EP3252406B1 - Verflüssigungsverfahren von kohlendioxid aus einem erdgasstrom - Google Patents

Verflüssigungsverfahren von kohlendioxid aus einem erdgasstrom Download PDF

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Publication number
EP3252406B1
EP3252406B1 EP17171766.3A EP17171766A EP3252406B1 EP 3252406 B1 EP3252406 B1 EP 3252406B1 EP 17171766 A EP17171766 A EP 17171766A EP 3252406 B1 EP3252406 B1 EP 3252406B1
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Prior art keywords
natural gas
unit
liquefaction
current
stream
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EP17171766.3A
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English (en)
French (fr)
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EP3252406A1 (de
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Pierre COSTA DE BEAUREGARD
Michele MURINO
Delphine PICHOT
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • 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
    • F25J1/005—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 expansion of a gaseous refrigerant stream 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
    • F25J1/0002—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
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    • 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
    • F25J1/0027—Oxides of carbon, e.g. CO2
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    • 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
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    • 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
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    • F25J1/0203—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle
    • F25J1/0204—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR cycle
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    • 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
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    • 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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0236—Heat exchange integration providing refrigeration for different processes treating not the same feed stream
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    • 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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
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    • 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
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    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
    • F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
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    • 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
    • F25J2205/50—Processes or apparatus using other separation and/or other processing means using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/60—Natural gas or synthetic natural gas [SNG]
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    • 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
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    • F25J2215/04—Recovery of liquid products
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    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
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    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/80—Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.

Definitions

  • the present invention relates to a process for liquefying a stream of hydrocarbons such as natural gas in particular in a process for the production of liquefied natural gas and liquid CO 2 .
  • refrigerant streams are used to produce cold at different levels of a main heat exchanger by vaporizing against the stream of hydrocarbons to be liquefied (typically natural gas).
  • the present invention relates in particular to a thermal integration process between a natural gas liquefaction unit and a CO 2 purification / liquefaction unit.
  • natural gas can be stored and transported over long distances more easily in the liquid state than in gaseous form, because it occupies a smaller volume for a given mass and does not need to be stored at high pressure.
  • natural gas typically contains hydrocarbons and CO 2 (approximately 0.5% to 5% mol). To avoid freezing of the latter during the liquefaction of natural gas, it should be removed.
  • One way of removing CO 2 from the natural gas stream is, for example, an amine wash located upstream of a liquefaction cycle.
  • Amine washing separates the CO 2 from the feed gas by washing the natural gas stream with an amine solution in an absorption column.
  • the amine solution enriched in CO 2 is recovered in the tank of this absorption column and is regenerated at low pressure in a column for regenerating the amine distillation (or stripping in English).
  • This purification is carried out using a dedicated CO 2 purification unit requiring the installation of a dedicated refrigeration cycle (typically a refrigeration system operating with ammonia for example).
  • a dedicated refrigeration cycle typically a refrigeration system operating with ammonia for example.
  • the function of the so-called “cold group” refrigeration cycle consists in providing the cold necessary for the CO 2 purification / liquefaction process.
  • the condenser of the distillation column used in step 3 represents approximately 50% of the total cold requirements. This cold can be brought in via a dedicated refrigeration cycle (typically with ammonia or propane) possibly coupled with a water cooling system.
  • Document US2011 / 126451 A1 shows a process according to the preamble of claim 1.
  • the refrigeration production system represents a significant cost of the unit for purifying and liquefying CO 2 and adds complexity of implementation on the site of implementation of the process which represents a constraint.
  • An existing solution consists in dissociating the two units (liquefaction of natural gas and purification of CO 2 ) which requires the installation of two systems of production of frigories, one for the liquefaction unit of natural gas and one for the CO 2 purification unit.
  • the inventors of the present invention then developed a solution which makes it possible to solve the problem raised above, namely to minimize the investment in a system for producing frigories in the CO 2 purification / liquefaction unit and therefore d '' optimize investment costs while maintaining optimal efficiency for liquefying natural gas in the liquefaction unit.
  • thermal coupling is meant pooling of the means for producing frigories to ensure the thermal balance of the two units, typically a refrigeration cycle compressor, and possibly a turbine / blower system in the case of nitrogen cycle.
  • turbine / booster system is meant a turbine mechanically coupled (via a common shaft) to a single-stage compressor. The power generated through the turbine is directly transmitted to the single-stage compressor.
  • This thermal integration is materialized by the pooling of any column, heat exchanger, unit or other suitable arrangement (typically a heat exchanger) where currents related to the natural gas liquefaction process and currents related to the CO purification / liquefaction process 2 heat exchange.
  • the process which is the subject of the present invention makes it possible to dispense with the cold group initially necessary for liquefying the CO 2 and to extract the cold directly from the natural gas liquefier.
  • This thermal integration thus makes it possible to dispense with equipment in the CO 2 purification unit.
  • the proposed integration makes it possible to supply cold at the three necessary temperature levels.
  • the present invention also relates to a device for producing liquefied natural gas and liquefied CO 2 comprising a unit for treating a feed gas, producing at least one gas stream enriched in CO 2 and a stream of depleted natural gas. in CO 2 , and a natural gas liquefaction unit, said natural gas liquefaction unit comprising at least one main heat exchanger and a frigory production system characterized in that the frigory production system is capable of and designed for liquefying both the stream enriched in CO 2 from the processing unit and the stream of natural gas depleted in CO 2 flowing in the natural gas liquefaction unit, said natural gas liquefaction unit comprising at least one refrigeration cycle supplied by a refrigerant stream from the main exchanger.
  • the refrigeration requirement of a natural gas liquefaction unit is generally greater than the refrigeration requirement of a CO 2 purification / liquefaction unit, it is relevant to take advantage of the available capacity of the machines (compressors and / or turbine / boosters) of the natural gas liquefaction unit to fully or at least partially meet the refrigeration requirement of the CO 2 purification / liquefaction unit and in particular limit the investment in machinery of the purification / liquefaction unit of CO 2 .
  • the incremental investment to increase the liquefaction capacity of a hydrocarbon liquefier is much lower than the incremental investment to increase the liquid production capacity of a CO 2 purification / liquefaction unit.
  • the stream of hydrocarbons to be liquefied is generally a stream of natural gas obtained from natural gas fields, oil reservoirs or a domestic gas network distributed via pipelines.
  • the flow of natural gas is made up mostly of methane.
  • the feed stream comprises at least 80 mol% of methane.
  • natural gas contains quantities of heavier hydrocarbons than methane, such as for example ethane, propane, butane and pentane as well as certain aromatic hydrocarbons.
  • the natural gas stream also contains non-hydrocarbon products such as H 2 O, N 2 , CO 2 , H 2 S and other sulfur compounds, mercury and others.
  • the feed stream containing natural gas is therefore pretreated before being introduced into the heat exchanger.
  • This pretreatment includes the reduction and / or elimination of undesirable components such as CO 2 and H 2 S, or other steps such as pre-cooling and / or pressurization. Since these measures are well known to those skilled in the art, they are not further detailed here.
  • natural gas as used in the present application relates to any composition containing hydrocarbons including at least methane.
  • the heat exchanger can be any heat exchanger, any unit or other arrangement adapted to allow the passage of a certain number of flows, and thus allow a direct or indirect heat exchange between one or more lines of refrigerant, and a or more feed streams.
  • a natural gas feed stream 1 (considered flow rate 500,000 tonnes per year or approximately 60 tonnes per hour) containing CO 2 is introduced into a treatment unit 2 in which said stream 1 is separated into at least two gas streams 3 and 4.
  • the natural gas feed stream 1 contains for example from 0.1 to 5 mol% of CO 2 .
  • the first stream 3 is a stream of natural gas depleted in CO 2 .
  • the second stream 4 is a stream enriched in CO 2 .
  • the processing unit 2 is a unit which separates the CO 2 from the natural gas stream, for example a chemical absorption unit, in particular an amine washing unit (type MDEA, MEA, etc.) which makes it possible to produce CO 2 pure (or concentrated) at low pressure (typically slightly higher than pressure atmospheric).
  • a chemical absorption unit in particular an amine washing unit (type MDEA, MEA, etc.) which makes it possible to produce CO 2 pure (or concentrated) at low pressure (typically slightly higher than pressure atmospheric).
  • amine washing unit type MDEA, MEA, etc.
  • pure CO 2 is meant a stream containing more than 95 mol% of CO 2 on a dry basis.
  • the stream of natural gas 3 depleted in CO 2 is introduced into l main exchanger 8 of a natural gas liquefaction unit 5 in order to be liquefied.
  • the pressure of this gas stream is for example between 25 and 60 bar absolute.
  • the gas stream 3 contains between 30 ppm by volume and 500 ppm by volume of benzene, usually less than 100 ppm by volume.
  • the gas stream 3 is cooled by heat exchange in the heat exchanger 8 in contact with a refrigerant.
  • the heat exchanger 8 is supplied with at least one stream of refrigerant 8.
  • this stream may be composed of a stream of mixed refrigerant or nitrogen which provides the cold necessary for liquefying the stream of natural gas.
  • the refrigerant stream is sent to the high pressure exchanger (typically from 30 to 60 bar) and returned to low pressure (from 1 to 10 bar).
  • the recompression energy necessary for the operation of the refrigeration cycle is provided by a cycle compressor (possibly supplemented by a turbine / booster system as part of a nitrogen cycle)
  • the stream of natural gas 3 depleted in CO 2 introduced into the main exchanger 8 of a natural gas liquefaction unit 5 is for example liquefied according to the process described in the following lines.
  • the stream of natural gas cooled to a temperature between -20 ° C and -70 ° C, typically between -35 ° C and -40 ° C at the exchanger outlet 8 is introduced into a unit 11 for separating heavy hydrocarbons natural gas stream, for example a washing column in which the heavy products 10 are separated from natural gas.
  • heavy products is meant hydrocarbons having more than four carbon atoms and aromatic compounds including in particular benzene.
  • a gas stream no longer presenting a risk of freezing due to the presence of heavy hydrocarbons or aromatic derivatives (comprising typically less than 1 ppm by volume of benzene) is recovered to be introduced into a second section of the heat exchanger 8.
  • By heat exchange it is cooled to the desired temperature (typically -160 ° C) to be sent to a means for liquefied natural gas 14.
  • the stream of mixed refrigerant recovered at the outlet of the heat exchanger 8 is introduced into a phase separator pot producing a gas stream containing the light elements of the refrigerant at the top of the pot and a liquid stream 13 containing the heavy elements of the refrigerant in the tank of pot.
  • the refrigerant current circulates in closed cycle in the heat exchanger 8 in order to provide the cold necessary to liquefy said stream 3 of natural gas.
  • the liquefaction cycle 9 uses a refrigerant which can be a mixture of refrigerants typically chosen from nitrogen, methane, ethane, ethylene, propane, butane, pentane. It can be a cycle based on a refrigeration cycle consisting of a refrigerant or a mixture of several refrigerants.
  • a refrigerant stream is introduced into the system 9 for producing frigories from the liquefaction unit 5 via a compressor (and optionally via a compressor / booster system).
  • the second gas stream 4 enriched in CO 2 from the treatment unit 2 is compressed at medium pressure (typically 25 Bar abs), cooled, purified (elimination of all traces of H 2 O Hydrocarbons, sulfur derivatives in particular) then returned to a distillation column (stripping column) which separates the incondensables at the head from the concentrated liquid CO 2 15 recovered in the tank.
  • medium pressure typically 25 Bar abs
  • purified elimination of all traces of H 2 O Hydrocarbons, sulfur derivatives in particular
  • part of the liquid stream 13 containing the heavy elements of the refrigerant is extracted and is sent into circulation between the CO 2 purification / liquefaction unit 6 and the natural gas liquefaction unit 5.
  • a refrigerant cycle dedicated to the CO 2 purification / liquefaction unit 6 is avoided by increasing the power of the cycle dedicated to the liquefaction of natural gas (typically around 5%).

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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)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Carbon And Carbon Compounds (AREA)

Claims (7)

  1. Verfahren zur Erzeugung von verflüssigtem Erdgas (14) und flüssigem Kohlendioxid (CO2) (15), mindestens die folgenden Schritte umfassend:
    - Schritt a): Trennen eines Erdgasspeisegases (1), das Kohlenwasserstoffe und Kohlendioxid enthält, in einer Verarbeitungseinheit (2), in einen an CO2 angereicherten gasförmigen Strom (4) und einen an CO2 abgereicherten Erdgasstrom (3);
    - Schritt b): Verflüssigen des aus dem Schritt a) hervorgegangenen an CO2 abgereicherten Erdgastroms (3) in einer Erdgasverflüssigungseinheit (5), die mindestens einen Hauptwärmeaustauscher (8) und ein Frigorienerzeugungssystem (9) umfasst, wobei die Erdgasverflüssigungseinheit (5) mindestens einen Kühlzyklus umfasst, der von einem Kühlstrom gespeist wird;
    - Schritt c): gleichzeitiges Verflüssigen des aus dem Schritt a) hervorgegangenen an CO2 angereicherten gasförmigen Stroms (4) in einer CO2-Verflüssigunseinheit (6);
    dadurch gekennzeichnet, dass die zum Verflüssigen des an CO2 angereicherten gasförmigen Stroms (4) und zum Verflüssigen des Erdgases erforderliche Kälte vom Frigorienerzeugungssystem (9) der Erdgasverflüssigungseinheit (5) geliefert wird, und dadurch, dass die zum Verflüssigen des an CO2 angereicherten gasförmigen Stroms (4) erforderliche Kälte teilweise (13) aus dem Kältestrom stammt, der den Kühlzyklus der Erdgasverflüssigungseinheit (5) speist; dadurch gekennzeichnet, dass das Speisegas (1) 0,1 Mol-% bis 5 Mol-% CO2 umfasst, und dadurch gekennzeichnet, dass das Frigorienerzeugungssystem mindestens einen Kompressor und ein Turbinenverdichtersystem umfasst.
  2. Verfahren nach einem der vorstehenden Ansprüche, dadurch gekennzeichnet, dass der aus dem Schritt a) hervorgegangene an CO2 angereicherte gasförmige Strom (4) mindestens 95 Mol-% CO2 umfasst.
  3. Verfahren nach einem der vorstehenden Ansprüche, dadurch gekennzeichnet, dass vor dem Schritt b) das aus dem Schritt a) hervorgegangene Erdgas (3) in einer Vorverarbeitungseinheit (7) vorverarbeitet wird.
  4. Verfahren nach einem der vorstehenden Ansprüche, dadurch gekennzeichnet, dass die im Schritt a) eingesetzte Verarbeitungseinheit (2) eine Einheit zum Waschen mit Aminen ist.
  5. Verfahren nach einem der vorstehenden Ansprüche, dadurch gekennzeichnet, dass der aus dem Schritt a) hervorgegangene an CO2 angereicherte gasförmige Strom (4) vor dem Schritt c) gereinigt wird, wobei die zu dieser Reinigung erforderliche Kälte vom Frigorienerzeugungssystem der Erdgasverflüssigungseinheit (5) geliefert wird.
  6. Verfahren nach einem der vorstehenden Ansprüche, dadurch gekennzeichnet, dass der so gereinigte, an CO2 angereicherte Strom mindestens 99,5 Mol-% CO2 umfasst.
  7. Verfahren nach einem der vorstehenden Ansprüche, dadurch gekennzeichnet, dass der Kühlstrom (13), der den mindestens einen Kühlzyklus der Erdgasverflüssigungseinheit (5) speist, mindestens einen der Bestandteile enthält, die ausgewählt sind aus Stickstoff, Methan, Ethylen, Ethan, Propan, Ammoniak, Butan und Pentan.
EP17171766.3A 2016-06-02 2017-05-18 Verflüssigungsverfahren von kohlendioxid aus einem erdgasstrom Active EP3252406B1 (de)

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FR3141758A1 (fr) 2022-11-04 2024-05-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Appareil et procédé de production de gaz naturel refroidi et de CO2 liquide
FR3138196B3 (fr) 2022-11-04 2024-07-12 Air Liquide Appareil et procédé de production de gaz naturel refroidi et de CO2 liquide

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CA2317539C (en) * 1998-01-08 2003-08-19 Satish Reddy Autorefrigeration separation of carbon dioxide
JP4138399B2 (ja) * 2002-08-21 2008-08-27 三菱重工業株式会社 液化天然ガスの製造方法
RU2011106108A (ru) * 2008-07-18 2012-08-27 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. (NL) Двухстадийный способ производства очищенного газа
US20110126451A1 (en) * 2009-11-30 2011-06-02 Chevron U.S.A., Inc. Integrated process for converting natural gas from an offshore field site to liquefied natural gas and liquid fuel
CN103415752A (zh) * 2010-03-25 2013-11-27 曼彻斯特大学 制冷方法
EP2575996A4 (de) * 2010-06-03 2015-06-10 Ortloff Engineers Ltd Behandlung von kohlenwasserstoffgas
US10787615B2 (en) * 2014-01-28 2020-09-29 Praxair Technology, Inc. Method and system for treating a flow back fluid exiting a well site
DE102014005936A1 (de) * 2014-04-24 2015-10-29 Linde Aktiengesellschaft Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion

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