WO2013151220A1 - Appareil de distillation fractionnée de gaz naturel - Google Patents

Appareil de distillation fractionnée de gaz naturel Download PDF

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Publication number
WO2013151220A1
WO2013151220A1 PCT/KR2012/008137 KR2012008137W WO2013151220A1 WO 2013151220 A1 WO2013151220 A1 WO 2013151220A1 KR 2012008137 W KR2012008137 W KR 2012008137W WO 2013151220 A1 WO2013151220 A1 WO 2013151220A1
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Prior art keywords
vapor stream
gas
heat exchanger
natural gas
expander
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PCT/KR2012/008137
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English (en)
Korean (ko)
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윤호병
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삼성중공업 주식회사
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Priority to US14/390,394 priority Critical patent/US20150082828A1/en
Publication of WO2013151220A1 publication Critical patent/WO2013151220A1/fr

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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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • 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
    • C10L3/10—Working-up natural gas or synthetic 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
    • F25J3/0204—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
    • F25J3/0238—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
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/06—Heat exchange, direct or indirect
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/48—Expanders, e.g. throttles or flash tanks
    • 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
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/543—Distillation, fractionation or rectification for separating fractions, components or impurities during preparation or upgrading of a fuel
    • 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
    • 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
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • 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
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop

Definitions

  • the present invention relates to a natural gas fractional distillation apparatus, and more particularly, to a natural gas fractional distillation apparatus capable of improving energy efficiency.
  • Natural gas is generally recovered from gas wells that have been drilled into the underground reservoir. Natural gas is mostly made up of methane and contains many small amounts of components such as water, hydrogen sulfide, carbon dioxide, mercury, nitrogen, and heavier hydrocarbons such as ethane, propane and butane.
  • heavy hydrocarbons such as ethane, propane and butane, which are heavier than methane, are also valuable as commodities, condensed and recovered as natural gas liquids, and fractionated to produce valuable products.
  • Such a natural gas liquid recovery process uses a distillation column to separate methane and heavy hydrocarbons from pretreated natural gas and then liquefy methane and heavy hydrocarbons.
  • a fractional distillation apparatus for obtaining liquefied natural gas is classified into an overhead vapor stream containing methane and a component strengthening lower stream that is heavier than methane after the raw natural gas flows into the distillation column.
  • the technical problem to be solved by the present invention is to provide a natural gas fractional distillation apparatus that can improve energy efficiency by improving a part of the process to reduce the energy consumed in fractionating the natural gas as a raw material.
  • the condensed natural gas is introduced, the gas-liquid separator for separating the condensed natural gas into steam and liquid flow; A gas separator for separating the vapor stream separated from the gas-liquid separator into a first vapor stream and a second vapor stream; A first heat exchanger for condensing the first vapor stream separated from the gas separator; A first expander for expanding the first vapor stream condensed in the first heat exchanger; A second expander for expanding the second vapor stream separated from the gas separator; And the liquid stream separated by the gas-liquid separator, the first vapor stream expanded in the first expander, and the second stream expanded in the second expander are introduced, and the top vapor stream and methane containing methane.
  • a natural gas fractional distillation apparatus may be provided which mutually heat exchanges the streams.
  • the condensed natural gas is introduced, the gas-liquid separator for separating the condensed natural gas into steam and liquid flow; A gas separator for separating the vapor stream separated from the gas-liquid separator into a first vapor stream and a second vapor stream; A first heat exchanger for condensing the first vapor stream separated from the gas separator; A first expander for expanding the first vapor stream condensed in the first heat exchanger; A second expander for expanding the second vapor stream separated from the gas separator; And the liquid stream separated by the gas-liquid separator, the first vapor stream expanded in the first expander, and the second stream expanded in the second expander are introduced, and the top vapor stream and methane containing methane.
  • a natural gas fractional distillation apparatus may be provided which mutually heat exchanges the streams.
  • the first heat exchanger may further include a second heat exchanger configured to discharge the condensed natural gas by mutually exchanging the overhead vapor stream and the natural gas discharged after the heat exchange.
  • the second heat exchanger may further include a compressor for compressing the overhead vapor stream discharged after heat exchange.
  • the condensed natural gas is introduced, the gas-liquid separator for separating the condensed natural gas into a vapor flow and a liquid flow;
  • a gas separator for separating the vapor stream separated from the gas-liquid separator into a first vapor stream and a second vapor stream;
  • a first heat exchanger for condensing the first vapor stream separated from the gas separator;
  • a first expander for expanding the first vapor stream condensed in the first heat exchanger;
  • a second expander for expanding the second vapor stream separated from the gas separator;
  • the liquid stream separated by the gas-liquid separator, the first vapor stream expanded in the first expander and the second stream expanded in the second expander are introduced, and the top vapor stream including methane and methane than A distillation column for fractionating heavy component-enhanced bottoms;
  • the condensed natural gas is introduced, the gas-liquid separator for separating the condensed natural gas into a vapor flow and a liquid flow;
  • a gas separator for separating the vapor stream separated from the gas-liquid separator into a first vapor stream and a second vapor stream;
  • a first heat exchanger for condensing the first vapor stream separated from the gas separator;
  • a first expander for expanding the first vapor stream condensed in the first heat exchanger;
  • a second expander for expanding the second vapor stream separated from the gas separator;
  • the liquid stream separated by the gas-liquid separator, the first vapor stream expanded in the first expander and the second stream expanded in the second expander are introduced, and the top vapor stream including methane and methane than A distillation column for fractionating heavy component-enhanced bottoms;
  • the second heat exchanger may further include a compressor for compressing the overhead vapor stream discharged after heat exchange.
  • the condensed natural gas is introduced, the gas-liquid separator for separating the condensed natural gas into a vapor flow and a liquid flow;
  • a gas separator for separating the vapor stream separated from the gas-liquid separator into a first vapor stream and a second vapor stream;
  • a first heat exchanger for condensing the first vapor stream separated from the gas separator;
  • a first expander for expanding the first vapor stream condensed in the first heat exchanger;
  • a third heat exchanger for heating the first vapor stream expanded by the first expander;
  • a second expander for expanding the second vapor stream separated from the gas separator;
  • the top streams including methane, wherein the liquid stream separated from the gas-liquid separator, the first streams heated in the third heat exchanger, and the second streams expanded in the second expander are introduced.
  • a distillation column for fractionating a component-enhanced lower stream that is heavier than methane wherein the first heat exchanger exchanges heat between the first vapor stream separated from the gas separator and the overhead vapor stream, and the third heat exchanger includes:
  • the natural gas fractional distillation apparatus may be provided by mutually heat-exchanging the first vapors expanded by the first expander and the top vapors discharged from the first heat exchanger.
  • the third heat exchanger may further include a second heat exchanger configured to discharge the condensed natural gas by mutually heat-exchanging the tower vapor stream and natural gas discharged after heat exchange.
  • the second heat exchanger may further include a compressor for compressing the overhead vapor stream discharged after heat exchange.
  • the gas separator may separate the first vapor stream and the second vapor stream in a ratio of 2: 8 to 1: 9.
  • Embodiments of the present invention mutually heat exchange in the first heat exchanger for the first vapor stream and the overhead vapor stream discharged from the gas separator and the first vapor stream expanded in the first expander or the second vapor stream expanded in the second expander Or mutually heat-exchange the natural gas and the overhead vapor stream and the first vapor stream expanded in the first expander or the second vapor stream expanded in the second expander in the second heat exchanger, or discharge from the first heat exchanger.
  • a third heat exchanger for mutually heat-exchanging the top vapor streams and the first vapor streams discharged from the first expander, it is possible to reduce energy consumed in fractionating natural gas as a raw material to improve energy efficiency.
  • FIG. 1 is a block diagram showing a natural gas fractional distillation apparatus according to a first embodiment of the present invention.
  • Figure 2 is a block diagram showing a natural gas fractional distillation apparatus according to a second embodiment of the present invention.
  • Figure 3 is a block diagram showing a natural gas fractional distillation apparatus according to a third embodiment of the present invention.
  • Figure 4 is a block diagram showing a natural gas fractional distillation apparatus according to a fourth embodiment of the present invention.
  • FIG. 5 is a block diagram showing a natural gas fractional distillation apparatus according to a fifth embodiment of the present invention.
  • Natural gas streams to be described below are defined as all hydrocarbon compounds including methane, ethane, propane, butane, etc., from which water, hydrogen sulfide, carbon dioxide, mercury, nitrogen and the like have been removed.
  • FIG. 1 is a block diagram showing a natural gas fractional distillation apparatus 100 according to a first embodiment of the present invention.
  • the natural gas fractional distillation apparatus 100 includes a gas-liquid separator 110 in which condensed natural gas flows in, but separates the condensed natural gas into a vapor stream and a liquid stream. And a first heat exchanger for condensing the vapor stream separated from the gas-liquid separator 110 into a first vapor stream and a second vapor stream, and a first vapor stream separated from the gas separator 120.
  • a first expander 140 that expands the first vapor stream condensed in the first heat exchanger 130
  • a second expander that expands the second vapor stream separated from the gas separator 120 ( 150, the liquid stream separated from the gas-liquid separator 110, the first vapor stream expanded in the first expander 140, and the second vapor stream expanded in the second expander 150 flow in, but include methane.
  • the natural gas fractional distillation apparatus 100 uses energy of the first vapor stream cooled by depressurization in the first expander 140 as a refrigerant of the first heat exchanger 130 to be applied to the distillation column 160. And energy used in the compressor 180 for condensing and cooling the overhead vapor stream discharged from the distillation column 160.
  • the second heat exchanger 170 serves to condense the natural gas in the gaseous state which has been subjected to the pretreatment process to the condensed natural gas.
  • the natural gas condensed in the second heat exchanger 170 is discharged along the second flow path 102. At this time, the natural gas in the second heat exchanger 170 exchanges heat with the overhead vapor stream cooled through the distillation tower 160 and the first heat exchanger 130 in sequence.
  • the condensed natural gas is introduced into the gas-liquid separator 110 along the second flow path 102.
  • the gas-liquid separator 110 separates the condensed natural gas into a vapor state in a gas state and a liquid state in a liquid state.
  • the liquid flows into the lower position of the distillation column 160 along the third flow passage 113.
  • the gaseous vapor stream separated from the gas-liquid separator 110 flows into the gas separator 120 along the fourth flow path 111.
  • the gas separator 120 separates the vapor stream into the first vapor stream and the second vapor stream according to a preset ratio.
  • the first vapor stream and the second vapor stream are separated into 2: 8 to 1: 9. This is, by separating the steam flow flowing into the distillation column 160 into the first steam flow and the second steam flow in the same ratio as described above, by cooling the top steam flow discharged from the distillation column 160 by using the first steam flow.
  • energy used in the compressor 180 for condensing and cooling the overhead vapor stream In order to improve energy efficiency of the entire natural gas fractional distillation apparatus 100 by reducing energy used in the compressor 180 for condensing and cooling the overhead vapor stream.
  • the second vapor stream separated from the gas separator 120 flows into the second expander 150 along the fifth flow path 122.
  • the second expander 150 serves to expand the second vapor stream and to lower its temperature.
  • the second vapor stream expanded in the second expander 150 may change from the gas state to the liquid state as the temperature decreases, and the gas state and the liquid state may coexist.
  • the second vapor stream passing through the second expander 150 flows into the distillation column 160 along the sixth flow path 124.
  • the sixth flow path 124 may include the third flow path 113 such that the second vapor stream passing through the sixth flow path 124 flows into an upper position of the distillation column 160 than the liquid flow passing through the third flow path 113. More connected to the upper position of the distillation column 160.
  • the top column steam discharged to the upper portion of the distillation column 160 is cooled by using a second steam flow flowing into the distillation column 160 along the sixth flow path 124, This is to reduce the cooling heat input to the cooling of the steam stream.
  • the first steam flows into the first heat exchanger 130 along the seventh flow path 121, and the first steam flows discharged from the first heat exchanger 130 are formed along the eighth flow path 123. 1 is sequentially introduced into the expander 140.
  • the first vapor stream is rapidly expanded, decompressed, and the temperature thereof is drastically lowered, may be changed from a gas state to a liquid state, and a gas state and a liquid state may coexist.
  • the first vapor stream passing through the first inflator 140 maintains the lowest temperature in this embodiment.
  • the first steam flow discharged from the first expander 140 flows into the first heat exchanger 130 again along the ninth flow path 125.
  • a top steam flow discharged along the eleventh flow path 161 from the upper portion of the distillation column 160 flows into the first heat exchanger 130.
  • the first heat exchanger 130 may include the first vapor flow introduced along the seventh flow path 121, the first vapor flow introduced again along the ninth flow path 125, and the eleventh flow path 161.
  • the incoming top streams are exchanged with each other.
  • the first vapor flow introduced along the ninth flow path 125 serves as a refrigerant. Therefore, the first steam flowed in along the seventh flow path 121 is condensed and discharged, and the top steam flowed in along the eleventh flow path 161 is also condensed and discharged from the first heat exchanger 130. In addition, the first vapor flow introduced along the ninth flow path 125 is heated and discharged from the first heat exchanger 130.
  • the first heat exchanger 130 since the overhead steam flows through the first heat exchanger 130 is cooled and discharged, energy used in the compressor 180 for condensing and cooling the overhead steam flow can be reduced, and passed through the first expander 140. Afterwards, the first vapor stream passing through the first heat exchanger 130 is elevated to flow into the distillation tower 160, thereby reducing energy used in the distillation tower 160.
  • the first vapor stream passing through the first heat exchanger 130 flows into the distillation tower 160 along the tenth flow path 127, and is more than the second vapor stream passing through the sixth flow path 124. Flows into the upper position. That is, the tenth flow path 127 is connected to the upper position of the distillation column 160 than the sixth flow path 124.
  • the liquids, the first vapors, and the second vapors introduced into the distillation column 160 may be disposed adjacent to the distillation column 160 along the circulation passage installed under the distillation column 160. After heated and vaporized by, it is introduced again into the distillation column (160).
  • the distillation column 160 separates the methane-enhanced overhead vapor stream and the component-enhanced lower stream heavier than methane from the raw natural gas.
  • the overhead vapor stream is discharged from the upper portion of the distillation column 160 and cooled along the eleventh flow path 161 through the first heat exchanger 130, and discharged from the first heat exchanger 130 along the twelfth flow path 163. And flows into the second heat exchanger 170.
  • the second heat exchanger 170 serves to mutually heat-exchange the raw natural gas that has undergone the pretreatment process and the top vapors introduced along the twelfth flow path 163. As described above, the natural gas passing through the second heat exchanger 170 is condensed and discharged along the second flow path 102.
  • top vapors discharged from the second heat exchanger 170 are introduced into the compressor 180 along the thirteenth flow path 165, compressed and condensed, and then stored along the fourteenth flow path 167. ) Can be stored.
  • the component-enhanced bottoms heavier than the methane discharged from the distillation column 160 may be stored externally along the discharge passage 162 connected to the lower portion of the distillation column 160.
  • FIG. 2 is a block diagram showing a natural gas fractional distillation apparatus 100a according to a second embodiment of the present invention.
  • the natural gas fractional distillation apparatus (100a) according to the second embodiment of the present invention, the gas-liquid separator (110a) is introduced into the condensed natural gas, but separates the condensed natural gas into steam and liquid flow And a first heat exchanger for condensing the vapor stream separated from the gas-liquid separator 110a into a first vapor stream and a second vapor stream, and a first vapor stream separated from the gas separator 120a.
  • a second heat exchanger 170a for discharging the natural gas condensed by exchanging the top vapors and natural gas discharged after the exchange, and a top vapor stream discharged after the heat exchange in the second heat exchanger 170a; 180a).
  • the second heat exchanger 170a serves to condense the natural gas in the gaseous state after the pretreatment process to the condensed natural gas.
  • the natural gas condensed in the second heat exchanger 170a is discharged along the second flow path 102a.
  • the natural gas in the second heat exchanger (170a) is mutually heat exchanged with the overhead vapor stream cooled through the distillation column (160a) and the first heat exchanger (130a) in sequence.
  • the condensed natural gas flows into the gas-liquid separator 110a along the second flow path 102a.
  • the gas-liquid separator 110a serves to separate the condensed natural gas into a vapor state in a gas state and a liquid state in a liquid state.
  • the liquid flows into the lower position of the distillation column 160a along the third flow passage 113a.
  • the gaseous vapor stream separated from the gas-liquid separator 110a flows into the gas separator 120a along the fourth flow path 111a.
  • the gas separator 120a separates the vapor stream into the first vapor stream and the second vapor stream according to a preset ratio.
  • the first vapor stream and the second vapor stream are separated into 2: 8 to 1: 9. This is, by separating the steam flowing into the distillation column 160a into the first steam and the second steam at the same ratio as above, and cooling the top steam flow discharged from the distillation column 160a by using the second steam.
  • the compressor 180a In order to improve energy efficiency of the entire natural gas fractional distillation apparatus 100a by reducing energy used in the compressor 180a for condensing and cooling the overhead steam stream.
  • first steam flow separated from the gas separator 120a flows into the first heat exchanger 130a along the seventh flow path 121a, and the first steam flow discharged from the first heat exchanger 130a is made of a first steam flow.
  • the first vapor stream is rapidly expanded, decompressed, and the temperature thereof is drastically lowered, may be changed from a gas state to a liquid state, and a gas state and a liquid state may coexist.
  • the first vapor stream passing through the first expander 140a maintains the lowest temperature in this embodiment.
  • the first steam flow discharged from the first expander 140a flows into the distillation tower 160a along the ninth flow path 125a, and the second steam flows through the tenth flow path 127a. Flows into the upper position. That is, the ninth flow path 125a is connected to the upper position of the distillation column 160a than the tenth flow path 127a.
  • the second vapor stream and the ninth flow path 125a which are vaporized in the distillation column 160a and introduced into the distillation column 160a along the tenth flow path 127a, are discharged to the top of the distillation column 160a.
  • the second vapor stream and the ninth flow path 125a which are vaporized in the distillation column 160a and introduced into the distillation column 160a along the tenth flow path 127a, are discharged to the top of the distillation column 160a.
  • the second vapor stream separated from the gas separator 120a flows into the second expander 150a along the fifth flow path 122a.
  • the second expander 150a serves to expand the second vapor stream and to lower its temperature.
  • the second vapor stream expanded in the second expander 150a may change from the gas state to the liquid state as the temperature decreases, and the gas state and the liquid state may coexist.
  • the second vapor stream passing through the second expander 150a flows into the first heat exchanger 130a along the sixth flow path 124a.
  • a top steam flow discharged from the upper portion of the distillation column 160a along the eleventh flow path 161a flows into the first heat exchanger 130a.
  • the first heat exchanger 130a flows along the first steam flow flowing along the seventh flow passage 121a and the second steam flow flowing along the sixth flow passage 124a and the eleventh flow passage 161a.
  • the top vapor streams are heat exchanged.
  • the second vapor flow introduced along the sixth flow path 124a serves as a refrigerant. Therefore, the first steam flowed in along the seventh flow path 121a is condensed and discharged, and the top steam flowed in along the eleventh flow path 161a is also condensed and discharged from the first heat exchanger 130a. In addition, the second vapor stream introduced along the sixth flow path 124a is heated by the first heat exchanger 130a and discharged.
  • the overhead steam flows through the first heat exchanger 130a is cooled and discharged, energy used in the compressor 180a for condensing and cooling the overhead steam flow can be reduced, and passed through the second expander 150a. Afterwards, the second vapor stream passing through the first heat exchanger 130a is elevated to flow into the distillation tower 160a, thereby reducing energy used in the distillation tower 160a.
  • the second vapor stream passing through the first heat exchanger 130a flows into the distillation tower 160a along the tenth flow path 127a, and is compared with the first vapor stream passing through the ninth flow path 125a in the distillation tower 160a. Flows into the lower position. That is, the tenth flow path 127a is connected to a lower position of the distillation column 160a than the ninth flow path 125a.
  • the second vapor stream and the ninth flow path 125a which are vaporized in the distillation column 160a and introduced into the distillation column 160a along the tenth flow path 127a, are discharged to the top of the distillation column 160a.
  • the second vapor stream and the ninth flow path 125a which are vaporized in the distillation column 160a and introduced into the distillation column 160a along the tenth flow path 127a, are discharged to the top of the distillation column 160a.
  • the liquids, the first vapors, and the second vapors introduced into the distillation column 160a are disposed adjacent to the distillation column 160a along the circulation passage installed under the distillation column 160a. After heating and vaporizing by the flow, the distillation column 160a is introduced again.
  • the distillation column 160a serves to separate the methane-enhanced overhead stream and the component-enhanced lower stream that is heavier than methane from the raw natural gas.
  • the overhead vapor stream is discharged from the upper portion of the distillation column 160a and cooled along the eleventh flow path 161a through the first heat exchanger 130a and discharged from the first heat exchanger 130a along the twelfth flow path 163a. And flows into the second heat exchanger 170a.
  • the second heat exchanger 170a serves to mutually heat-exchange the raw natural gas that has undergone the pretreatment process and the top vapors introduced along the twelfth flow path 163a. As described above, the natural gas passing through the second heat exchanger 170a is condensed and discharged along the second flow path 102a.
  • the storage vessel (not shown) is provided along the fourteenth flow path 167a. ) Can be stored.
  • the component-enhanced lower stream that is heavier than the methane discharged from the distillation column 160a may be stored externally along the discharge passage 162a connected to the lower portion of the distillation column 160a.
  • FIG. 3 is a block diagram showing a natural gas fractional distillation apparatus 100b according to a third embodiment of the present invention.
  • the natural gas fractional distillation apparatus (100b) according to the third embodiment of the present invention, the gas-liquid separator (110b) is introduced into the condensed natural gas, but separates the condensed natural gas into steam and liquid flow And a first heat exchanger for condensing the vapor stream separated from the gas-liquid separator 110b into a first vapor stream and a second vapor stream, and a first vapor stream separated from the gas separator 120b.
  • the second heat exchanger 170b serves to condense the natural gas in the gaseous state after the pretreatment process to the condensed natural gas.
  • the second heat exchanger 170b receives the tower vapor stream cooled sequentially through the natural gas, the distillation column 160b, and the first heat exchanger 130b, and the first vapor stream reduced in pressure and cooled through the first expander 140b. Heat exchange with each other.
  • the natural gas condensed in the second heat exchanger 170b is discharged along the second flow path 102b.
  • the condensed natural gas flows into the gas-liquid separator 110b along the second flow path 102b.
  • the gas-liquid separator 110b serves to separate the condensed natural gas into a gaseous vapor stream and a liquid stream liquid.
  • the liquid flows into the lower position of the distillation column 160b along the third flow passage 113b.
  • the gaseous vapor stream separated from the gas-liquid separator 110b flows into the gas separator 120b along the fourth flow path 111b.
  • the gas separator 120b separates the vapor stream into the first vapor stream and the second vapor stream according to a preset ratio.
  • the first vapor stream and the second vapor stream are separated into 2: 8 to 1: 9. This is by separating the steam flowing into the distillation column 160b into the first steam and the second steam in the same ratio as described above, and cooling the top steam flow discharged from the distillation column 160b by using the first steam.
  • the compressor 180b In order to improve energy efficiency of the entire natural gas fractional distillation apparatus 100b by reducing energy used in the compressor 180b for condensing and cooling the overhead vapor stream.
  • the second vapor stream separated from the gas separator 120b flows into the second expander 150b along the fifth flow path 122b.
  • the second expander 150b serves to expand the second vapor stream and to lower its temperature.
  • the second vapor stream expanded in the second expander 150b may change from the gas state to the liquid state as the temperature decreases, and the gas state and the liquid state may coexist.
  • the second vapor stream passing through the second expander 150b flows into the distillation column 160b along the sixth flow path 124b.
  • the sixth flow path 124b is connected to the third flow path 113b such that the second vapor flow through the sixth flow path 124b flows into the upper position of the distillation column 160b than the liquid flow through the third flow path 113b. More connected to the upper position of the distillation column 160b.
  • the first steam flows into the first heat exchanger 130b along the seventh flow path 121b and the first steam flows discharged from the first heat exchanger 130b follows the eighth flow path 123b. 1 is sequentially introduced into the expander 140b.
  • the first vapor stream is rapidly expanded, decompressed, and the temperature thereof is drastically lowered, may be changed from a gas state to a liquid state, and a gas state and a liquid state may coexist.
  • the first vapor stream passing through the first inflator 140b maintains the lowest temperature in this embodiment.
  • the first vapor flow discharged from the first expander 140b flows into the second heat exchanger 170b along the ninth flow path 125b.
  • the first vapor stream passing through the second heat exchanger 170b flows into the distillation tower 160b along the tenth flow path 127b, and is located at an upper position of the distillation tower 160b than the second vapor stream passing through the sixth flow path 124b. Flows into. That is, the tenth flow path 127b is connected to the upper position of the distillation column 160b than the sixth flow path 124b.
  • the second vapor stream and the tenth flow path 127b which are vaporized in the distillation column 160b and introduced into the distillation column 160b along the sixth flow path 124b, are discharged to the top of the distillation column 160b.
  • the second vapor stream and the tenth flow path 127b which are vaporized in the distillation column 160b and introduced into the distillation column 160b along the sixth flow path 124b, are discharged to the top of the distillation column 160b.
  • the liquids, the first vapors, and the second vapors introduced into the distillation column 160b are installed in the vicinity of the distillation column 160b along the circulation passage installed under the distillation column 160b. After heating and vaporizing by, it is introduced again into the distillation column (160b).
  • the distillation column 160b serves to discriminate the methane-enhanced overhead stream and the component-enhanced lower stream that is heavier than methane from the raw natural gas.
  • the overhead vapor stream is discharged from the upper portion of the distillation column 160b and cooled along the eleventh flow path 161b through the first heat exchanger 130b and discharged from the first heat exchanger 130b along the twelfth flow path 163b. And flows into the second heat exchanger 170b.
  • the second heat exchanger 170b mutually heat-exchanges the raw natural gas that has undergone the pretreatment process and the top steam flowed along the twelfth flow path 163b and the first steam flowed along the ninth flow path 125b. do. As described above, the natural gas passed through the second heat exchanger 170b is condensed and discharged along the second flow path 102b.
  • the first steam flowed in from the second heat exchanger 170b along the ninth flow path 125b serves as a refrigerant. Therefore, the natural gas introduced along the first flow path 101b is condensed and discharged, and the top steam flowed along the twelfth flow path 163b is also condensed and discharged from the second heat exchanger 170b. In addition, the first vapor flow introduced along the ninth flow path 125b is heated and discharged by the second heat exchanger 170b.
  • the overhead steam flows through the second heat exchanger 170b is cooled and discharged, energy used in the compressor 180b for condensing and cooling the overhead steam flow can be reduced, and passes through the first expander 140b. Afterwards, the first vapor stream passing through the second heat exchanger 170b is heated up and introduced into the distillation tower 160b, thereby reducing energy used in the distillation tower 160b.
  • the top vapors discharged from the second heat exchanger 170b are introduced into the compressor 180b along the thirteenth flow path 165b, compressed and condensed, and then stored along the fourteenth flow path 167b. ) Can be stored.
  • the component-enhanced bottom stream that is heavier than the methane discharged from the distillation column 160b may be stored externally along the discharge passage 162b connected to the lower portion of the distillation column 160b.
  • FIG. 4 is a block diagram showing a natural gas fractional distillation apparatus 100c according to a fourth embodiment of the present invention.
  • the natural gas fractional distillation apparatus (100c) according to the fourth embodiment of the present invention, the gas-liquid separator (110c) is introduced into the condensed natural gas, but separates the condensed natural gas into steam and liquid flow And a first heat exchanger for condensing the vapor stream separated from the gas-liquid separator 110c into a first vapor stream and a second vapor stream, and a first vapor stream separated from the gas separator 120c.
  • Group 130c a first expander 140c for expanding the first vapor stream condensed in the first heat exchanger 130c, and a second expander for expanding the second vapor stream separated from the gas separator 120c ( 150c), the liquid stream separated from the gas-liquid separator 110c, the first vapor stream expanded in the first expander 140c, and the second vapor stream expanded in the second expander 150c flow in, but include methane.
  • the distillation column 160c which fractionates the vapor stream and the component-enhanced lower stream heavier than methane, and the first heat exchanger 130c, respectively, Heat exchange with the steam flow and the top steam flow discharged from the first heat exchanger (130c), the second steam flows and the natural gas expanded in the second expander (150c) and the second gas to discharge the condensed natural gas A heat exchanger (170c) and a compressor (180c) for compressing the overhead vapor stream discharged after the heat exchange in the second heat exchanger (170c).
  • the natural gas After the natural gas passes through the pretreatment process, the natural gas flows into the second heat exchanger 170c along the first flow path 101c.
  • the second heat exchanger 170c serves to condense the natural gas in the gaseous state after the pretreatment process to the condensed natural gas.
  • the second heat exchanger (170c) is a top gas stream and the second steam flow is cooled and decompressed through the second expander (150c) and the second column expander (150c) cooled in sequence through the natural gas, distillation column (160c) and the first heat exchanger (130c) Heat exchange with each other.
  • the natural gas condensed in the second heat exchanger 170c is discharged along the second flow path 102c.
  • the condensed natural gas flows into the gas-liquid separator 110c along the second flow path 102c.
  • the gas-liquid separator 110c serves to separate the condensed natural gas into a vapor state in a gas state and a liquid state in a liquid state.
  • the liquid flows into the lower position of the distillation column 160c along the third flow passage 113c.
  • the gaseous vapor stream separated from the gas-liquid separator 110c flows into the gas separator 120c along the fourth flow path 111c.
  • the gas separator 120c separates the vapor stream into the first vapor stream and the second vapor stream according to a preset ratio.
  • the first vapor stream and the second vapor stream are separated into 2: 8 to 1: 9. This is, by separating the steam flow flowing into the distillation column 160c into the first steam flow and the second steam flow in the same ratio as above, and cooling the top steam flow discharged from the distillation column 160c by using the second steam flow.
  • the compressor 180c In order to improve energy efficiency of the entire natural gas fractional distillation apparatus 100c by reducing energy used in the compressor 180c for condensing and cooling the overhead vapor stream.
  • the first vapor stream separated from the gas separator 120c flows into the first heat exchanger 130c along the seventh flow path 121c, and the first vapor stream discharged from the first heat exchanger 130c is made of It flows into the 1st inflator 140c sequentially along the 8 flow path 123c.
  • the first vapor stream is rapidly expanded, decompressed, and the temperature thereof is drastically lowered, may be changed from a gas state to a liquid state, and a gas state and a liquid state may coexist.
  • the first vapor stream passing through the first inflator 140c maintains the lowest temperature in this embodiment.
  • the first steam flow discharged from the first expander 140c flows into the distillation tower 160c along the ninth flow path 125c, and the second steam flows through the tenth flow path 126c rather than the second steam flow through the tenth flow path 126c.
  • the ninth flow path 125c is connected to an upper position of the distillation column 160c than the tenth flow path 126c.
  • the second vapor stream and the ninth flow path 125c which are vaporized in the distillation column 160c and introduced into the distillation column 160c along the tenth flow path 126c, are discharged to the top of the distillation tower 160c.
  • the cooling heat introduced into the cooling step by using the first steam flows into the distillation column (160c) in order to cool.
  • the second vapor stream separated from the gas separator 120c flows into the second expander 150c along the fifth flow path 122c.
  • the second expander 150c serves to expand the second vapor stream and to lower its temperature.
  • the second vapor stream expanded in the second expander 150c may change from a gas state to a liquid state as its temperature decreases, and also a gas state and a liquid state may coexist.
  • the second vapor stream passing through the second expander 150c flows into the second heat exchanger 170c along the sixth flow path 124c.
  • the second vapor stream passing through the second heat exchanger 170c flows into the distillation tower 160c along the tenth flow path 126c, rather than the first vapor stream passing through the ninth flow path 125c. Flows into the lower position. That is, the tenth flow path 126c is connected to a lower position of the distillation column 160c than the ninth flow path 125c.
  • the second vapor stream and the ninth flow path 125c which are vaporized in the distillation column 160c and introduced into the distillation column 160c along the tenth flow path 126c, are discharged to the top of the distillation tower 160c.
  • the cooling heat introduced into the cooling step by using the first steam flows into the distillation column (160c) in order to cool.
  • the liquids, the first vapors, and the second vapors introduced into the distillation column 160c are disposed adjacent to the distillation column 160c along the circulation passage installed under the distillation column 160c. After heating and vaporizing by, it is introduced again into the distillation column (160c).
  • the distillation column 160c serves to discriminate the methane-enhanced overhead stream and the component-enhanced lower stream that is heavier than methane from the raw natural gas.
  • the overhead vapor stream is discharged from the upper portion of the distillation column 160c and cooled along the eleventh flow path 161c through the first heat exchanger 130c and discharged from the first heat exchanger 130c along the twelfth flow path 163c. And flows into the second heat exchanger 170c.
  • the second heat exchanger 170c mutually heat-exchanges the raw natural gas, which has undergone pretreatment, with the top vapors introduced along the twelfth flow path 163c and the second vapors introduced along the sixth flow path 124c. do. As described above, the natural gas that has passed through the second heat exchanger 170c is condensed and discharged along the second flow path 102c.
  • the second steam flowed in from the second heat exchanger 170c along the sixth flow path 124c serves as a refrigerant. Accordingly, the natural gas introduced along the first flow path 101c is condensed and discharged, and the top vapor flows introduced along the twelfth flow path 163c are also condensed and discharged from the second heat exchanger 170c. In addition, the second vapor stream introduced along the sixth flow path 124c is heated and discharged by the second heat exchanger 170c.
  • the second heat exchanger 170c since the overhead steam flows through the second heat exchanger 170c is cooled and discharged, energy used in the compressor 180c for condensing and cooling the overhead steam flow can be reduced, and passed through the second expander 150c. Afterwards, the second vapor stream passing through the second heat exchanger 170c is heated up and introduced into the distillation tower 160c, thereby reducing energy used in the distillation tower 160c.
  • the top vapors discharged from the second heat exchanger 170c are introduced into the compressor 180c along the thirteenth flow path 165c, compressed and condensed, and then stored along the fourteenth flow path 167c. ) Can be stored.
  • the component-enhanced bottoms heavier than the methane discharged from the distillation column 160c may be stored externally along the discharge passage 162c connected to the lower portion of the distillation column 160c.
  • FIG. 5 is a block diagram showing a natural gas fractional distillation apparatus (100d) according to a fifth embodiment of the present invention.
  • the natural gas fractional distillation apparatus (100d) according to the fifth embodiment of the present invention, a gas-liquid separator (110d) for introducing the condensed natural gas flow into the condensed natural gas into steam and liquid flow And a first heat exchanger for condensing the vapor stream separated from the gas-liquid separator 110d into a first vapor stream and a second vapor stream, and a first vapor stream separated from the gas separator 120d.
  • the first vapor stream and the second vapor stream expanded in the second expander (150d) is introduced, but the top vapor stream containing methane and heavier than methane
  • a compressor 180d for compressing the overhead vapor stream discharged after the heat exchange in the second heat exchanger 170d.
  • the natural gas fractional distillation apparatus 100d includes a third heat exchanger configured to mutually heat-exchange the top vapors discharged from the first heat exchanger 130d and the first vapors discharged from the first expander 140d ( By additionally installing 190d, it is possible to reduce the energy used in the compressor 180d for condensing and cooling the energy applied to the distillation column 160d and the overhead vapor stream discharged from the distillation column 160d.
  • the second heat exchanger 170d serves to condense the natural gas in the gaseous state after the pretreatment process to the condensed natural gas.
  • the natural gas condensed in the second heat exchanger 170d is discharged along the second flow path 102d.
  • the natural gas in the second heat exchanger (170d) is mutually heat exchanged with the overhead vapor stream cooled through the distillation column (160d), the first heat exchanger (130d) and the third heat exchanger (190d) in sequence.
  • the condensed natural gas flows into the gas-liquid separator 110d along the second flow path 102d.
  • the gas-liquid separator 110d separates the condensed natural gas into a gaseous vapor stream and a liquid liquid stream.
  • the liquid flows into the lower position of the distillation column 160d along the third flow passage 113d.
  • the gaseous vapor stream separated from the gas-liquid separator 110d flows into the gas separator 120d along the fourth flow path 111d.
  • the gas separator 120d separates the vapor stream into the first vapor stream and the second vapor stream according to a preset ratio.
  • the first vapor stream and the second vapor stream are separated into 2: 8 to 1: 9. This is by separating the steam flowing into the distillation column 160d into the first steam and the second steam in the same ratio as described above, and cooling the top steam flow discharged from the distillation column 160d by using the first steam.
  • the compressor 180d In order to improve energy efficiency of the entire natural gas fractional distillation apparatus 100d by reducing energy used in the compressor 180d for condensing and cooling the overhead vapor stream.
  • the second vapor stream separated from the gas separator 120d flows into the second expander 150d along the fifth flow path 122d.
  • the second expander 150d serves to expand the second vapor stream and lower its temperature.
  • the second vapor stream expanded in the second expander 150d may change from a gaseous state to a liquid state as its temperature decreases, and a gaseous state and a liquid state may coexist.
  • the second vapor stream passing through the second expander 150d flows into the distillation column 160d along the sixth flow path 124d.
  • the sixth flow path 124d is connected to the third flow path 113d such that the second vapor stream passing through the sixth flow path 124d flows into the upper position of the distillation column 160d than the liquid flow passing through the third flow path 113d. It is more connected to the upper position of the distillation column 160d.
  • the first steam flows into the first heat exchanger 130d along the seventh flow path 121d and the first steam flows discharged from the first heat exchanger 130d passes through the eighth flow path 123d. 1 is sequentially introduced into the expander 140d.
  • the first vapor stream is rapidly expanded, decompressed, and the temperature thereof is drastically lowered, may be changed from a gas state to a liquid state, and a gas state and a liquid state may coexist.
  • the first vapor stream passing through the first inflator 140d maintains the lowest temperature in this embodiment.
  • first steam flow discharged from the first expander 140d flows into the third heat exchanger 190d along the ninth flow path 125d.
  • a top steam flow discharged along the eleventh flow path 161d and the twelfth flow path 163d flows into the third heat exchanger 190d from the top of the distillation column 160d.
  • the first heat exchanger 130d exchanges heat between the first steam flowing in along the seventh flow passage 121d and the top steam flowing in along the eleventh flow passage 161d.
  • the first steam flowed from the first heat exchanger 130d along the seventh flow passage 121d serves as a refrigerant. Therefore, the first steam flowed in along the seventh flow path 121d is heated and discharged, and the top steam flowed in along the eleventh flow path 161d is condensed and discharged.
  • the first vapor stream passing through the first heat exchanger 130d flows into the first expander 140d along the eighth flow path 123d.
  • the first vapor stream is rapidly expanded, decompressed, and the temperature thereof is drastically lowered, may be changed from a gas state to a liquid state, and a gas state and a liquid state may coexist.
  • the first vapor stream passing through the first inflator 140d maintains the lowest temperature in this embodiment.
  • the first steam flow discharged from the first expander 140d flows into the third heat exchanger 190d along the ninth flow path 125d.
  • the top steam flow discharged to the first heat exchanger 130d is introduced into the third heat exchanger 190d along the twelfth flow path 163d.
  • the third heat exchanger 190d exchanges heat between the first steam flowing in along the ninth flow path 125d and the top steam flowing in along the twelfth flow path 163d.
  • the first steam flowed along the ninth flow path 125d serves as a refrigerant. Therefore, the top steam flowed in along the twelfth flow path 163d is condensed and discharged, and the first steam flowed in through the ninth flow path 125d is heated by the third heat exchanger 190d and discharged.
  • the overhead steam flows through the third heat exchanger 190d is cooled and discharged, energy used in the compressor 180d for condensing and cooling the overhead steam flow can be reduced, and passed through the first expander 140d. Afterwards, the first vapor stream passing through the third heat exchanger 190d is heated up and introduced into the distillation tower 160d, thereby reducing energy used in the distillation tower 160d.
  • the first vapor stream passing through the third heat exchanger 190d flows into the distillation tower 160d along the tenth flow path 127d, and the second vapor stream passing through the sixth flow path 124d is larger than that of the distillation tower 160d. Flows into the upper position. That is, the tenth flow path 127d is connected to the upper position of the distillation column 160d than the sixth flow path 124d.
  • the second vapor stream and the tenth flow path 127d which are vaporized in the distillation column 160d and introduced into the distillation column 160d along the sixth flow path 124d, are discharged to the top of the distillation column 160d.
  • the first steam flows into the distillation column (160d) along.
  • the liquids, the first vapors, and the second vapors introduced into the distillation column 160d are reboilers 164d installed adjacent to the distillation column 160d along the circulation flow path installed under the distillation column 160d. After heating and vaporizing by the flow, the distillation column 160d is introduced again.
  • the distillation column 160d serves to discriminate the methane-enhanced overhead vapor stream and the component-enhanced lower stream heavier than methane from the raw natural gas.
  • the overhead vapor stream is discharged from the upper part of the distillation column 160d and cooled along the eleventh flow path 161d via the first heat exchanger 130d and further along the twelfth flow path 163d to the third heat exchanger 190d. After cooling, the liquid is introduced into the second heat exchanger 170d along the fifteenth flow path 165d.
  • the second heat exchanger 170d serves to mutually heat-exchange the raw natural gas that has undergone the pretreatment process and the top vapors introduced along the fifteenth flow path 165d. As described above, the natural gas that has passed through the second heat exchanger 170d is condensed and discharged along the second flow path 102d.
  • the top vapors discharged from the second heat exchanger 170d are introduced into the compressor 180d along the thirteenth flow path 167d, compressed and condensed, and then stored along the fourteenth flow path 169d. ) Can be stored.
  • the component-enhanced bottoms heavier than the methane discharged from the distillation column 160d may be stored externally along the discharge passage 162d connected to the lower portion of the distillation column 160d.
  • the present invention can reduce the energy consumed in fractionating the natural gas as a raw material can improve the energy efficiency.

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Abstract

L'invention concerne un appareil de distillation fractionnée de gaz naturel. L'appareil de distillation fractionnée de gaz naturel selon une forme de réalisation de la présente invention comprend : un séparateur gaz-liquide dans lequel le gaz naturel condensé s'écoule et qui sépare le gaz naturel condensé en un courant de vapeur et un courant liquide ; un séparateur de gaz qui sépare le courant de vapeur séparé dans le séparateur gaz-liquide en un premier courant de vapeur et un second courant de vapeur ; un premier échangeur de chaleur qui condense le premier courant de vapeur séparé dans le séparateur de gaz ; un premier dispositif d'expansion qui dilate le premier courant de vapeur condensé dans le premier échangeur de chaleur ; un second dispositif d'expansion qui dilate le second courant de vapeur séparé dans le séparateur de gaz ; et une tour de distillation dans laquelle le courant de liquide séparé dans le séparateur gaz-liquide, le premier courant de vapeur dilaté dans le premier dispositif d'expansion, et le second courant de vapeur dilaté dans le second dispositif d'expansion s'écoulent pour être divisés en un courant de vapeur de tête contenant du méthane et un courant inférieur renforcé en composant qui est plus lourd que le méthane. Le premier échangeur de chaleur est capable d'échanger de la chaleur entre le premier courant de vapeur séparé dans le séparateur de gaz et le premier courant de vapeur et le courant de vapeur de tête dilaté dans le premier dispositif d'expansion.
PCT/KR2012/008137 2012-04-03 2012-10-08 Appareil de distillation fractionnée de gaz naturel WO2013151220A1 (fr)

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