WO2003074955A1 - Method for liquefying a hydrocarbon-rich flow - Google Patents

Method for liquefying a hydrocarbon-rich flow Download PDF

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Publication number
WO2003074955A1
WO2003074955A1 PCT/EP2003/002081 EP0302081W WO03074955A1 WO 2003074955 A1 WO2003074955 A1 WO 2003074955A1 EP 0302081 W EP0302081 W EP 0302081W WO 03074955 A1 WO03074955 A1 WO 03074955A1
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WO
WIPO (PCT)
Prior art keywords
hydrocarbon
stream
refrigerant
liquefied
boiling
Prior art date
Application number
PCT/EP2003/002081
Other languages
German (de)
French (fr)
Inventor
Heinz Bauer
Herwig Landes
Rainer Sapper
Thorsten SCHÜLER
Original Assignee
Linde Aktiengesellschaft
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Publication date
Application filed by Linde Aktiengesellschaft filed Critical Linde Aktiengesellschaft
Priority to AU2003218673A priority Critical patent/AU2003218673A1/en
Publication of WO2003074955A1 publication Critical patent/WO2003074955A1/en
Priority to NO20044222A priority patent/NO20044222L/en

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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
    • 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
    • F25J1/0211—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 a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0212—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 a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
    • 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
    • F25J1/0002—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
    • F25J1/0025—Boil-off gases "BOG" from storages
    • 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
    • F25J1/003—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
    • F25J1/0047—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 an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—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 an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F25J1/0055—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 an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
    • 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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0092—Mixtures of hydrocarbons comprising possibly also minor amounts of nitrogen
    • 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
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • 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 a refrigerant mixture stream.
  • Natural gas liquefaction plants are either designed as so-called LNG baseload plants - plants for liquefying natural gas to supply natural gas as primary energy - or as so-called peak shaving plants - plants for liquefying natural gas to meet peak demand.
  • the aforementioned peak shaving plants are operated with expansion turbines or refrigerant mixtures in the refrigeration circuits.
  • LNG Baseload Plants are usually operated with refrigeration circuits that consist of hydrocarbon mixtures. These mixed cycles are more energy efficient than expander cycles and, with the large liquefaction capacities of the Baseload Plants, enable relatively low energy consumption.
  • the object of the present invention is to provide a generic method for liquefying a hydrocarbon-rich stream, in particular one Specify natural gas flow, which has a lower energy consumption compared to an expander process, but the equipment complexity - compared to conventional refrigerant mixture circuits - can be kept low. Furthermore, the procedural effort and thus the personnel required to operate the process should be minimized or optimized.
  • the refrigerant mixture flow consists of two components, one of the components being a component of the hydrocarbon-rich stream to be liquefied and the other component being a heavy hydrocarbon, at least at least propane or propylene, and before cooling and cooling-providing expansion of the two components, the refrigerant mixture is separated into a higher-boiling and a lower-boiling refrigerant fraction.
  • the inventive method for liquefying a hydrocarbon-rich stream combines the technical simplicity of an expander process with the operational or procedural simplicity and the energetic advantages of mixed refrigerant circuits.
  • the compression of the refrigerant mixture be carried out by means of an at least two-stage compression and the higher-boiling refrigerant fraction is mixed with the lower-boiling refrigerant fraction at an intermediate pressure level.
  • a dry, pretreated hydrocarbon-rich stream for example natural gas
  • the hydrocarbon-rich stream has, for example, a pressure between 10 and 60 bar.
  • the hydrocarbon-rich stream is then expanded via valve a and line 2 into the separator D1, in which undesired, heavier components, such as, for example, higher hydrocarbons, are separated off.
  • a C 2. -Rich fraction is drawn off via line 3, further cooled in the heat exchanger E1, thereby liquefied and possibly supercooled and then fed via line 4 and expansion valve b to the (intermediate) storage tank T or relaxed in it ,
  • a liquid fraction - in this case, liquefied natural gas (LNG) - can be withdrawn from line (intermediate) storage container T via line 5 and used for further use.
  • LNG liquefied natural gas
  • boil-off gas is withdrawn from the (intermediate) storage tank T via line 9, heated in the heat exchanger E1 against process streams to be cooled, and discharged via the fuel or fuel gas line 8 to be described.
  • the liquid fraction which may have been separated from the hydrocarbon-rich stream to be liquefied, is drawn off via line 7, in which an expansion valve c is arranged, and is heated in the heat exchanger E1 against process streams to be cooled, in the valve connected downstream of the heat exchanger E1 d relaxed and then discharged via line 8 as fuel or fuel gas from the process.
  • the above-described cooling and liquefaction of the hydrocarbon-rich stream is carried out according to the invention in the heat exchange against a refrigerant mixture stream which consists of two components.
  • the corresponding refrigeration circuit in the embodiments according to FIGS. 1 and 2 each has a two-stage compressor unit, consisting of the compressor stages C1 and C2. Each compressor stage is followed by an air or water cooler E2 or E3.
  • the refrigeration circuit also has a so-called warm separator D2.
  • the provision of only one warm separator considerably reduces the operational complexity of the method according to the invention, compared with the known refrigerant mixture circuits.
  • the separator D2 the refrigerant mixture is separated into a lower-boiling and a higher-boiling fraction.
  • the lower-boiling fraction is removed from the separator D2 at its head via line 23, cooled in the heat exchanger E1 and partially condensed and then expanded at the cold end of the heat exchanger E1 in the expansion valve f to provide cold.
  • the relaxed fraction is fed back to the heat exchanger E1 via line 24, evaporates in it against process streams to be cooled and is overheated and then fed via line 20 to the first stage C1 of the two-stage compressor unit.
  • the compressed lower-boiling fraction is then fed via line 21 to the second compressor stage C2 - the admixture of the higher-boiling fraction will be discussed in more detail below - and compressed to the final refrigerant circuit pressure, which is, for example, between 20 and 60 bar.
  • the second compressor stage C2 is also a
  • Downstream heat exchanger E3 as cooler.
  • the refrigerant mixture which has been cooled and partially condensed in the aftercooler E3 is then fed back to the separator D2 via line 22.
  • a higher-boiling liquid fraction is drawn off from the bottom of the separator D2 via line 25, cooled in the heat exchanger E1 and then expanded in the expansion valve e to the desired intermediate pressure in a cooling manner.
  • This fraction is then in turn fed to the heat exchanger E1 via line 26, warmed and evaporated therein against process streams to be cooled, and then fed via line 27 to the compressor unit before its second compressor stage C2.
  • Reliquefaction compressor C3 fed, compressed in this and then fed to the heat exchanger E1 via line 9 '.
  • a desired partial flow of the boil-off gas can now be re-liquefied in the heat exchanger E1 and fed back to the (intermediate) storage tank T via line 0 and expansion valve g or can be expanded therein.
  • Such a boil-off re-liquefaction circuit is expediently only provided if this is necessary and / or sensible due to the amount of boil-off gas that arises.

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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

The invention relates to a method for liquefying a hydrocarbon-rich flow (1), especially a natural gas flow, whereby the hydrocarbon-rich flow is liquefied by heat-exchange (E1) against a coolant mixture flow (22). The coolant mixture flow consists of two components, one of the components being part of the hydrocarbon-rich flow to be liquefied and the other component being heavy hydrocarbon, at least propane or propylene. The inventive method is characterized in that prior to cooling (E1) and refrigeration expansion (e, f) of the two components, the coolant mixture is separated (D2) into a higher-boiling (25) and a lower-boiling (23) coolant fraction.

Description

Beschreibung description
Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen StromesProcess for liquefying a hydrocarbon-rich stream
Die Erfindung betrifft ein Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes, insbesondere eines Erdgasstromes, wobei die Verflüssigung des Kohlenwasserstoff-reichen Stromes im Wärmetausch gegen einen Kaltemittelgemischstrom erfolgt.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 a refrigerant mixture stream.
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 designed as so-called LNG baseload plants - plants for liquefying natural gas to supply natural gas as primary energy - or as so-called peak shaving plants - plants for liquefying natural gas to meet peak demand.
Die vorgenannten Peak Shaving Plants werden mit Expansionsturbinen oder Kältemittelmischungen in den Kältekreisläufen betrieben.The aforementioned peak shaving plants are operated with expansion turbines or refrigerant mixtures in the refrigeration circuits.
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 operated with refrigeration circuits that consist of hydrocarbon mixtures. These mixed cycles are more energy efficient than expander cycles and, with the large liquefaction capacities of the Baseload Plants, enable relatively low energy consumption.
In energetischer Hinsicht problematisch sind jedoch Verfahren zur Verflüssigung von Erdgas, die eine Verflüssigungsleistung im Bereich von wenigen hundert Nm3/h bis zu einigen zehntausend Nm3/h aufweisen. Bei diesen Verflüssigungsverfahren werden oftmals die vorbeschriebenen Expander-Prozesse realisiert, wobei jedoch energetische Nachteile in Kauf genommen werden müssen.In terms of energy, however, processes for liquefying natural gas are problematic, which have a liquefaction capacity in the range from a few hundred Nm 3 / h to a few tens of thousands Nm 3 / h. With these liquefaction processes, the above-described expander processes are often implemented, although energy disadvantages have to be accepted.
Alternativ zu diesen Expander-Prozessen kommen auch sog. Single-Flow-Prozesse zur Anwendung; diese sind jedoch hinsichtlich ihres Betriebes sowie Equipments als vergleichsweise aufwendig einzustufen.As an alternative to these expander processes, so-called single-flow processes are also used; however, these are to be classified as comparatively complex in terms of their operation and equipment.
Aufgabe der vorliegenden Erfindung ist es, ein gattungsgemäßes Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes, insbesondere eines Erdgasstromes anzugeben, das gegenüber einem Expander-Prozess einen geringeren Energieverbrauch aufweist, wobei jedoch der apparative Aufwand - verglichen mit herkömmlichen Kältemittelgemischkreisläufen - niedrig gehalten werden kann. Ferner sollen der verfahrenstechnische Aufwand und damit das erforderliche Personal für den Betrieb des Prozesses minimiert bzw. optimiert werden.The object of the present invention is to provide a generic method for liquefying a hydrocarbon-rich stream, in particular one Specify natural gas flow, which has a lower energy consumption compared to an expander process, but the equipment complexity - compared to conventional refrigerant mixture circuits - can be kept low. Furthermore, the procedural effort and thus the personnel required to operate the process should be minimized or optimized.
Zur Lösung dieser Aufgabe wird vorgeschlagen, dass der Kaltemittelgemischstrom aus zwei Komponenten besteht, wobei eine der Komponenten ein Bestandteil des zu verflüssigenden Kohlenwasserstoff-reichen Stromes und die andere Komponente ein schwerer Kohlenwasserstoff, zumindest wenigstens Propan oder Propylen ist, und vor der Abkühlung und kälteleistenden Entspannung der beiden Komponenten eine Auftrennung des Kältemittelgemisches in eine höher siedende und eine tiefer siedende Kältemittelfraktion erfolgt.To solve this problem, it is proposed that the refrigerant mixture flow consists of two components, one of the components being a component of the hydrocarbon-rich stream to be liquefied and the other component being a heavy hydrocarbon, at least at least propane or propylene, and before cooling and cooling-providing expansion of the two components, the refrigerant mixture is separated into a higher-boiling and a lower-boiling refrigerant fraction.
Das erfindungsgemäße Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes vereinigt die apparatetechnische Einfachheit eines Expander-Prozesses mit der betriebs- bzw. verfahrenstechnischen Einfachheit sowie den energetischen Vorteilen von Kältemittelgemischkreisläufen.The inventive method for liquefying a hydrocarbon-rich stream combines the technical simplicity of an expander process with the operational or procedural simplicity and the energetic advantages of mixed refrigerant circuits.
Das erfindungsgemäße Verfahren weiterbildend wird vorgeschlagen, dass die Verdichtung des Kältemittelgemisches mittels einer wenigstens zweistufigen Verdichtung erfolgt und die höher siedende Kältemittelfraktion der tiefer siedenden Kältemittelfraktion auf einer Zwischendruckstufe zugemischt wird.Further developing the method according to the invention, it is proposed that the compression of the refrigerant mixture be carried out by means of an at least two-stage compression and the higher-boiling refrigerant fraction is mixed with the lower-boiling refrigerant fraction at an intermediate pressure level.
Das erfindungsgemäße Verfahren sowie weitere Ausgestaltungen desselben, dieThe inventive method and further refinements of the same
Gegenstände der abhängigen Patentansprüche darstellen, seien im Folgenden anhand der in den Figuren 1 und 2 dargestellten Ausführungsbeispiele näher erläutert. Hierbei unterscheiden sich die in den Figuren 1 und 2 dargestellten Ausführungsbeispiele lediglich dadurch, dass bei dem anhand der Figur 2 dargestellten Ausführungsbeispiel eine Rückverflüssigung des aus dem Speicherbehälter abgezogenen Boil-Off-Gases erfolgt.Represent subjects of the dependent claims, are explained in more detail below with reference to the embodiments shown in Figures 1 and 2. Here, the exemplary embodiments shown in FIGS. 1 and 2 differ only in that, in the exemplary embodiment shown in FIG. 2, the boil-off gas drawn off from the storage container is re-liquefied.
Gemäß der in der Figur 1 dargestellten Verfahrensweise wird dem erfindungsgemäßen Verflüssigungsverfahren über Leitung 1 ein trockener, vorbehandelter Kohlenwasserstoff-reicher Strom, beispielsweise Erdgas, zugeführt und im Wärmetauscher E1 abgekühlt sowie teilweise kondensiert. Der Kohlenwasserstoffreiche Strom weist beispielsweise einen Druck zwischen 10 und 60 bar auf.According to the procedure shown in FIG. 1, a dry, pretreated hydrocarbon-rich stream, for example natural gas, is fed to the liquefaction process according to the invention via line 1 and cooled in the heat exchanger E1 and partially condensed. The hydrocarbon-rich stream has, for example, a pressure between 10 and 60 bar.
Anschließend wird der Kohlenwasserstoff-reiche Strom über Ventil a sowie Leitung 2 in den Abscheider D1 , in dem ggf. unerwünschte schwerere Komponenten, wie beispielsweise höhere Kohlenwasserstoffe, abgetrennt werden, entspannt. Am Kopf des Abscheiders D1 wird eine C2.-reiche Fraktion über Leitung 3 abgezogen, im Wärmetauscher E1 weiter abgekühlt, dabei verflüssigt und ggf. unterkühlt und anschließend über Leitung 4 und Entspannungsventii b dem (Zwischen)Speicherbehälter T zugeführt bzw. in diesen entspannt.The hydrocarbon-rich stream is then expanded via valve a and line 2 into the separator D1, in which undesired, heavier components, such as, for example, higher hydrocarbons, are separated off. At the top of the separator D1, a C 2. -Rich fraction is drawn off via line 3, further cooled in the heat exchanger E1, thereby liquefied and possibly supercooled and then fed via line 4 and expansion valve b to the (intermediate) storage tank T or relaxed in it ,
Über Leitung 5 kann aus dem (Zwischen)Speicherbehälter T eine Flüssigfraktion - im vorliegenden Falle also verflüssigtes Erdgas (LNG) - abgezogen und seiner weiteren Verwendung zugeführt werden. Während der (Zwischen)Speicherung anfallendes Boil- Off-Gas wird aus dem (Zwischen)Speicherbehälter T über Leitung 9 abgezogen, im Wärmetauscher E1 gegen abzukühlende Verfahrensströme angewärmt und über die noch zu beschreibende Fuel- bzw. Brenngasleitung 8 abgeführt.A liquid fraction - in this case, liquefied natural gas (LNG) - can be withdrawn from line (intermediate) storage container T via line 5 and used for further use. During the (intermediate) storage, boil-off gas is withdrawn from the (intermediate) storage tank T via line 9, heated in the heat exchanger E1 against process streams to be cooled, and discharged via the fuel or fuel gas line 8 to be described.
Aus dem Sumpf des vorbeschriebenen Abscheiders D1 wird über Leitung 7, in der ein Entspannungsventil c angeordnet ist, die ggf. aus dem zu verflüssigenden Kohlenwasserstoff-reichen Strom abgetrennte Flüssigfraktion abgezogen, im Wärmetauscher E1 gegen abzukühlende Verfahrensströme angewärmt, in dem dem Wärmetauscher E1 nachgeschalteten Ventil d entspannt und anschließend über Leitung 8 als Fuel- bzw. Brenngas aus dem Prozess abgeführt.From the sump of the above-described separator D1, the liquid fraction, which may have been separated from the hydrocarbon-rich stream to be liquefied, is drawn off via line 7, in which an expansion valve c is arranged, and is heated in the heat exchanger E1 against process streams to be cooled, in the valve connected downstream of the heat exchanger E1 d relaxed and then discharged via line 8 as fuel or fuel gas from the process.
Die vorbeschriebene Abkühlung und Verflüssigung des Kohlenwasserstoff-reichen Stromes erfolgt erfindungsgemäß im Wärmetausch gegen einen Kaltemittelgemischstrom, der aus zwei Komponenten besteht. Der entsprechende Kältekreislauf weist bei den Ausführungsformen gemäß der Figuren 1 und 2 jeweils eine zweistufige Verdichtereinheit, bestehend aus den Verdichterstufen C1 sowie C2, auf. Jeder Verdichterstufe ist ein Luft- oder Wasserkühler E2 bzw. E3 nachgeschaltet. Ferner weist der Kältekreislauf einen sog. warmen Abscheider D2 auf. Das Vorsehen lediglich eines warmen Abscheiders reduziert - verglichen mit den bekannten Kältemittelgemischkreisläufen - den betriebstechnischen Aufwand des erfindungsgemäßen Verfahrens erheblich. In dem Abscheider D2 wird das Kältemittelgemisch in eine tiefer siedende sowie eine höher siedende Fraktion aufgetrennt. Die tiefer siedende Fraktion wird dem Abscheider D2 an dessen Kopf über Leitung 23 entnommen, im Wärmetauscher E1 abgekühlt sowie teilweise kondensiert und anschließend am kalten Ende des Wärmetauschers E1 im Entspannungsventil f kälteleistend entspannt. Über Leitung 24 wird die entspannte Fraktion wieder dem Wärmetauscher E1 zugeführt, in ihm gegen abzukühlende Verfahrensströme verdampft sowie überhitzt und anschließend über Leitung 20 der ersten Stufe C1 der zweistufigen Verdichtereinheit zugeführt.The above-described cooling and liquefaction of the hydrocarbon-rich stream is carried out according to the invention in the heat exchange against a refrigerant mixture stream which consists of two components. The corresponding refrigeration circuit in the embodiments according to FIGS. 1 and 2 each has a two-stage compressor unit, consisting of the compressor stages C1 and C2. Each compressor stage is followed by an air or water cooler E2 or E3. The refrigeration circuit also has a so-called warm separator D2. The provision of only one warm separator considerably reduces the operational complexity of the method according to the invention, compared with the known refrigerant mixture circuits. In the separator D2, the refrigerant mixture is separated into a lower-boiling and a higher-boiling fraction. The lower-boiling fraction is removed from the separator D2 at its head via line 23, cooled in the heat exchanger E1 and partially condensed and then expanded at the cold end of the heat exchanger E1 in the expansion valve f to provide cold. The relaxed fraction is fed back to the heat exchanger E1 via line 24, evaporates in it against process streams to be cooled and is overheated and then fed via line 20 to the first stage C1 of the two-stage compressor unit.
Nach Verdichtung in der ersten Verdichterstufe C1 erfolgt eine Abkühlung in dem nachgeschalteten Wärmetauscher E2. Anschließend wird die verdichtete tiefer siedende Fraktion über Leitung 21 der zweiten Verdichterstufe C2 zugeführt - auf die Zumischung der höher siedenden Fraktion wird im Folgenden noch näher eingegangen werden - und auf den Kältemittelkreislaufenddruck, der beispielsweise zwischen 20 und 60 bar liegt, verdichtet. Auch der zweiten Verdichterstufe C2 ist einAfter compression in the first compressor stage C1, cooling takes place in the downstream heat exchanger E2. The compressed lower-boiling fraction is then fed via line 21 to the second compressor stage C2 - the admixture of the higher-boiling fraction will be discussed in more detail below - and compressed to the final refrigerant circuit pressure, which is, for example, between 20 and 60 bar. The second compressor stage C2 is also a
Wärmetauscher E3 als Kühler nachgeschaltet. Das in dem Nachkühler E3 abgekühlte und teilweise kondensierte Kältemittelgemisch wird dann über Leitung 22 wieder dem Abscheider D2 zugeführt.Downstream heat exchanger E3 as cooler. The refrigerant mixture which has been cooled and partially condensed in the aftercooler E3 is then fed back to the separator D2 via line 22.
Aus dem Sumpf des Abscheiders D2 wird über Leitung 25 eine höher siedende Flüssigfraktion abgezogen, im Wärmetauscher E1 abgekühlt und anschließend im Entspannungsventil e kälteleistend auf den gewünschten Zwischendruck entspannt. Anschließend wird diese Fraktion über Leitung 26 wiederum dem Wärmetauscher E1 zugeführt, in ihm gegen abzukühlende Verfahrensströme angewärmt sowie verdampft und anschließend über Leitung 27 der Verdichtereinheit vor deren zweiter Verdichterstufe C2 zugeführt.A higher-boiling liquid fraction is drawn off from the bottom of the separator D2 via line 25, cooled in the heat exchanger E1 and then expanded in the expansion valve e to the desired intermediate pressure in a cooling manner. This fraction is then in turn fed to the heat exchanger E1 via line 26, warmed and evaporated therein against process streams to be cooled, and then fed via line 27 to the compressor unit before its second compressor stage C2.
Die in der Figur 2 dargestellte Verfahrensweise unterscheidet sich von der in der Figur 1 Dargestellten lediglich dadurch, dass das über Leitung 9 aus dem (Zwischen)Speicherbehälter T abgezogene Boil-Off-Gas nunmehr einemThe procedure shown in FIG. 2 differs from that shown in FIG. 1 only in that the boil-off gas drawn off from the (intermediate) storage container T via line 9 is now one
Rückverflüssigungsverdichter C3 zugeführt, in diesem verdichtet und anschließend über Leitung 9' dem Wärmetauscher E1 zugeführt wird. Nunmehr kann ein gewünschter Teilstrom des Boil-Off-Gases in dem Wärmetauscher E1 rückverflüssigt und über Leitung 0 und Entspannungsventil g wieder dem (Zwischen)Speicherbehälter T zugeführt bzw. in diesen entspannt werden. Ein derartiger Boil-Off-Rückverflüssigungskreislauf wird zweckmäßigerweise jedoch nur dann vorgesehen, wenn dies aufgrund der anfallenden Boil-Off-Gasmenge erforderlich und/oder sinnvoll ist. Reliquefaction compressor C3 fed, compressed in this and then fed to the heat exchanger E1 via line 9 '. A desired partial flow of the boil-off gas can now be re-liquefied in the heat exchanger E1 and fed back to the (intermediate) storage tank T via line 0 and expansion valve g or can be expanded therein. Such a boil-off re-liquefaction circuit is expediently only provided if this is necessary and / or sensible due to the amount of boil-off gas that arises.

Claims

Patentansprüche claims
1. Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes, insbesondere eines Erdgasstromes, wobei die Verflüssigung des Kohlenwasserstoff-reichen Stromes im Wärmetauach gegen einen Kaltemittelgemischstrom erfolgt, dadurch gekennzeichnet, dass der1. A 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 exchanger against a refrigerant mixture stream, characterized in that the
Kaltemittelgemischstrom aus zwei Komponenten besteht, wobei eine der Komponenten ein Bestandteil des zu verflüssigenden Kohlenwasserstoff-reichen Stromes und die andere Komponente ein schwerer Kohlenwasserstoff, zumindest wenigstens Propan oder Propylen ist, und vor der Abkühlung und kälteleistenden Entspannung der beiden Komponenten eine Auftrennung desThe mixed refrigerant stream consists of two components, one of the components being a component of the hydrocarbon-rich stream to be liquefied and the other component being a heavy hydrocarbon, at least at least propane or propylene, and a separation of the two components prior to cooling and expansion of the cooling effect
Kältemittelgemisches in eine höher siedende und eine tiefer siedende Kältemittelfraktion erfolgt.Refrigerant mixture takes place in a higher-boiling and a lower-boiling refrigerant fraction.
2. Verfahren nach Anspruch 1 , dadurch gekennzeichnet, dass die Verdichtung des Kältemittelgemisches mittels einer wenigstens zweistufigen Verdichtung erfolgt und die höher siedende Kältemittelfraktion der tiefer siedenden Kältemittelfraktion auf einer Zwischendruckstufe zugemischt wird.2. The method according to claim 1, characterized in that the compression of the refrigerant mixture is carried out by means of an at least two-stage compression and the higher-boiling refrigerant fraction is mixed with the lower-boiling refrigerant fraction at an intermediate pressure level.
3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass der verflüssigte Kohlenwasserstoff-reiche Strom zumindest teilweise zwischengespeichert wird und bei dieser Zwischenspeicherung anfallendes Boil-Off-Gas im Wärmetausch gegen den Kaltemittelgemischstrom rückverflüssigt wird.3. The method according to claim 1 or 2, characterized in that the liquefied hydrocarbon-rich stream is at least partially temporarily stored and boil-off gas generated during this intermediate storage is liquefied in heat exchange against the mixed refrigerant stream.
4. Verfahren nach einem der vorhergehenden Ansprüche 1 bis 3, dadurch gekennzeichnet, dass der zu verflüssigende Kohlenwasserstoff-reiche Strom bei tiefen Temperaturen entspannt und von bei dieser Entspannung anfallenden flüssigen Kohlenwasserstoffen befreit wird. 4. The method according to any one of the preceding claims 1 to 3, characterized in that the hydrocarbon-rich stream to be liquefied relaxes at low temperatures and is freed from liquid hydrocarbons occurring during this relaxation.
PCT/EP2003/002081 2002-03-06 2003-02-28 Method for liquefying a hydrocarbon-rich flow WO2003074955A1 (en)

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CN107436072A (en) * 2017-08-14 2017-12-05 新地能源工程技术有限公司 Natural gas liquefaction system and method with refrigerant supplementary device
CN107436072B (en) * 2017-08-14 2019-11-29 新地能源工程技术有限公司 Natural gas liquefaction system and method with refrigerant supplementary device
RU2807859C1 (en) * 2022-10-28 2023-11-21 Общество с ограниченной ответственностью научно-исследовательский и проектный институт "ПЕГАЗ" Natural gas liquefaction plant (embodiments)
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