WO2020021633A1 - Dispositif de traitement de gaz naturel et procédé de traitement de gaz naturel - Google Patents

Dispositif de traitement de gaz naturel et procédé de traitement de gaz naturel Download PDF

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Publication number
WO2020021633A1
WO2020021633A1 PCT/JP2018/027710 JP2018027710W WO2020021633A1 WO 2020021633 A1 WO2020021633 A1 WO 2020021633A1 JP 2018027710 W JP2018027710 W JP 2018027710W WO 2020021633 A1 WO2020021633 A1 WO 2020021633A1
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Prior art keywords
natural gas
condensate
methane
gas
supply line
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PCT/JP2018/027710
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English (en)
Japanese (ja)
Inventor
徹 中山
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日揮グローバル株式会社
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Application filed by 日揮グローバル株式会社 filed Critical 日揮グローバル株式会社
Priority to KR1020207016933A priority Critical patent/KR102642311B1/ko
Priority to CN201880077980.1A priority patent/CN111433329A/zh
Priority to PCT/JP2018/027710 priority patent/WO2020021633A1/fr
Publication of WO2020021633A1 publication Critical patent/WO2020021633A1/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
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • 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
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/68—Separating water or hydrates
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/20—Integration in an installation for liquefying or solidifying a fluid stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements

Definitions

  • the present invention relates to a natural gas processing apparatus for processing natural gas.
  • Natural gas processing equipment for processing natural gas which is a hydrocarbon gas produced from a wellhead, includes a pretreatment facility that performs pretreatment to remove various impurities from natural gas before liquefaction, and a pretreatment And a liquefaction facility for liquefying natural gas to obtain LNG (Liquidized Natural Gas).
  • a pretreatment facility moisture and carbon dioxide are removed to prevent clogging of the natural gas cooled to -150 ° C or less in the liquefaction facility, and impurities such as hydrogen sulfide are removed. Done.
  • Patent Literature 1 discloses that when liquefied natural gas (LNG) is produced from natural gas or CSG (coal seam gas), natural gas before liquefaction is brought into contact with MDEA (N-methyldiethanolamine).
  • LNG liquefied natural gas
  • MDEA N-methyldiethanolamine
  • An absorption facility that absorbs and removes hydrogen sulfide and carbon dioxide, and a natural gas that flows through a dehydration plant (adsorption tower) equipped with a molecular sieve (adsorbent) container to adsorb and remove moisture.
  • the facilities are listed.
  • the gas output from development to depletion gradually increases after the start of natural gas output, and shifts to a period (plateau period) in which the output is stable at a high output. Then, following the plateau period, a decline period in which the output gradually decreases, and the production of natural gas ends soon.
  • the supply amount of the natural gas supplied to each facility changes with the change in the production amount of the natural gas.
  • the pretreatment equipment for removing impurities including the above-mentioned absorption equipment and adsorption equipment is generally designed to increase the processing efficiency when processing the supply amount of natural gas during the plateau period. For this reason, there has been a problem that the processing efficiency deteriorates in the decline period in which the output gradually decreases.
  • the present invention has been made under such a background, and provides a technique for stably removing impurities contained in natural gas even when the supply amount of natural gas is reduced. Is to do.
  • the natural gas processing apparatus of the present invention includes an adsorption facility for adsorbing and removing impurities contained in natural gas using an adsorbent, and an absorption facility for bringing natural gas into contact with an absorbent to remove impurities contained in natural gas.
  • an impurity removal equipment group that removes impurities contained in natural gas supplied via the supply line
  • a natural gas treated in the impurity removal equipment group is separated by distillation into methane and heavy hydrocarbons having 2 or more carbon atoms, and a distillation equipment for sending the methane through an air supply line,
  • a recycle gas line for dividing a part of the supplied methane and merging with natural gas supplied from the supply line to the impurity removal equipment group.
  • the natural gas processing device may have the following features.
  • a liquefaction facility for liquefying methane sent from the distillation facility is provided.
  • the air supply line includes a compressor that pressurizes the methane, and the recycle gas line is provided at a position where a part of the methane is diverted from an outlet side of the compressor. thing.
  • C After separating the condensate which is a liquid component contained in the natural gas before being supplied to the impurity removing equipment group, the natural gas after the condensate separation is supplied to the impurity removing equipment group via the supply line.
  • the condensate is supplied via a condensate supply line, a vapor pressure adjusting device for adjusting the vapor pressure of the condensate by distilling and separating light hydrocarbons contained in the condensate, A condensate recycle line that separates a part of the condensate after the light hydrocarbons are separated by the vapor pressure adjusting equipment, and merges with the condensate supplied to the steam pressure adjusting node equipment from the condensate supply line. .
  • the condensate recycle line is detachably provided between a condensate extraction line for extracting condensate from the vapor pressure adjusting node equipment and the condensate supply line.
  • the impurity removal equipment group and the distillation equipment are provided on a floating body floating on the sea.
  • a liquefaction facility for liquefying methane sent from the distillation facility is provided on the floating body.
  • a plurality of pretreatment facilities when processing natural gas, prior to liquefaction of natural gas, a plurality of pretreatment facilities perform impurity removal treatment, and then separate into methane and heavy hydrocarbons. It is recycled at the entrance of the removal process. Therefore, even when the processing amount of natural gas decreases, the processing amount of natural gas in each pretreatment facility can be maintained, and efficient and stable processing can be performed.
  • the natural gas processing apparatus of this example is configured as a natural gas liquefaction apparatus that separates and liquefies methane contained in natural gas (also indicated as NG in each figure).
  • NG processed by the natural gas liquefaction apparatus of this example contains at least hydrogen sulfide or carbon dioxide, and further contains moisture, mercury, and oxygen.
  • the natural gas from which the liquid has been separated is first subjected to removal of carbon dioxide, hydrogen sulfide, and the like (these may be collectively referred to as “acid gas”) in an acid gas removal step 22.
  • the equipment in the acid gas removal step 22 is constituted by, for example, an absorption equipment provided with an absorption tower for bringing an absorption liquid that absorbs an acid gas into contact with natural gas in a countercurrent direction, and an acid that may be solidified in LNG during liquefaction. Gases such as carbon dioxide and hydrogen sulfide are absorbed and removed from natural gas into the absorbing solution.
  • the natural gas treated in the acid gas removing step 22 is further removed in a water removing step 23. Further, in the natural gas treated in the water removing step 23, mercury is removed in the mercury removing step 24.
  • the equipment for performing the water removal step 23 and the mercury removal step 24 includes, for example, an adsorption tower which is an adsorption apparatus filled with an adsorbent for adsorbing moisture and a mercury adsorbent for adsorbing mercury, respectively. These adsorption towers allow natural gas to pass through the adsorption tower, thereby allowing natural gas to pass through gaps between the adsorbents filled in the adsorption tower, thereby bringing the natural gas into contact with the adsorbent.
  • This mercury removal step 24 can be placed before the acid gas removal step 22.
  • the equipment group including the pretreatment equipment for performing the acid gas removal step 22, the water removal step 23, and the mercury removal step 24 is referred to as an impurity removal equipment group 20.
  • the natural gas from which the impurities have been removed is separated into methane and heavy hydrocarbons having 2 or more carbon atoms in a hydrocarbon separation step 25.
  • a hydrocarbon separation step for example, a distillation facility (demethanizer) is used.
  • the detailed description of the hydrocarbon separation equipment including the demethanizer will be described later.
  • the methane separated in the hydrocarbon separation step 25 is liquefied in the liquefaction step 26 to become liquefied natural gas (LNG).
  • the LNG is then vaporized (end-flashed) by partially vaporizing (end-flashing) the LNG, thereby performing an end-flash gas step 27 for adjusting the temperature of the LNG, a step 28 for storing the LNG, and the like, and is shipped to an LNG tanker, for example.
  • a part of the liquid component (condensate) gas-liquid separated from the natural gas in the gas-liquid separation step 21 is stored as a condensate 32 and shipped after a vapor pressure adjustment step 31 for removing light hydrocarbons is performed. You. Furthermore, the antifreeze containing water is phase-separated from the gas-liquid separated condensate, and the antifreeze regeneration process 30 is performed on the antifreeze. Monoethylene glycol (MEG) or the like is used as the antifreeze, and the regenerated antifreeze is supplied to the natural gas well. Further, the end flash gas and the boil-off gas (BOG) evaporated from the LNG in the LNG storage step 28 are subjected to a pressure increasing process 29 and are mainly used as combustion gas. It can be liquefied again by returning to the previous stage.
  • MEG Monoethylene glycol
  • BOG boil-off gas
  • the methane separated in the hydrocarbon separation step 25 is returned to the supply line 100 that supplies the natural gas to the acid gas removal step 22, and is converted into the natural gas supplied from the gas-liquid separation step 21 side.
  • a recycle gas line 10 for merging is provided. The recycle gas line 10 will be described together with the description of the equipment for performing the hydrocarbon separation step 25.
  • FIG. 2 is a configuration example of a hydrocarbon separation facility constituting a natural gas processing apparatus.
  • the hydrocarbon separation equipment includes a natural gas supply line 101 to which the natural gas processed in the mercury removal step 24 is supplied, cold boxes 11 and 12 for cooling the natural gas supplied from the natural gas supply line 101, A feed separator 13 that performs gas-liquid separation of natural gas that has been cooled and partially liquefied in boxes 11 and 12, and a natural gas is distilled to separate methane and heavy hydrocarbons having 2 or more carbon atoms.
  • a demethanizer 17 A demethanizer 17.
  • Natural gas supplied from the natural gas supply line 101 is cooled by the cold boxes 11 and 12 and is separated into gas and liquid by the feed separator 13. Then, a part of the gas component is decompressed and expanded by the expander 14 and supplied to the demethanizer 17 as a gas-liquid mixture at ⁇ 50 to ⁇ 80 ° C.
  • Reference numeral 15 in FIG. 2 denotes a JT (Joule-Thomson) valve 15. Further, the remaining gas component of the natural gas separated into gas and liquid by the feed separator 13 is cooled in the cold box 16 and then decompressed and expanded by the decompression valve 104 to obtain a gas-liquid mixture at -70 to -100 ° C. Is supplied to the demethanizer 17.
  • the liquid component gas-liquid separated by the feed separator 13 is used as a refrigerant for the cold box 12 and then supplied to the demethanizer 17.
  • the demethanizer 17 separates methane by distilling the supplied gas-liquid mixture of natural gas, and discharges the methane through an air supply line 105 provided at the top of the tower. Also, heavy hydrocarbons (C2 +), which are heavier than ethane, are allowed to flow out of the bottom of the tower. Note that reference numeral 171 in FIG. 2 indicates a reboiler. Further, the hydrocarbon separation equipment according to the present embodiment uses methane discharged from the demethanizer 17 and liquid components of natural gas separated by the feed separator 13 as refrigerant for the cold boxes 11 and 12. That is, the demethanizer 17 according to the present embodiment is configured as a distillation apparatus of a self-refrigerant type.
  • the methane flowing out of the demethanizer 17 is used as a refrigerant for the cold box 11, is pressurized by the compressor 311 and the booster compressor 312, is further cooled by the air cooler 320, and is sent to equipment for performing the liquefaction step 26. .
  • One end of the recycle gas line 10 is connected to a downstream side of the compressor 311 in the air supply line 105.
  • the other end of the recycle gas line 10 is connected to a supply line 100 on the inlet side of the impurity removing equipment group 20, in this example, on the inlet side of the acid gas removing step 22, as shown in FIG.
  • the recycle gas line 10 may be provided with a pressure control valve V10.
  • the amount of natural gas produced varies depending on the time elapsed since the development of the well.
  • the facilities in the natural gas processing apparatus for example, in the liquefaction facility for performing the liquefaction step 26 and the subsequent steps 27 and 28, even if the supply amount of the natural gas changes, the processing efficiency is hardly affected. .
  • the energy required to liquefy methane gas per unit weight and end-flash or store LNG does not change significantly.
  • the acid gas removal step 22 uses an absorption tower, and the moisture removal step 23 and the mercury removal step 24 use an adsorption tower.
  • the amount of supplied natural gas is less than the design flow rate
  • the amount of absorbing liquid also decreases in accordance with the amount of natural gas, so that both the steam load and the liquid load make the appropriate operation range.
  • the absorption tower cannot exhibit predetermined performance, and as a result, it may be difficult to continue the operation of the absorption tower.
  • the natural gas supplied to the adsorption tower in the water removal step 23 and the mercury removal step 24 becomes smaller than a fluctuation range suitable for operation
  • the natural gas supplied to the adsorption tower becomes a part of the filled adsorbent.
  • a drift channeling
  • natural gas comes into contact with only a part of the filled adsorbent, and the adsorption efficiency of components to be adsorbed (moisture and mercury) contained in the gas deteriorates.
  • the short circuit path may be fixed.
  • the life of the adsorbent may be extremely shorter than the design life on the premise of the entire adsorbent.
  • the demethanizer 17 in the hydrocarbon separation step 25 is a distillation column.
  • this demethanizer is a process of separating heavy hydrocarbons by performing self-cooling by introducing cold gas generated by the expander 14 into the cold boxes 11, 12, and 16 by supplying supplied natural gas to the cold boxes 11, 12, and 16.
  • the amount of supplied gas decreases, the cooling heat obtained by the expander 14 also decreases, and the efficiency of separating heavy hydrocarbons decreases.
  • the influence of the natural gas supply from the well base being lower than the design flow rate is mainly manifested in the impurity removing equipment group 20 and the demethanizer 17 which is the distillation equipment in the hydrocarbon separation step 25. .
  • the design flow rate of natural gas in each facility is often set based on the supply flow rate of natural gas during the plateau period.
  • small and medium-sized gas fields have a relatively short plateau period, and may transition to a decline period in a short period of several years to 10 years. For this reason, the period during which the natural gas processing device exhibits the performance according to the design flow rate is shortened, and the production efficiency may be reduced.
  • the natural gas processing apparatus when the gas field at the base of the well enters the decline period and the supply of natural gas decreases, a part of the methane gas is removed through the recycle gas line 10 into the impurity removal equipment group. Recycle to the entrance side of 20. For example, when the supply flow rate of the natural gas supplied to the acid gas removal step 22 via the supply line 100 becomes lower than a preset flow rate, the recycle gas line 10 is brought online. Then, the amount of methane gas recycled is adjusted by the control valve V10 shown in FIG. 2 so that the supply flow rate of the natural gas supplied to the acid gas removal step 22 is substantially equal to, for example, the plateau period.
  • the natural gas supplied to the impurity removing equipment group 20 is supplied to the impurity removing equipment group 20.
  • natural gas is supplied to the absorption tower in the acid gas removal step 22 at a flow rate similar to that during the plateau period.
  • the supply flow rate of the natural gas supplied to the impurity removing equipment group 20 and the hydrocarbon separation equipment that is, the flow rate of the natural gas flowing in each equipment can be maintained at about the same as the plateau period.
  • the steam load due to the shortage of the natural gas flow rate can be maintained at an operable flow rate, and the state in which the acid gas can be efficiently absorbed can be maintained.
  • each of the adsorption towers in the subsequent water removal step 23 and the mercury removal step 24 the occurrence of channeling due to a shortage of the flow rate of natural gas can be suppressed, and the state in which moisture and mercury can be adsorbed efficiently can be maintained.
  • the demethanizer (distillation equipment) 17 in the hydrocarbon separation equipment a reduction in the amount of cold heat generated due to a shortage of the supply flow rate of the liquefied natural gas and a reduction in the steam load in the distillation column are suppressed, and the distillation and separation of methane gas is efficiently performed. It can be carried out.
  • the natural gas flow rate can be maintained.
  • the amount of methane gas recycled is not limited to the case where the pressure on the inlet side of the impurity removing equipment group 20 is adjusted to an amount that can be maintained at the same level as the plateau period. For example, in consideration of the flow rate that can be supplied to the recycle gas line 10, even if the pressure is set to be maintained at a value equal to or more than 80% of the plateau period, an appropriate value according to the facility capacity or the like may be set. Good.
  • the impurity removal treatment is performed before the natural gas is liquefied, and then the hydrocarbon separation step 25 is performed. It is recycled at the entrance. Therefore, the output of the natural gas at the well base is reduced, and even when the supply of the natural gas is reduced, the amount of the natural gas supplied to the impurity removing equipment group 20 can be maintained at the same level as the plateau period. . Therefore, the pretreatment equipment (acid gas absorption tower or moisture and mercury adsorption tower) provided in the impurity removal equipment group 20 and the demethanizer 17 provided in the hydrocarbon separation equipment reduce the supply amount of natural gas. It is possible to suppress a decrease in the processing efficiency and perform a stable processing.
  • the equipment for performing the vapor pressure adjustment step 31 includes a distillation column (stabilizer) 131 for condensate, and the condensate separated in the gas-liquid separation step 21 described above is supplied via the condensate supply line 106. Is done.
  • an extraction line 108 for extracting the light gas separated by distillation of the condensate is connected to the top of the stabilizer 131, and the extracted light gas is compressed by, for example, the compressor 41 and then to the acid gas removal step 22. Merges with the supply line 100.
  • a condensate extraction line 107 for extracting condensate from which light gas accumulated at the bottom of the stabilizer 131 has been separated is connected to the bottom of the stabilizer 131, and the extracted condensate is discharged to the condensate storage step 32.
  • Reference numeral 43 provided on the condensate extraction line 107 indicates a cooler.
  • a branch line 109 branches off from the condensate extraction line 107.
  • the reboiler 42 is interposed in the branch line 109, and heats the condensate containing the extracted heavy component and returns the condensate to the stabilizer 131.
  • One end of a condensate recycle line 110 is connected to the condensate extraction line 107 downstream of the cooler 43, and the other end is connected to a condensate supply line 106.
  • Reference numeral 44 in FIG. 3 indicates a pump.
  • the vapor pressure adjusting step 31 when the amount of condensate supplied to the stabilizer 131 decreases with the decrease in the amount of natural gas produced from the well base, the liquid load decreases and the processing efficiency decreases. Then, by returning the condensate containing heavy components to the inlet side through the condensate recycle line 110, the supply amount of the condensate to the stabilizer 131 can be maintained at the same level as the plateau period. Accordingly, even when the production amount of natural gas at the base of the well decreases during the decline period, the stabilizer 131 can suppress the decrease in the processing efficiency due to the decrease in the amount of condensate.
  • a condensate recycle line 110 may be detachably provided to the condensate supply line 106 and the condensate extraction line 107.
  • the condensate recycle line 110 can be installed when the well enters a decline period in which the production amount of natural gas decreases.
  • the stabilizer 131 can be installed from the beginning of construction.
  • the above-mentioned recycle gas line 10 for methane gas shown in FIG. 2 has a large diameter and a long drawing distance, it is difficult to make it detachable. Therefore, it is possible to exemplify a case where a natural gas liquefaction apparatus is installed at the time of construction, and the use of the natural gas liquefaction apparatus is started at the timing when the output of natural gas decreases.
  • each of the above embodiments is not limited to the case where the present invention is applied to a natural gas liquefaction apparatus provided with a natural gas liquefaction facility.
  • a recycled gas line for recycling part of the methane gas to the inlet side of the impurity removing equipment group 20 10 may be provided.
  • the natural gas processing device provided with the recycled gas line 10 may be provided on a floating body floating on the ocean.
  • Reference Signs List 10 supply line 17 demethanizer 22 acid gas removal step 23 moisture removal step 24 mercury removal step 25 hydrocarbon removal step 26 liquefaction step 31 vapor pressure adjustment step 100 recycle gas line 101 pretreatment equipment 102 liquefaction equipment 131 condensate distillation tower 311 compressor

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  • Oil, Petroleum & Natural Gas (AREA)
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  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
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Abstract

Le problème décrit par la présente invention est de fournir une technique permettant d'éliminer les impuretés contenues dans un gaz naturel de manière stable même lorsque la quantité d'alimentation du gaz naturel est réduite. À cet effet, dans un dispositif de traitement de gaz naturel, un traitement d'élimination d'impuretés est effectué avant la liquéfaction de gaz naturel, puis une étape de séparation d'hydrocarbures (25) est effectuée, de telle sorte qu'une partie du méthane obtenue après la séparation peut être recyclée sur un côté d'orifice d'entrée d'un groupe d'installations d'élimination d'impuretés (20). Par conséquent, même lorsque la quantité de production de gaz naturel dans une tête de puits est réduite et que la quantité d'alimentation du gaz naturel est réduite, la quantité d'un gaz devant être fourni au groupe d'installations d'élimination d'impuretés (20) peut être augmentée. Par conséquent, la réduction du rendement de traitement dans le groupe d'installations d'élimination d'impuretés (20) avec la diminution de la quantité d'un gaz à traiter dans celui-ci (20) peut être empêchée.
PCT/JP2018/027710 2018-07-24 2018-07-24 Dispositif de traitement de gaz naturel et procédé de traitement de gaz naturel WO2020021633A1 (fr)

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KR1020207016933A KR102642311B1 (ko) 2018-07-24 2018-07-24 천연가스 처리 장치 및 천연가스 처리 방법
CN201880077980.1A CN111433329A (zh) 2018-07-24 2018-07-24 天然气处理装置以及天然气处理方法
PCT/JP2018/027710 WO2020021633A1 (fr) 2018-07-24 2018-07-24 Dispositif de traitement de gaz naturel et procédé de traitement de gaz naturel

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Citations (4)

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Publication number Priority date Publication date Assignee Title
JP2939814B2 (ja) * 1990-03-05 1999-08-25 日本酸素株式会社 メタン分離装置及び方法
JP4230956B2 (ja) * 2003-04-16 2009-02-25 エア プロダクツ アンド ケミカルズ インコーポレイテッド 天然ガスからのメタンより重い成分回収方法及び装置
JP5041650B2 (ja) * 2001-06-08 2012-10-03 オートロフ・エンジニアーズ・リミテッド 天然ガス液化
WO2015155818A1 (fr) * 2014-04-07 2015-10-15 三菱重工コンプレッサ株式会社 Installation flottante de production de gaz liquéfié

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Publication number Priority date Publication date Assignee Title
US20110067439A1 (en) 2007-07-09 2011-03-24 Lng Technology Pty Ltd. Method and system for production of liquid natural gas
EP2892631B1 (fr) * 2012-09-07 2018-11-14 Chevron U.S.A., Inc. Procédé permettant d'éliminer du mercure présent dans du gaz naturel
US9816754B2 (en) * 2014-04-24 2017-11-14 Air Products And Chemicals, Inc. Integrated nitrogen removal in the production of liquefied natural gas using dedicated reinjection circuit
EP2977430A1 (fr) * 2014-07-24 2016-01-27 Shell Internationale Research Maatschappij B.V. Stabilisateur de condensat d'hydrocarbure et procédé de production d'un flux de condensat d'hydrocarbure stabilisé

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2939814B2 (ja) * 1990-03-05 1999-08-25 日本酸素株式会社 メタン分離装置及び方法
JP5041650B2 (ja) * 2001-06-08 2012-10-03 オートロフ・エンジニアーズ・リミテッド 天然ガス液化
JP4230956B2 (ja) * 2003-04-16 2009-02-25 エア プロダクツ アンド ケミカルズ インコーポレイテッド 天然ガスからのメタンより重い成分回収方法及び装置
WO2015155818A1 (fr) * 2014-04-07 2015-10-15 三菱重工コンプレッサ株式会社 Installation flottante de production de gaz liquéfié

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