EP1941218A1 - Appareil et procédés de traitement des hydrocarbures destinés à produire du gaz naturel liquéfié - Google Patents

Appareil et procédés de traitement des hydrocarbures destinés à produire du gaz naturel liquéfié

Info

Publication number
EP1941218A1
EP1941218A1 EP05759335A EP05759335A EP1941218A1 EP 1941218 A1 EP1941218 A1 EP 1941218A1 EP 05759335 A EP05759335 A EP 05759335A EP 05759335 A EP05759335 A EP 05759335A EP 1941218 A1 EP1941218 A1 EP 1941218A1
Authority
EP
European Patent Office
Prior art keywords
lng
stream
gas
zone
cooling loop
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP05759335A
Other languages
German (de)
English (en)
Inventor
Ned P. Baudat
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
WOOD GROUP MUSTANG, INC.
Original Assignee
Mustang Engineering LP
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Mustang Engineering LP filed Critical Mustang Engineering LP
Publication of EP1941218A1 publication Critical patent/EP1941218A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0247—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 4 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • 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
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • 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
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return 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
    • 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
    • F25J1/0201—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 using only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—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 using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration 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
    • 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
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
    • F25J1/0277—Offshore use, e.g. during shipping
    • F25J1/0278—Unit being stationary, e.g. on floating barge or fixed platform
    • 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
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • 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
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
    • 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
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/72—Processing device is used off-shore, e.g. on a platform or floating on a ship or barge

Definitions

  • TITLE APPARATUS AND METHODS FOR PROCESSING HYDROCARBONS
  • the present invention relates to apparatus and methods for processing hydrocarbons. In another aspect, the present invention relates to apparatus and methods for processing natural gas. In still another aspect, the present invention relates to apparatus and methods for processing natural gas into liquified natural gas .
  • the liquefaction of natural gas is generally accomplished by reducing the temperature of natural gas to a liquefaction temperature of about -240 0 F to about -260 0 F at or near atmospheric pressure.
  • This liquefaction temperature range is typical for many natural gas streams because the boiling point of methane at atmospheric pressure is about -259 0 F.
  • conventional processes known in the art require substantial refrigeration to reduce and maintain natural gas at its liquefaction temperature. The most common of these refrigeration processes are: (1) the cascade process; (2) the single mixed refrigerant process; and (3) the propane pre-cooled mixed refrigerant process.
  • a cascade process produces LNG by employing several closed- loop cooling circuits, each utilizing a single pure refrigerant and collectively configured in order of progressively lower temperatures.
  • the first cooling circuit commonly utilizes propane or propylene as the refrigerant
  • the second circuit may utilize ethane or ethylene
  • the third circuit generally utilizes methane as the refrigerant.
  • a single mixed refrigerant process produces LNG by employing a single closed-loop cooling circuit utilizing a multicomponent refrigerant consisting of components such as nitrogen, methane, ethane, propane, butanes and pentanes.
  • the mixed refrigerant undergoes the steps of condensation, expansion and recompression to reduce the temperature of natural gas by employing a unitary collection of heat exchangers known as a "cold box.”
  • a propane pre-cooled mixed refrigerant process produces LNG by employing an initial series of propane-cooled heat exchangers in addition to a single closed-loop cooling circuit, which utilizes a multi-component refrigerant consisting of components such as nitrogen, methane, ethane and propane. Natural gas initially passes through one or more propane-cooled heat exchangers, proceeds to a main exchanger cooled by the multi- component refrigerant, and is thereafter expanded to produce LNG.
  • the construction and maintenance of such plants is expensive because of the cost of constructing, operating and maintaining one or more external, single or mixed refrigerant, closed-loop cooling circuits.
  • U.S. Pat. No. 3,360,944 to Knapp et al produces LNG by separating a natural gas feed stream into a major stream and a minor stream, cooling the major and minor streams to produce a liquid component, and thereafter using a substantial portion a the liquid component as a refrigerant for the process.
  • the liquid component is vaporized while undergoing heat exchange, compressed and discharged from the process.
  • the Knapp process results in only a minor portion of the natural gas feed stream processed into LNG.
  • U.S. Pat. No. 3,616,652 to Engal discloses a process for producing LNG in a single stage by compressing a natural gas feed stream, cooling the compressed natural gas feed stream to produce a liquefied stream, dramatically expanding the liquefied stream to an intermediate-pressure liquid, and then flashing and separating the intermediate-pressure liquid in a single separation step to produce LNG and a low-pressure flash gas.
  • the low-pressure flash gas is recirculated, substantially compressed and reintroduced into the intermediate pressure liquid.
  • the Engal process inefficiently expands its process stream pressure to a level that results in a substantial and highly inefficient recompression of its flash gas. Consequently, the Engal process yields a small volume of LNG compared to the amount of work required for its production, thus reducing the cost viability of the process.
  • U.S. Pat. No. 5,755,114 issued to Foglietta discloses a hybrid liquefaction cycle for the production of LNG.
  • the Foglietta process passes a pressurized natural gas feed stream into heat exchange contact with a closed-loop propane or propylene refrigeration cycle prior to directing the natural gas feed stream through a turboexpander cycle to provide auxiliary refrigeration.
  • the Foglietta process can be implemented with only one closed-loop refrigeration cycle, as opposed to cascade type mixed refrigerant systems currently used to produce atmospheric LNG.
  • the Foglietta process still requires at least one closed- loop refrigeration cycle comprising propane or propylene, both of which are explosive, not easily dispersed and must be stored on the vessels that transport the Foglietta product .
  • U.S. Pat. No. 6,023,942 to Thomas et al discloses a process for producing a methane-rich liquid product having a temperature above about -112 0 C. (-170°F.) at a pressure that is sufficient for the liquid product to be at or below its bubble point.
  • the resulting product is a pressurized liquid natural gas ("PLNG"), which has a pressure substantially above atmospheric pressure.
  • PLNG liquid natural gas
  • the Thomas et al . process can be implemented without external refrigeration, the product is pressurized requiring the use of specially designed heavy, thick-walled containers and transports (e.g., a PLNG ship, truck or railcar) . This higher pressure, heavier walled equipment adds substantial weight and expense to any commercial project.
  • the PLNG consumer will also require additional liquefaction, transport, and storage equipment to consume the PLNG, adding further cost to the supply and demand value chain.
  • U.S. Patent No. 6,564,578 issued May 20, 2003 to Fischer- Calderon, is directed to a process for producing LNG by directing a feed stream comprising natural gas to a cooling stage that (a) cools the feed stream in at least one cooling step producing a cooled feed stream, (b) expands the cooled feed stream in at least one expansion step by reducing the pressure of the cooled feed stream producing a refrigerated vapor component and a liquid component, and (c) separates at least a portion of the refrigerated vapor component from the liquid component wherein at least a portion of the cooling for the process is derived from at least a portion of the refrigerated vapor component; and repeating steps (a) through (c) one or more times until at least substantial portion of the feed stream in the first cooling stage is processed into LNG wherein the feed stream in step (a) comprises at least a portion of the liquid component produced from a previous cooling stage.
  • process stream 3 is shown in FIG. 1 with leading zero(s) , which leading zero(s) may or may not be used herein.
  • process stream 3 is shown in FIG. 1 with leading zero(s) , which leading zero(s) may or may not be used herein.
  • FIG. 1 as "003,” and may be referred to herein as process stream
  • FIG. 1 some process streams are shown with an alphabetic end character, for example streams 029a, 029b, 029b2, 029c, 029d and 029e.
  • these streams with the same number but different alphabetic end characters have the same composition, but may have different temperatures, pressures, and the physical state of the materials flowing therethrough may have changed (i.e., from liquid to gas, or gas to liquid, or from one state to a mixture of states, or a mixture of states to one state) .
  • a process for producing liquified natural gas includes all or any combination of the following: operating a gas cooling loop by (1) contacting a natural gas stream (process stream 003) with a return stream (process stream 009h) of the gas cooling loop to form a combined stream (process stream 005) , wherein the natural gas stream comprises methane and heavier hydrocarbons, and the return stream (process stream 009h) comprises methane, (2) passing the combined stream (process stream 005) through a heat transfer zone and then to a gas cooling loop first gas/liquid separation zone forming a first separation zone gas stream (process stream 008) comprising methane and a gas ⁇ cooling loop first separation zone liquid stream (process stream 007) comprising heavier hydrocarbons, (3) passing the first separation zone gas stream (process stream 009a) through an expansion zone, then through the transfer zone, and then through a compression zone to form the return stream (process stream 009h) of the gas cooling loop;
  • process stream 030 to LNG storage and recovering any LNG vapors as an LNG boiloff stream (process stream 039) and combining the boiloff stream with the return stream (process stream 029e) of the LNG cooling loop, and recovering LNG product from LNG storage as an LNG product stream (process stream 034) .
  • a more specific embodiment of the above embodiment includes the use of a multizone heat transfer zone. Specifically, according to a more specific embodiment of the above embodiment, there is provided a process for producing liquified natural gas.
  • the process of this embodiment includes all or any combination of the following: operating a gas cooling loop by (1) contacting a natural gas stream (003) with a return stream (009h) " of the gas cooling loop to form a combined stream (005) , wherein the natural gas stream comprises methane and heavier hydrocarbons, and the return stream (009h) comprises methane, (2) passing the combined stream (005) through a first zone of a heat transfer zone and then to a gas cooling loop first gas/liquid separation zone forming a first separation zone gas stream (008) comprising methane and a gas cooling loop first separation zone liquid stream (007) comprising heavier hydrocarbons, (3) passing the first separation zone gas stream (009a) through an expansion zone, then through a second zone of the transfer zone, then through the first zone of the heat transfer zone, and then through a compression zone to form the return stream (009h) of the gas cooling loop; taking the gas cooling loop first separation zone liquid stream (007) as a distillation zone feed stream (019) , and distilling this distillation zone feed stream
  • an apparatus for producing liquified natural gas includes the equipment as necessary to implement the method embodiments described above, including any portion of the method embodiments as described above.
  • an apparatus for processing natural gas comprising: a gas cooling loop unit comprising, a natural gas inlet line for receiving the natural gas, a heat exchange zone, a gas/liquid separation zone having a gas exit line and a liquid exit line, an gas cooling loop expansion zone, and a gas cooling loop compression zone, and gas cooling loop piping defining a gas cooling loop flow path suitable to allow the received natural gas from the inlet line to be combined with a gas cooling loop recycled gas from the compression zone and flow, through a first path through the heat exchange zone, to the gas/liquid separator wherein any condensed liquid exits through the liquid exit line, and any remaining gas exits through the gas exit line, with the remaining gas then passing through the expansion zone, through a second path through the heat exchange zone, through the compression zone to be recycled back as the gas cooling loop recycled gas,-
  • distillation unit having an inlet, a gas outlet, and a liquid outlet, wherein the inlet is connected to the gas cooling loop liquid exit line;
  • an LNG cooling loop unit ⁇ an LNG compression zone, the heat exchanger zone, an LNG expander, an LNG recovery unit, and LNG piping defining an LNG cooling loop path suitable to allow a compressed LNG boiloff gas and a third LNG recycle gas to be combined into a combined gas which flows through the LNG compression zone, through a third path through the heat exchange zone, through the expander, and through a first LNG splitter and split into a first LNG recycle gas and a first LNG remaining gas, with the first remaining gas flowing through a fourth path through the heat exchange zone, and through a second LNG splitter and split into a second LNG recycle gas and a second LNG remaining gas, with the second remaining gas flowing through a fifth path through the heat exchange zone, and through a third LNG splitter and split into a third LNG recycle gas and a third LNG remaining gas, with the third LNG remaining gas passing through the distillation unit, and distilled into the compressed LNG boiloff gas and an LNG product, with the first LNG recycle gas passing through a sixth path through the heat exchange zone and recycled through the compression zone, with the second LNG recycle gas
  • an apparatus for processing natural gas comprising: a gas cooling loop unit comprising, a natural gas inlet line for receiving the natural gas, a heat exchange unit having first, second, and third zones, a gas/liquid separation zone having a gas exit line and a liquid exit line, an gas cooling loop expansion zone, and a gas cooling loop compression zone, and gas cooling loop piping defining a gas cooling loop flow path suitable to allow the received natural gas from the inlet line to be combined with a gas cooling loop recycled gas from the compression zone and flow, through a first path through the first zone of the heat exchange unit, to the gas/liquid separator wherein any condensed liquid exits through the liquid exit line, and any remaining gas exits through the gas exit line, with the remaining gas then passing through the expansion zone, through a second path through the second zone and then first zone of the heat exchange unit, through the compression zone to be recycled back as the gas cooling loop recycled gas;
  • distillation unit having an inlet, a gas outlet, and a “liquid outlet, wherein the inlet is connected to the " gas cooling loop liquid exit line,-
  • an LNG cooling loop unit comprising, an LNG compression zone, the heat exchanger unit, an LNG expander, an LNG recovery unit, and LNG piping defining an LNG cooling loop path suitable to allow a compressed LNG boiloff gas and a third LNG recycle gas to be combined into a combined gas which flows through the LNG compression zone, through a third path through the first zone of the heat exchange unit, through the expander, and through a first LNG splitter and split into a first LNG recycle gas and a first LNG remaining gas, with the first remaining gas flowing through a fourth path through the second zone of the heat exchange unit, and through a second LNG splitter and split into a second LNG recycle gas and a second LNG remaining gas, with the second remaining gas flowing through a fifth path through the third zone of the heat exchange unit, and through a third LNG splitter and split into a third LNG recycle gas and a third LNG remaining gas, with the third LNG remaining gas passing through the distillation unit, and distilled into the compressed LNG boiloff gas and an LNG product, with the first LNG recycle gas passing through a sixth path through the first zone
  • FIG. 1 is a schematic process flow diagram illustrating one embodiment of the process and apparatus of the present invention, showing various process streams and equipment, the main process loops including gas cooling loop 220, LNG cooling loop 240, and liquifaction loop 260, and the main process equipment including separators 103, 105, 107 and 108, compressors 131, 132, 135, 137, 138, 139, and 134, liquifaction exchangers 122, 124, 125, distillation unit 160, and LNG storage tank 109.
  • the main process loops including gas cooling loop 220, LNG cooling loop 240, and liquifaction loop 260
  • the main process equipment including separators 103, 105, 107 and 108, compressors 131, 132, 135, 137, 138, 139, and 134, liquifaction exchangers 122, 124, 125, distillation unit 160, and LNG storage tank 109.
  • Process 100 includes as main process loops, the gas cooling loop 220, LNG cooling loop 240, and liquifaction loop 260.
  • the main process equipment includes separators 103, 105, 107 and 108, compressors 131, 132, 135, 137, 138, 139, and 134, liquifaction exchangers 122, 124, 125, distillation unit 160, and LNG storage tank 109.
  • the proposed design operating conditions i.e., temperature, pressure, flowrates
  • the composition of the input feed gas being processed can vary depending upon the composition of the input feed gas being processed, equipment design variations, process design variations, and the particular manner in which the equipment and process are being operated.
  • conditions may also vary depending upon particular operating goals/limitations, which force/require that any plant be operated in a certain manner.
  • Flowrates vary depending upon plant capacity and size.
  • any temperatures, pressures, flowrates, heating/cooling duties, and the like, shown in FIGs. 1 and 2 should be considered merely design examples, and that may vary depending upon any number of design/operational circumstances . It is to be understood that values inside or outside those ranges could be utilized, given particular circumstances.
  • shown in Table ⁇ are temperature and pressure ranges are provided for a number of the process streams in FIG. 1.
  • composition ranges for a number of selected streams are shown in Table 2 .
  • Table 1 examples of temperature and pressure ranges for selected process streams.
  • the various physical components of the present invention may be any that are well known to those of skill in the art .
  • the patentability of the apparatus of the present invention does not reside in the patentablity of any single piece of equipment, but rather in the unique and nonobvious arrangement of the various equipment to form the overall apparatus or portion of the apparatus.
  • individual process steps are generally known to those of skill in the art.
  • the patentability of the process of the present invention does not reside in the " patentablity of any single process step, but rather in the unique and nonobvious arrangement of the various process steps to form the overall process or a portion of the process .
  • Inlet gas stream 1 comprises natural gas.
  • natural gas is understood to mean raw natural gas or treated natural gas .
  • Raw natural gas primarily comprises light hydrocarbons such as methane, ethane, propane, butanes, pentanes, hexanes and impurities like benzene, but may also comprise small amounts of non-hydrocarbon impurities, such as nitrogen, hydrogen sulfide, carbon dioxide, and traces of helium, carbonyl sulfide, various mercaptans or water.
  • Treated natural gas primarily comprises methane and ethane, but may also comprise a small percentage of heavier hydrocarbons, such as propane, butanes and pentanes.
  • natural gas While natural gas ideally contains primarily light hydrocarbons, it unfortunately many times also comprises small amounts of non-hydrocarbon impurities, such as nitrogen, hydrogen sulfide, carbon dioxide, and traces of helium, carbonyl sulfide, various mercaptans or water.
  • non-hydrocarbon impurities such as nitrogen, hydrogen sulfide, carbon dioxide, and traces of helium, carbonyl sulfide, various mercaptans or water.
  • the exact percentage composition of the raw natural gas is dependant upon its reservoir source and any gas plant pre-processing steps. For instance, natural gas may comprise as little as 55 mole percent methane. However, it is preferable that the natural gas suitable for this process comprises at least about 75 mole percent methane, more preferably at " least about 85 mole percent methane, and most preferably at least about 90 mole percent methane for best results.
  • the exact composition of the non-hydrocarbon impurities also varies depending upon the reservoir source of the natural
  • a common optional pretreatment for inlet gas stream 1 includes passing it thru an amine absorber to remove CO 2 .
  • CO 2 will also solidify at cryogenic temperatures and cause operational problems in the cryogenic liquification exhanger.
  • gas to be pretreated thru an amine absorber is first heated to about 100 0 F, as the heating prevents/reduces foaming in the amine absorption process and increases mass transfer of the CO 2 to the amine fluid.
  • Another common pretreatment for inlet gas stream 1 includes passing it thru a mercury guard bed, as mercury is corrosive to the aluminum equipment commonly used in cryogenic operations. Even if mercury is not seen in the process, it is generally preferred to guard against its presence.
  • Inlet gas stream 1 is received by inlet separator 103 where it is separated into gas stream 3 and liquid stream 2 (the computer model shown in FIG. 1, assumes that stream 6 is split into equal streams 1 and 2, with stream 2 flowing to a second identical process 100.
  • Gas cooling loop 220 is fed by gas stream 3 which is shown flowing to optional tee 403 where it may be split into rarely used optional emergency fuel gas stream 58 and gas stream 4.
  • Process gas stream 4 flows to tee 404 where it is combined with recycle gas stream 9h to form gas stream 5. As will be shown below, this recycle gas stream 9h completes cooling loop 220.
  • Gas stream 5 is now passed thru a lower, generally first stage of LNG liquefaction exchanger 122 (1 st flow path thru the liquefaction exchanger) where it is cooled to about -50°F and partially condenses.
  • LNG liquefaction exchanger used herein may be any suitable
  • the liquefaction exchanger comprises exchangers 122 , 124 and 125, which may also be thought of as stand alone exchangers, or may be thought of as first, second and third zones of the liquefaction heat exchanger.
  • Cooled gas stream 5, exiting as gas stream 6, is received by separator 105 where it is separated into gas stream 8 and liquid stream 7.
  • Tee 406 separates gas stream 8 into gas streams 9a and 10.
  • Gas stream 10 is used to regulate the volume and flow of gas cooling loop 220, and is expanded and cooled into partially condensed stream 11 having a pressure of about 280 psia by expander 408, non-limiting examples of which include a turboexpander or a Joule-Thompson valve.
  • stream 11 Received into separator 107, stream 11 is separated into gas stream 13 and liquid stream 12. This gas stream 13 becomes gas stream 14 and passes thru LNG liquefaction exchanger (9 th flow path) exiting as stream 15 and feeding into mixer 416.
  • Gas stream 9a is expanded by expander 142 to a pressure of about 225 psia into expanded cool gas stream 9b to provide cooling duty to the liquefaction exchangers.
  • Gas stream 9b is passed thru an upper stage of LNG liquefaction exchanger 124, exiting as gas stream 9c, which is then passed thru an upper stage of LNG liquefaction exchanger 122, exiting as gas stream 9d (2 nd flow path thru exchangers 124 and 122) .
  • gas stream 9d Before gas stream 9d can be recycled back to join inlet gas 4 and complete gas cooling loop 220, its pressure must be increased and its temperature cooled to match that of inlet gas stream 4. While one compressor and one heat exchanger could be utilized, the embodiment as shown in FIG. 1, utilizes compressors 138 and 139, and heat exchangers 156 and 157.
  • Gas stream 9d is compressed by methane booster compressor 139 into discharged gas stream 9e having a pressure of about 310 psia.
  • This methane booster compressor 139 is driven by methane expander 142, so the discharge pressure of methane booster compressor depends on the mechanical efficiency of both devices.
  • Stream 9e exits heat exchanger 157 as a cooler stream 9f at a temperature of about 95 0 F.
  • This gas stream 9f is compressed by methane compressor 138 into discharged gas stream 9g having a pressure of about 310 psia.
  • Stream 9g exits heat exchanger 157 as a cooler stream 9h at a temperature of about 95°F, and then joins gas stream 4 to complete gas cooling loop 220.
  • one or more, preferably all, of the liquid streams removed from gas cooling loop 220 are sent to distillation tower 160.
  • liquid streams 2 and 7 are combined at tee 409 into liquid stream 17 which passes thru valve 413 exiting as stream 18.
  • Liquid stream 12 passes thru valve 414 and exits as stream 16.
  • These streams 16 and 18 are combined at tee 411 into stream 19 which is received by distillation tower 160.
  • Heavy hydrocarbon components exit the bottom of distillation tower as stream 20, and may be blended with crude product from the production site, or otherwise sold or disposed.
  • Overhead stream 21 becomes stream 21b and flows into LNG cooling loop at mixer 416.
  • the front end of LNG cooling loop 240 is fed by stream 39 which comprises recovered vapors from LNG receiver 108 and LNG storage tank 109, and recycled cooling stream 29e, which are combined at tee 417 into feed stream 40. While the present embodiment is shown illustrated with a series of four compressors 131, 132, 135 and 137 utilized in LNG cooling loop 240, it should be understood that any number of compressors may be utilized as dictated by the process design and economics.
  • Stream 40 is compressed in first stage LNG compressor 131 and discharged as stream 41 at a pressure of about 85 psia. This stream 41 is cooled by air-cooler 151 into cooled stream 42 having a temperature of about 95°F. Recycled cooling stream 26d and stream 41 are combined at mixer 419 into stream 43. Stream 43 is compressed in LNG booster compressor 132 and discharged as stream 44 at a pressure of about 110 psia. This stream 44 is cooled by air-cooler 152 into cooled stream 45 having a temperature of about 95°F.
  • the LNG booster expander 132 is driven by the LNG refrigerant expander 141, so the discharge pressure of the LNG booster compressor depends on the mechanical efficiency of both devices.
  • Stream 45 is compressed in third stage LNG compressor 135 and discharged as stream 46 at a pressure of about 205 psia.
  • This stream 46 is cooled by air-cooler 153 into " cooled stream 47 having a temperature of about 95 0 F.
  • Recycled cooling stream 23c and stream 47 are combined at mixer 421 into stream 48.
  • Stream 48 is compressed in fourth stage LNG compressor 137 and discharged as stream 49 at a pressure of about 740 psia. This stream 49 is cooled by air-cooler 155 into cooled stream 50 having a temperature of about 95 0 F.
  • Optional tee 422 splits stream 50 into optional stream 51F to allow for fuel gas takeoff if desired, and into stream 51 which is passed thru LNG liquefaction exchanger 122 exiting as stream 52 cooled to about 25°F (3 rd flow path) .
  • Gas stream 52 then enters LNG refrigerant expander 141 where it exits as stream 53 at a pressure of about 265 psia and a temperature of about - 6O 0 F.
  • this stream 53 is combined into stream 22 with earlier described stream 21b from overhead of distillation tower
  • streams 21b and 15 may be introduced into LNG cooling loop 240 at any number of suitable points.
  • streams 21b and 15 are introduced into LNG cooling loop 240 to rather immediately through the 4 th flow path, although any number of other points might also be suitable depending upon process conditions.
  • streams 21b and 15 are introduced into LNG cooling loop 240 at points that are efficient for the process, which generally means trying to match temperature, pressure, and/or composition of these streams to the introduction point.
  • Stream 22 is split by tee 423 (1 st splitter) into streams 23a and 24B.
  • Stream 23a is expanded thru valve 425 into stream 23b, which passes thru LNG liquefaction exchanger 122 (6 th flow path) , exiting as earlier described recycled cooling stream 23c which feeds into mixer 421.
  • Stream 24 passes thru LNG liquefaction exchanger 124 (4 th flow path), exiting as stream 25, which is split by tee 428 into stream 26a and stream 27.
  • Stream 26a is expanded thru valve 429 into stream 26b, which passes thru LNG liquefaction exchanger 124, exiting as stream 26c.
  • This stream 26c then passes thru LNG liquefaction exchanger 122, exiting as earlier described recycled cooling stream 26d which feeds into mixer 419 (7 th flow path thru exchangers 124 and 122) .
  • Stream 27 passes thru LNG liquefaction unit 125 exiting as stream 28 (5 th flow path) .
  • This stream 28 is split tee 431 into streams 29a and 30.
  • Stream 29a is expanded thru valve 432 into stream 29b, which passes thru LNG liquefaction exchanger 125, exiting as stream
  • stream 29c passes thru LNG liquefaction exchanger
  • Gas stream 30 is expanded thru valve 433 where it liquefies, forming stream 31 at pressure of about 20 psia and a temperature of about -250 0 F. This LNG stream 31 is received by LNG receiver vessel 108.
  • LNG receiver vessel liquid stream 32 passes thru valve 435 and enters as stream 33 into LNG storage tank 109.
  • LNG receiver vessel vapor stream 35 passes thru valve 436 forming stream 36, which is joined at mixer 438 by LNG storage tank vapor stream 37, to form stream 38a which becomes stream 38b.
  • LNG boiloff compressor 134 compresses stream 38b to about 25 psia into earlier described stream 39, which feeds into mixer 417 at the front end of LNG cooling loop 240.
  • Liquid remaining in LNG storage tank 109 is the final LNG product and can be sold or stored as necessary.
  • LNG product stream 34 feeds into the intake side of LNG product pump 439.

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Abstract

La présente invention concerne un appareil et des procédés destinés à récupérer du GNL à partir de gaz naturel de réservoir, lesdits appareil et procédés impliquant de faire circuler une partie du gaz naturel à travers une boucle de refroidissement comportant des échangeurs de chaleur, une zone d’expansion et une zone de compression. Le procédé implique également d'éliminer les liquides de la boucle de refroidissement du gaz et de distiller ces liquides afin de récupérer un gaz distillé. Le procédé implique également de comprimer et de dilater diverses parties du gaz distillé et de faire passer ces parties à travers des échangeurs de chaleur en commun avec la boucle de refroidissement du gaz, de manière à chauffer ou refroidir, selon ce qui est souhaité. Le procédé implique également d’éliminer une partie du contenu de la boucle de refroidissement du GNL en tant que GNL produit.
EP05759335A 2005-06-09 2005-06-09 Appareil et procédés de traitement des hydrocarbures destinés à produire du gaz naturel liquéfié Withdrawn EP1941218A1 (fr)

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US10995910B2 (en) 2015-07-13 2021-05-04 Technip France Process for expansion and storage of a flow of liquefied natural gas from a natural gas liquefaction plant, and associated plant

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US6269656B1 (en) * 1998-09-18 2001-08-07 Richard P. Johnston Method and apparatus for producing liquified natural gas
WO2000079179A1 (fr) * 1999-06-23 2000-12-28 Chicago Bridge & Iron Company Systeme et appareil de condensation de vapeur evaporee provenant d'un conteneur de gaz naturel liquefie
US6564578B1 (en) * 2002-01-18 2003-05-20 Bp Corporation North America Inc. Self-refrigerated LNG process

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US10995910B2 (en) 2015-07-13 2021-05-04 Technip France Process for expansion and storage of a flow of liquefied natural gas from a natural gas liquefaction plant, and associated plant

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