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DE10226597A1 - Liquefying hydrocarbon-rich stream, especially natural gas stream, comprises relaxing hydrocarbon-rich stream before it is introduced into rectification stage - Google Patents

Liquefying hydrocarbon-rich stream, especially natural gas stream, comprises relaxing hydrocarbon-rich stream before it is introduced into rectification stage Download PDF

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Publication number
DE10226597A1
DE10226597A1 DE2002126597 DE10226597A DE10226597A1 DE 10226597 A1 DE10226597 A1 DE 10226597A1 DE 2002126597 DE2002126597 DE 2002126597 DE 10226597 A DE10226597 A DE 10226597A DE 10226597 A1 DE10226597 A1 DE 10226597A1
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Prior art keywords
hydrocarbon
rich
stream
rich stream
fraction
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DE2002126597
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German (de)
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Manfred BÖLT
Rainer Sapper
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Linde GmbH
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Linde GmbH
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—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
    • F25J1/02—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
    • F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
    • F25J1/025—Details related to the refrigerant production or treatment, e.g. make-up supply from feed gas itself
    • 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
    • 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
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual 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
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/64—Propane or propylene
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/66—Butane or mixed butanes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons

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

Abstract

Liquefying a hydrocarbon-rich stream, especially a natural gas stream, comprises carrying out the liquefaction of the hydrocarbon-rich stream in heat exchange with a coolant and/or coolant mixed stream, and separating the hydrocarbon-rich stream into a C2-rich fraction (7) and a C3+-rich stream. The hydrocarbon-rich stream is relaxed before being introduced into the rectification stage (T1) and the C2-rich fraction obtained by the rectification is compressed.

Description

Die Erfindung betrifft ein Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes, insbesondere eines Erdgasstromes, wobei die Verflüssigung des Kohlenwasserstoff-reichen Stromes im Wärmetausch gegen wenigstens einen Kältemittel- und/oder Kältemittelgemischstrom erfolgt und wobei der zu verflüssigende Kohlenwasserstoff-reiche Strom in einer rektifikatorischen Auftrennung in eine C2 –-reiche Fraktion, die der Verflüssigung unterworfen wird, und in eine C3+-reiche Fraktion aufgetrennt wird.The invention relates to a method for liquefying a hydrocarbon-rich stream, in particular a natural gas stream, the liquefaction of the hydrocarbon-rich stream taking place in the heat exchange with at least one refrigerant and / or refrigerant mixture stream, and the hydrocarbon-rich stream to be liquefied in a rectification separation into a C 2 - -rich fraction, which is subjected to liquefaction, and into a C 3+ -rich fraction.

Erdgasverflüssigungsanlagen werden entweder als sog. LNG Baseload Plants – also Anlagen zur Verflüssigung von Erdgas zur Versorgung mit Erdgas als Primärenergie – oder als sog. Peak Shaving Plants – also Anlagen zur Verflüssigung von Erdgas zur Deckung des Spitzenbedarfs – ausgelegt.Natural gas liquefaction plants are either as so-called LNG Baseload Plants Liquefaction plants of natural gas to supply natural gas as primary energy - or as so-called peak shaving Plants - well Liquefaction plants of natural gas to meet peak demand - designed.

Die vorgenannten Peak Shaving Plants werden mit Expansionsturbinen oder Kältemittelmischungen in den Kältekreisläufen betrieben. Die Kältekreisläufe enthalten oft nur eine oder wenige Komponenten.The aforementioned peak shaving plants are used with expansion turbines or refrigerant blends in the Refrigeration cycles operated. The refrigeration circuits included often only one or a few components.

LNG Baseload Plants werden im Regelfall mit Kältekreisläufen betrieben, die aus Kohlenwasserstoffgemischen bestehen. Diese Gemischkreisläufe sind energetisch effizienter als Expander-Kreisläufe und ermöglichen bei den großen Verflüssigungsleistungen der Baseload Plants entsprechend relativ niedrige Energieverbräuche.LNG Baseload Plants are usually included Refrigeration cycles operated, which consist of hydrocarbon mixtures. These are mixed cycles energetically more efficient than expander circuits and allow for the large liquefaction capacities the Baseload Plants correspondingly relatively low energy consumption.

Bei diesen Anlagen müssen zur Erzeugung des Inventars der Gemischkreisläufe, zur Deckung von Verlusten im Betrieb und aufgrund von Produktanforderungen die im Erdgas enthaltenen schweren Kohlenwasserstoffe abgetrennt werden. Dies geschieht üblicherweise durch eine rektifikatorische Fraktionierung des zu verflüssigenden Kohlenwasserstoff-reichen Stromes. Dabei wird nach einer Abkühlung und teilweiser Kondensation des zu verflüssigenden Kohlenwasserstoff-reichen Stromes mittels einer sog. HHC(Heavy Hydrocarbon)-Kolonne eine C3+-reiche Fraktion abgetrennt, bevor der verbleibende Strom – also das gasförmige Kopfprodukt aus der HHC-Kolonne – der weiteren Abkühlung und Verflüssigung unterworfen wird.In these plants, the heavy hydrocarbons contained in natural gas must be separated in order to generate the inventory of the mixture cycles, to cover losses during operation and due to product requirements. This is usually done by rectification fractionation of the hydrocarbon-rich stream to be liquefied. After cooling and partial condensation of the hydrocarbon-rich stream to be liquefied, a C 3+ -rich fraction is separated off using a so-called HHC (heavy hydrocarbon) column before the remaining stream - ie the gaseous top product from the HHC column - is subjected to further cooling and liquefaction.

Die in der HHC-Kolonne gewonnene Sumpffraktion wird normalerweise so mit schwereren Kohlenwasserstoffen angereichert, dass der geforderte Heizwert des LNG am Kopf der HHC-Kolonne eingestellt werden kann und dass bspw. C4-, C5- und C6-Kohlenwasserstoffe auf entsprechend geringe Anteile im Kopf der HH-Kolonne reduziert werden um ein mögliches Festwerden von z. B. Benzol im LNG zu verhindern.The bottoms fraction obtained in the HHC column is normally enriched with heavier hydrocarbons in such a way that the required calorific value of the LNG can be set at the top of the HHC column and that, for example, C 4 , C 5 and C 6 hydrocarbons are correspondingly low Shares in the top of the HH column are reduced to a possible solidification of z. B. to prevent benzene in LNG.

Die in der HHC-Kolonne gewonnene C3+-reiche Fraktion wird anschließend rektifikatorisch in ihre Bestandteile zerlegt, wobei diese teilweise als Make-Up-Fraktionen – bspw. C2H6 oder C3H8 – für den oder die Gemischkreisläufe verwendet oder als Nebenproduktströme – bspw. als LPG-Produktstrom – gewonnen und ggf. einer Weiterverarbeitung zugeführt werden.The C 3+ -rich fraction obtained in the HHC column is then rectified into its constituent parts, some of which are used as make-up fractions - for example C 2 H 6 or C 3 H 8 - for the mixture cycle or cycles can be obtained as by-product streams - for example as LPG product stream - and, if necessary, sent for further processing.

Diese Auftrennung der in der HHC-Kolonne gewonnenen C3+-reichen Fraktion wird bspw. mit folgenden Rektifikationskolonnen durchgeführt: Demethanizer, Deethanizer, Depropanizer und evtl. Debutanizer. Diese Kolonnen ermöglichen die Erzeugung folgender Fraktionen: Methan, Ethan und Ethan-Make-Up, Propan und Propan-Make-Up, LPG-Produkt (Flüssiggas) sowie eine C5+-Fraktion.This separation of the C 3+ -rich fraction obtained in the HHC column is carried out, for example, using the following rectification columns: demethanizer, deethanizer, depropanizer and possibly debutanizer. These columns enable the following fractions to be generated: methane, ethane and ethane make-up, propane and propane make-up, LPG product (liquid gas) and a C 5+ fraction.

Das gasförmige Kopfprodukt der HHC-Kolonne, das der weiteren Abkühlung und Verflüssigung unterworfen wird, unterliegt als LNG-Produktstrom bestimmten Heizwertanforderungen, so dass der Heizwert innerhalb eines bestimmten Bereiches mit fester Ober- sowie Untergrenze einstellbar sein sollte.The gaseous overhead of the HHC column, that of further cooling and subjected to liquefaction is subject to certain calorific value requirements as an LNG product stream, so that the calorific value within a certain range with fixed Upper and lower limits should be adjustable.

Aufgabe der vorliegenden Erfindung ist es, ein gattungsgemäßes Verfahren anzugeben, das es ermöglicht, den Heizwert des mittels des erfindungsgemäßen Verfahrens erzeugten, verflüssigten Kohlenwasserstoff-reichen Stromes in einem vergleichsweise weiten Bereich einzustellen.Object of the present invention is a generic method to indicate that it enables the calorific value of the liquefied produced by means of the method according to the invention Hydrocarbon-rich electricity in a comparatively wide range Range.

Zur Lösung dieser Aufgabe wird vorgeschlagen, dass der Kohlenwasserstoff-reiche Strom vor seiner Zuführung in die rektifikatorische Auftrennung entspannt und die in der rektifikatorischen Auftrennung gewonnene C2–-reiche Fraktion verdichtet wird.To solve this problem, it is proposed that the hydrocarbon-rich stream be expanded before it is fed into the rectification separation and that the C 2 - -rich fraction obtained in the rectification separation is compressed.

Bei der Verflüssigung eines Kohlenwasserstoff-reichen Stromes wird grundsätzlich versucht, den Druck, unter dem der Kohlenwasserstoff-reiche Strom vorliegt, zu nutzen und beizubehalten, um mit den dadurch möglichen Temperaturdifferenzen in den Wärmetauschern die Verflüssigung mit einem möglichst geringen spezifischen Energieverbrauch zu realisieren. Diese Verfahrensweise resultiert in einem vergleichsweise geringen Aufwand an Apparaten, insbesondere Wärmetauschern, sowie geringen Betriebskosten. Üblicherweise liegt Erdgas unter einem Druck von wenigstens 50 bar, oftmals auch unter einem Druck von 70 bar und darüber vor.When liquefying a hydrocarbon-rich Electricity is basically tried the pressure under which the hydrocarbon-rich stream is available to be used and maintained in order to be able to Temperature differences in the heat exchangers the liquefaction with one if possible to realize low specific energy consumption. This procedure results in a comparatively low outlay on equipment, especially heat exchangers, as well as low operating costs. Usually natural gas is under a pressure of at least 50 bar, often also under a pressure of 70 bar and above.

Der maximal nutzbare Druck des zu verflüssigenden Kohlenwasserstoff-reichen Stromes für die Verflüssigung ist jedoch begrenzt. Eine der Ursachen liegt darin begründet, dass die rektifikatorische Abtrennung der schweren Kohlenwasserstoffe aus dem zu verflüssigenden Kohlenwasserstoff-reichen Strom und damit die Einstellung des maximal geforderten Heizwertes des LNG-Produktstromes durch die Annäherung an den kritischen Druck und die Verringerung der Dichtedifferenz von Dampf und Flüssigkeit in der HHC-Kolonne erschwert bzw. begrenzt wird. Ferner kommen bei herkömmlichen Verflüssigungsanlagen aus einer Vielzahl von Gründen Plattenwärmetauscher zur Anwendung. Bei Erreichen bzw. oberhalb bestimmter Auslegungsdrücke wird deren Verwendung kostenungünstig, da bspw. die Anzahl der parallel einzusetzenden Plattenwärmetauscher stark ansteigt.However, the maximum usable pressure of the hydrocarbon-rich stream to be liquefied for liquefaction is limited. One of the reasons is that the rectification separation of the heavy hydrocarbons from the hydrocarbon-rich stream to be liquefied and thus the setting of the maximum required calorific value of the LNG product stream by approaching the critical pressure and reducing the density difference of steam and liquid is made difficult or limited in the HHC column. Also come with conventional liquefaction systems for a variety of reasons. When reaching or above certain design pressures, their use becomes inexpensive because, for example, the number of plate heat exchangers to be used in parallel increases sharply.

Diesen Problemen begegnet das erfindungsgemäße Verfahren dadurch, dass zunächst der Druck des zu verflüssigenden Kohlenwasserstoff-reichen Stromes vor dessen Abkühlung und Zuführung in die rektifikatorische Auftrennung verringert – die HHC-Kolonne kann somit in einem für sie günstigen Druckbereich betrieben werden – und anschließend lediglich das gasförmige Kopfprodukt der HHC-Kolonne wieder auf den gewünschten, höheren Druck verdichtet wird. Dadurch können im nachfolgenden Verflüssigungsteil die mit einem hohen Druck einhergehenden Vorteile realisiert werden.The method according to the invention addresses these problems in that at first the pressure of the liquefied Hydrocarbon-rich electricity before it is cooled and fed into the rectification separation is reduced - the HHC column can thus in one for they favorable printing range are operated - and then only the gaseous Top product of the HHC column is compressed again to the desired, higher pressure. This allows in the subsequent liquefaction part the advantages associated with high pressure are realized.

Beträgt beispielsweise der Druck eines zu verflüssigenden Erdgasstromes vor der Abkühlung und Zuführung des Erdgasstromes in die rektifikatorische Auftrennung 70 bar, so kann eine ausreichende Dichtedifferenz von Dampf und Flüssigkeit in der HHC-Kolonne bereits dann erreicht werden, wenn der Erdgasstrom auf einen Druck von etwa 58 bar entspannt wird. Würde die am Kopf der HHC-Kolonne abgezogene gasförmige Fraktion, die der Verflüssigung unterworfen wird, nunmehr bei lediglich etwa 58 bar verflüssigt werden, so hätte dies einen höheren Aufwand an Apparaten im Verflüssigungsteil sowie an Betriebskosten für den Verflüssigungsteil zur Folge. Aus diesem Grund erfolgt nunmehr erfindungsgemäß wiederum ein Verdichten der aus der HHC-Kolonne am Kopf abgezogenen gasförmigen, C2–-reiche Fraktion, bevor diese dem Verflüssigungsteil zugeführt wird.If, for example, the pressure of a natural gas stream to be liquefied before the cooling and feeding of the natural gas stream into the rectification separation is 70 bar, a sufficient density difference of steam and liquid in the HHC column can already be achieved when the natural gas stream is at a pressure of about 58 bar is relaxed. If the gaseous fraction drawn off at the top of the HHC column, which is subjected to the liquefaction, were now liquefied at only about 58 bar, this would result in a higher outlay in apparatus in the liquefaction section and in operating costs for the liquefaction section. For this reason, according to the invention, the gaseous, C 2 - -rich fraction withdrawn from the top of the HHC column is again compressed before it is fed to the liquefaction part.

Gemäß einer vorteilhaften Ausgestaltung des erfindungsgemäßen Verfahrens wird der Druck des Kohlenwasserstoff-reichen Stromes in der Entspannung um 10 bis 50 % verringert. Ebenso wird der Druck der der Verdichtung unterworfenen C2–-reichen Fraktion wieder vorzugsweise um 10 bis 50 % erhöht.According to an advantageous embodiment of the method according to the invention, the pressure of the hydrocarbon-rich stream is reduced by 10 to 50% in the expansion. Likewise, the pressure of the C 2 - -rich fraction subjected to compression is again preferably increased by 10 to 50%.

Das erfindungsgemäße Verfahren weiterbildend wird ferner vorgeschlagen, dass die Entspannung und/oder die Verdichtung mehrstufig ausgeführt sind.Further developing the method according to the invention it is also proposed that the relaxation and / or compression are carried out in several stages.

In vorteilhafter Weise wird die bei der Entspannung des zu verflüssigenden Kohlenwasserstoff-reichen Stromes gewonnene Energie zum Antreiben des oder der Verdichter verwendet.Advantageously, the the relaxation of the liquefied Hydrocarbon-rich electricity generated energy to drive the compressor or compressors used.

Das erfindungsgemäße Verfahren sowie weitere Ausgestaltungen desselben, die Gegenstände der abhängigen Patentansprüche darstellen, seien im Folgenden anhand des in der Figur dargestellten Ausführungsbeispieles näher erläutert.The method according to the invention and others Refinements of the same, which are the subject matter of the dependent claims, are based on the embodiment shown in the figure explained in more detail.

Gemäß der in der Figur dargestellten Verfahrensweise wird dem erfindungsgemäßen Verflüssigungsverfahren über Leitung 1 ein trockener und ggf. vorbehandelter Kohlenwasserstoff-reicher Strom, beispielsweise Erdgas, zugeführt.According to the procedure shown in the figure, the liquefaction process according to the invention is carried out via line 1 a dry and possibly pretreated hydrocarbon-rich stream, for example natural gas, is supplied.

Auf die ggf. notwendigen Vorbehandlungsschritte, wie beispielsweise Trocknung, CO2-Entfernung, Schwefelentfernung, etc. sei im Folgenden nicht näher eingegangen; die gängigen Verfahrensweisen sind dem Fachmann bekannt.The pretreatment steps that may be necessary, such as drying, CO 2 removal, sulfur removal, etc., are not discussed in more detail below; the usual procedures are known to the person skilled in the art.

Der über Leitung 1 herangeführte Erdgasstrom weist typischerweise einen Druck zwischen 70 und 100 bar auf. Im Expander X erfolgt nunmehr eine arbeitsleistende Entspannung auf einen Druck zwischen 40 und 70 bar. Anschließend wird der entspannte, Kohlenwasserstoff-reiche Strom über Leitung 1' dem Wärmetauscher E1 zugeführt und in diesem abgekühlt sowie teilweise kondensiert. Über Leitung 2 wird dieser Strom ein- oder zweiphasig der HHC-Kolonne T1 zugeführt. Der Sumpf der Kolonne T1 kann – wie in der Figur dargestellt – mittels eines Sumpfreboilers beheizt werden.The natural gas stream introduced via line 1 typically has a pressure between 70 and 100 bar. In the Expander X, there is now work-related relaxation to a pressure between 40 and 70 bar. The relaxed, hydrocarbon-rich stream is then fed via line 1 'to the heat exchanger E1 and is cooled in it and partially condensed. Via line 2 this stream is fed to the HHC column T1 in one or two phases. The bottom of column T1 can - as shown in the figure - be heated by means of a bottom reboiler.

Grundsätzlich ist es möglich, dass der entspannte, Kohlenwasserstoff-reiche Strom oder zumindest ein Teilstrom davon den Wärmetauscher E1 mittels einer in der Figur nicht dargestellten Leitung umgeht.Basically, it is possible that the relaxed, hydrocarbon-rich stream or at least one Partial flow of which the heat exchanger E1 bypasses by means of a line, not shown in the figure.

Am Kopf der Kolonne T1 wird über Leitung 4 eine C2 –-reiche Fraktion abgezogen, im Wärmetauscher E2 bzw. Kopfkondensator der Kolonne T1 abgekühlt und über Leitung 5 dem Abscheider D zugeführt. Aus dem Sumpf des Abscheiders D wird die in ihm gewonnene C3 –-Fraktion über Leitung 6 abgezogen und mittels der Pumpe P1 dem Kopf der HHC-Kolonne T1 als Rücklauf aufgegeben.At the top of column T1 is via line 4 a C 2 - -rich fraction is drawn off, cooled in the heat exchanger E2 or top condenser of the column T1 and via line 5 the separator D fed. C recovered in it 3 from the bottom of the separator D - fraction via line 6 withdrawn and fed to the top of the HHC column T1 as reflux by means of the pump P1.

Diese zurückgeführte C3 –-Fraktion ermöglicht es, dass in der HHC-Kolonne T1 C3+-Kohlenwasserstoffe mit einer ausreichenden Ausbeute aus dem zu verflüssigenden Kohlenwasserstoff-reichen Strom ausgewaschen werden. Ferner werden in der HHC-Kolonne T1 C5-Kohlenwasserstoffe sowie Benzol praktisch vollständig ausgewaschen. Der Benzolgehalt des am Kopf des Abscheiders D über Leitung 7 abgezogenen gasförmigen Stromes beträgt weniger als 1 ppm.This recycled C 3 - fraction makes it possible that in the HHC column T1 C 3+ hydrocarbons are washed out with a sufficient yield from the hydrocarbon-rich stream to be liquefied. Furthermore, T1 C 5 hydrocarbons and benzene are virtually completely washed out in the HHC column. The benzene content of the at the head of the separator D via line 7 withdrawn gaseous stream is less than 1 ppm.

Die am Kopf des Abscheiders D über Leitung 7 abgezogene, C2 –-reiche Fraktion wird in dem Verdichter V auf einen Druck zwischen 50 und 100 bar verdichtet und über Leitung 8 anschließend dem in der Figur nicht dargestellten Verflüssigungsteil, der im Wesentlichen beliebig ausgestaltet sein kann, zugeführt.The C 2 - -rich fraction drawn off at the top of the separator D via line 7 is compressed in the compressor V to a pressure between 50 and 100 bar and then via line 8 the liquefaction part, not shown in the figure, which is essentially of any design can, fed.

Sowohl der bereits beschriebene Expander X als auch der Verdichter V können hierbei mehrstufig ausgebildet sein. Der Verdichter V wird vorzugsweise durch den Expander X angetrieben.Both the Expander X as well as the compressor V can be multi-stage. The compressor V is preferred powered by the expander X.

Die aus dem Sumpf der HHC-Kolonne T1 über Leitung 3 abgezogene C3+-reiche Kohlenwasserstofffraktion wird über Ventil a in einen Demethanizer T3 entspannt. Am Kopf des Demethanizers T3 wird über Leitung 9 eine C1-Kohlenwasserstofffraktion abgezogen und bspw. als sog. Make-Up-Fraktion einem Kältemittel- bzw. Kältemittelgemischkreislauf zugeführt. Aus dem Sumpf des Demethanizers T3 wird über Leitung 10 eine C2+-Kohlenwasserstofffraktion abgezogen und über Ventil b in den Deethanizer T4 entspannt.The from the bottom of the HHC column T1 via line 3 drawn off C 3+ -rich hydrocarbon fraction is expanded via valve a in a Demethanizer T3. At the head of the Demethanizer T3 is via line 9 a C 1 hydrocarbon fraction is drawn off and, for example, as a so-called make-up fraction a refrigerant or mixed refrigerant circuit supplied. The swamp of the Demethanizer T3 becomes a pipe 10 a C 2+ hydrocarbon fraction is drawn off and expanded into the deethanizer T4 via valve b.

Am Kopf des Deethanizers T4 wird über Leitung 11 eine C2-Kohlenwasserstofffraktion abgezogen, die ggf. ebenfalls als Make-Up-Fraktion einem Kältemittel- bzw. Kältemittelgemischkreislauf zugeführt wird. Über Leitung 12 wird aus dem Sumpf des Deethanizers T4 eine C3+-Kohlenwasserstofffraktion abgezogen und über Ventil c in den Depropanizer T5 entspannt. Am Kopf des Depropanizers T5 wird über Leitung 13 eine C3-Kohlenwasserstoffproduktfraktion abgezogen.At the head of the Deethanizer T4 is via line 11 withdrawn a C 2 hydrocarbon fraction, which may also be supplied as a make-up fraction to a refrigerant or refrigerant mixture circuit. Via line 12 a C 3+ hydrocarbon fraction is drawn off from the bottom of the deethanizer T4 and expanded into the depropanizer T5 via valve c. At the head of the Depropanizer T5 is via line 13 a C 3 -Kohlenwasserstoffproduktfraktion withdrawn.

Über einen Seitenabzug (Leitung 14) wird aus dem Depropanizer T5 eine C3/C4-Produktfraktion – die sog. LPG-Produktfraktion – abgezogen und ggf. einer Weiterverarbeitung zugeführt. Diese LPG-Produktfraktion ist von großem wirtschaftlichen Wert, da LPG bei Umgebungstemperaturen verflüssigbar ist, einen hohen Energieinhalt aufweist und gut transportierbar ist. Darüber hinaus kann LPG umweltfreundlich verbrannt werden.Via a side trigger (line 14 ) a C 3 / C 4 product fraction - the so-called LPG product fraction - is withdrawn from the Depropanizer T5 and possibly further processed. This LPG product fraction is of great economic value because LPG can be liquefied at ambient temperatures, has a high energy content and is easy to transport. In addition, LPG can be burned in an environmentally friendly way.

Aus dem Sumpf des Depropanizers T5 wird über Leitung 15 eine C4+-Kohlenwasserstofffraktion abgezogen und über Ventil d in den Debutanizer T6 entspannt. Aus dem Kopfbereich des Debutanizers T6 wird über Leitung 16 eine C4-Produktfraktion abgezogen, während aus dem Sumpf über Leitung 17 eine C5+- bzw. Kohlenwasserstoff-Kondensatproduktfraktion abgezogen wird.The bottom of the Depropanizer T5 becomes a pipe 15 a C 4+ hydrocarbon fraction is drawn off and expanded into the Debutanizer T6 via valve d. A C 4 product fraction is drawn off from the head region of the Debutanizer T6 via line 16, while from the sump via line 17 a C 5+ or hydrocarbon condensate product fraction is withdrawn.

Das erfindungsgemäße Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes, insbesondere eines Erdgasstromes, ermöglicht es, den geforderten Heizwert der LNG-Produktfraktion in einem weiten Bereich einzustellen.The inventive method for liquefying a Hydrocarbon-rich stream, especially a natural gas stream, allows es, the required calorific value of the LNG product fraction in a wide range Range.

Claims (5)

Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes, insbesondere eines Erdgasstromes, wobei die Verflüssigung des Kohlenwasserstoff-reichen Stromes im Wärmetausch gegen wenigstens einen Kältemittel- und/oder Kältemittelgemischstrom erfolgt und wobei der zu verflüssigende Kohlenwasserstoff-reiche Strom in einer rektifikatorischen Auftrennung in eine C2–-reiche Fraktion, die der Verfüssigung unterworfen wird, und in eine C3+-reiche Fraktion aufgetrennt wird, dadurch gekennzeichnet, dass der Kohlenwasserstoff-reiche Strom (1) vor seiner Zuführung in die rektifikatorische Auftrennung (T1) entspannt (X) und die in der rektifikatorischen Auftrennung (T1) gewonnene C2 –-reiche Fraktion (7) verdichtet wird (V).Process for liquefying a hydrocarbon-rich stream, in particular a natural gas stream, the liquefaction of the hydrocarbon-rich stream taking place in the heat exchange with at least one refrigerant and / or refrigerant mixture stream, and the hydrocarbon-rich stream to be liquefied in a rectification separation into a C 2 - -fraction that is subjected to liquefaction and separated into a C 3+ -fraction, characterized in that the hydrocarbon-rich stream ( 1 ) relaxes (X) before it is fed into the rectification separation (T1) and the C 2 - -rich fraction obtained in the rectification separation (T1) ( 7 ) is compressed (V). Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass der Druck des Kohlenwasserstoff-reichen Strom (1) in der Entspannung (X) um 10 bis 50 verringert wird.A method according to claim 1, characterized in that the pressure of the hydrocarbon-rich stream ( 1 ) in the relaxation (X) is reduced by 10 to 50. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass der Druck der der Verdichtung (V) unterworfenen C2 –-reichen Fraktion (7) um 10 bis 50 % erhöht wird.A method according to claim 1 or 2, characterized in that the pressure of the C 2 - -rich fraction (V) subjected to compression (V) ( 7 ) is increased by 10 to 50%. Verfahren nach einem der vorhergehenden Ansprüche 1 bis 3, dadurch gekennzeichnet, dass die Entspannung (X) und/oder die Verdichtung (V) mehrstufig ausgeführt sind.Method according to one of the preceding claims 1 to 3, characterized in that the relaxation (X) and / or the Compression (V) are carried out in several stages. Verfahren nach einem der vorhergehenden Ansprüche 1 bis 4, dadurch gekennzeichnet, dass die bei der Entspannung (X) gewonnene Energie zum Antreiben des oder der Verdichter (V) verwendet wird.Method according to one of the preceding claims 1 to 4, characterized in that the obtained during relaxation (X) Energy is used to drive the compressor or compressors (V).
DE2002126597 2002-06-14 2002-06-14 Liquefying hydrocarbon-rich stream, especially natural gas stream, comprises relaxing hydrocarbon-rich stream before it is introduced into rectification stage Withdrawn DE10226597A1 (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006108821A1 (en) 2005-04-12 2006-10-19 Shell Internationale Research Maatschappij Method and apparatus for liquefying a natural gas stream
EP3048400A3 (en) * 2015-01-23 2016-11-23 Air Products And Chemicals, Inc. Improved separation of heavy hydrocarbons and ngls from natural gas in integration with liquefaction of natural gas

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006108821A1 (en) 2005-04-12 2006-10-19 Shell Internationale Research Maatschappij Method and apparatus for liquefying a natural gas stream
WO2006108820A1 (en) * 2005-04-12 2006-10-19 Shell Internationale Research Maatschappij B.V. Method and apparatus for liquefying a natural gas stream
RU2400683C2 (en) * 2005-04-12 2010-09-27 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Natural gas flow liquefaction method and equipment
EA014193B1 (en) * 2005-04-12 2010-10-29 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Method for liquefying a natural gas stream
CN101156038B (en) * 2005-04-12 2010-11-03 国际壳牌研究有限公司 Method and apparatus for liquefied natural gas streams
EP3048400A3 (en) * 2015-01-23 2016-11-23 Air Products And Chemicals, Inc. Improved separation of heavy hydrocarbons and ngls from natural gas in integration with liquefaction of natural gas

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