нагреватель деметанизатора, смешивают со вторым потоком, охлажденным в первом рекуперативном теплообменнике, и при минус 43,4°С разделяют в первом сепараторе на 4,0 т/час остатка, и 116,1 тыс. нм3/ч газа, который после охлаждения во втором рекуперативном теплообменнике ло минус 61,5°С разделяют во втором сепараторе на 8,2 т/час остатка, и 107,4 тыс. нм3/ч газа сепарации. Остатки сепарации и газ сепарации редуцируют до 3,3 МПа с помощью редуцирующих устройств, выполненных в виде двух редуцирующих вентилей и детандера, соответственно, и подают в деметанизатор. С низа деметанизатора выводят l1,6 т/час деметанизированного конденсата и подают в блок фракционирования, из которого выводят 7,5 т/час пропана-бутана автомобильного. Верх деэтанизатора блоки фракционирования охлаждают с. помощью холодильной машины с холодопроизводительностъю 520 кВт, записанной от детандера, 112,4 тыс. нм3/ч подготовленного газа, выводимого с верха демеганизатора, нагревают во втором рекуперативномThe operability of the plant is confirmed by the following example: raw natural gas containing 59.1 g/nm 3 C 3+ hydrocarbons in the amount of 119.0 thousand nm 3 /h at 6.25 MPa and 45°C is divided into two streams, 25, 6 thousand nm 3 /h of the first stream is fed to the demethanizer heater for cooling, mixed with the second stream, cooled in the first recuperative heat exchanger, and at minus 43.4 ° C, it is separated in the first separator into 4.0 t/h of the residue, and 116 ,1 thousand Nm 3 /h of gas, which, after cooling in the second recuperative heat exchanger lo minus 61.5°C, is divided in the second separator into 8.2 t/h of the residue, and 107.4 thousand Nm 3 /h of separation gas. Separation residues and separation gas are reduced to 3.3 MPa using reducing devices made in the form of two reducing valves and an expander, respectively, and fed into the demethanizer. From the bottom of the demethanizer, l1.6 t/h of demethanized condensate is removed and fed to the fractionation unit, from which 7.5 t/h of automotive propane-butane are removed. The top of the deethanizer fractionation blocks are cooled off. using a refrigerating machine with a cooling capacity of 520 kW recorded from the expander, 112.4 thousand nm 3 / h of the prepared gas discharged from the top of the demeganizer is heated in the second recuperative

теплообменнике, смешивают с 3,0 тыс. нм3/ч отходящего метансодержащего газа, подаваемого из блока фракционирования н выводят при 32,1°С. В первый рекуперативный теплообменник подают 357 кВт холода с помощью компрессионной холодильной машины, также запитанной от детандера.heat exchanger, mixed with 3.0 thousand Nm 3 /h of methane-containing off-gas supplied from the fractionation unit and removed at 32.1°C. The first recuperative heat exchanger is supplied with 357 kW of cold by means of a compression refrigeration machine, also powered by an expander.

Степень извлечения углеводородов С3+ составила 95,1%, энергия со стороны не использовалась.The degree of extraction of C 3+ hydrocarbons was 95.1%, no external energy was used.

При работе установки по прототипу в условиях примера, для привода холодильной машины охлаждения верха деэтанизатора использовано 270 кВт электроэнергии со стороны, а степень извлечения углеводородов С3+ составила 94,8%.When operating the installation according to the prototype under the conditions of the example, 270 kW of electricity from the outside was used to drive the refrigeration machine for cooling the top of the deethanizer, and the degree of extraction of C 3+ hydrocarbons was 94.8%.

Таким образом, предлагаемая установка позволяет повысить энергоэффективность и может найти применение а газовой промышленности.Thus, the proposed installation improves energy efficiency and can be used in the gas industry.

Claims (1)

Установка извлечения углеводородов С3+ из природного газа с помощью низкотемпературной конденсации, включающая расположенные на линии подачи природного газа первый рекуперативный: теплообменник, оснащенный компрессионной холодильной машиной, и сепаратор, оснащенный линией подачи газа сепарации со вторым рекуперативным теплообменником, соединенный с деметанизатором линией подачи остатка сепарации с редуцирующим устройством, при этом верх деметанизатора оснащен линией вывода отбензиненного газа, на которой расположены второй и первый рекуперативные теплообменники, а низ деметанизатора оснащен нагревателем, расположенным на байпасной линии первого рекуперативного теплообменника, а также соединен линией подачи деметанизированного конденсата с блоком фракционирования, оснащенным линиями вывода углеводородных фракций и соединенным линией вывода метансодержащего газа с линией вывода отбензиненного газа, отличающаяся тем, что на линии подачи газа сепарации в деметанизатор после второго рекуперативного теплообменника установлен дополнительный сепаратор, соединенный с деметанизатором линией подачи остатка сепарации с редуцирующим устройством и линией подачи газа дополнительной сепарации с детандером, соединенным посредством кинематических, и/или электрических, и/или магнитных, и/или гидравлических устройств с приводом(ами) компрессионной холодильной машины и/или иных охлаждающих устройств блока фракционирования и холодильной машиной, соединенной с первым рекуперативным теплообменником,Installation for the extraction of C 3+ hydrocarbons from natural gas using low-temperature condensation, including the first recuperative located on the natural gas supply line: a heat exchanger equipped with a compression refrigeration machine and a separator equipped with a separation gas supply line with a second recuperative heat exchanger connected to the demethanizer by a residue supply line separation device with a reducing device, while the top of the demethanizer is equipped with a strip gas outlet line, on which the second and first recuperative heat exchangers are located, and the bottom of the demethanizer is equipped with a heater located on the bypass line of the first recuperative heat exchanger, and is also connected by a demethanized condensate supply line to a fractionation unit equipped with hydrocarbon fractions output lines and connected by a methane-containing gas output line to a stripped gas output line, characterized in that on the separation gas supply line to the demethanizer after the second recuperation An additional separator is installed in the ratio heat exchanger, connected to the demethanizer by a separation residue supply line with a reducing device and an additional separation gas supply line to an expander connected by means of kinematic and/or electric and/or magnetic and/or hydraulic devices with a compression drive(s). a refrigerating machine and/or other cooling devices of the fractionation unit and a refrigerating machine connected to the first recuperative heat exchanger,
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