DE102012017653A1 - Process for liquefying a hydrocarbon-rich fraction - Google Patents
Process for liquefying a hydrocarbon-rich fraction Download PDFInfo
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- DE102012017653A1 DE102012017653A1 DE102012017653.8A DE102012017653A DE102012017653A1 DE 102012017653 A1 DE102012017653 A1 DE 102012017653A1 DE 102012017653 A DE102012017653 A DE 102012017653A DE 102012017653 A1 DE102012017653 A1 DE 102012017653A1
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- hydrocarbon
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- carbon dioxide
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- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 53
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 52
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 33
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 66
- 239000000203 mixture Substances 0.000 claims abstract description 45
- 239000003507 refrigerant Substances 0.000 claims abstract description 35
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 33
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 33
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000001816 cooling Methods 0.000 claims abstract description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000003345 natural gas Substances 0.000 claims abstract description 7
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 6
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims abstract description 5
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 7
- 230000000274 adsorptive effect Effects 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 4
- 230000008929 regeneration Effects 0.000 claims description 3
- 238000011069 regeneration method Methods 0.000 claims description 3
- -1 for example Chemical class 0.000 claims description 2
- 239000007788 liquid Substances 0.000 description 8
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 210000003918 fraction a Anatomy 0.000 description 4
- 210000000540 fraction c Anatomy 0.000 description 4
- 238000009434 installation Methods 0.000 description 3
- 241001295925 Gegenes Species 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000003949 liquefied natural gas Substances 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- BUHVIAUBTBOHAG-FOYDDCNASA-N (2r,3r,4s,5r)-2-[6-[[2-(3,5-dimethoxyphenyl)-2-(2-methylphenyl)ethyl]amino]purin-9-yl]-5-(hydroxymethyl)oxolane-3,4-diol Chemical compound COC1=CC(OC)=CC(C(CNC=2C=3N=CN(C=3N=CN=2)[C@H]2[C@@H]([C@H](O)[C@@H](CO)O2)O)C=2C(=CC=CC=2)C)=C1 BUHVIAUBTBOHAG-FOYDDCNASA-N 0.000 description 1
- 206010016352 Feeling of relaxation Diseases 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 210000002196 fr. b Anatomy 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 150000003464 sulfur compounds Chemical class 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
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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
- F25J1/003—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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- 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
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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
- F25J1/006—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
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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
- 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
- F25J1/0095—Oxides of carbon, e.g. CO2
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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
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- 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
- F25J1/0214—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 dual level refrigeration cascade with at least one MCR cycle
- F25J1/0215—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 dual level refrigeration cascade with at least one MCR cycle with one SCR cycle
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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
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
- F25J1/0277—Offshore use, e.g. during shipping
- F25J1/0278—Unit being stationary, e.g. on floating barge or fixed platform
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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
- F25J1/0243—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.
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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
- F25J1/0243—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.
- F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
- F25J1/0283—Gas turbine as the prime mechanical driver
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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
- F25J1/0243—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.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
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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
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- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/12—Particular process parameters like pressure, temperature, ratios
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Abstract
Es wird ein Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion, insbesondere von Erdgas, beschrieben, bei dem – die zu verflüssigende Kohlenwasserstoff-reiche Fraktion (A–B) im indirekten Wärmetausch gegen einen mehrstufigen Vorkühlkreislauf (1–9, 30–37, 40–47) abgekühlt wird (E1B–E4B), – das Kältemittel des Vorkühlkreislaufes zu wenigstens 95 Vol.-% aus Kohlendioxid besteht, – die abgekühlte Kohlenwasserstoff-reiche Fraktion (C) im indirekten Wärmetausch gegen einen Gemischkreislauf (10–19) verflüssigt und unterkühlt wird (E7, E8, E10), und – das Kältemittelgemisch des Gemischkreislaufes ausschließlich die Komponente(n) Stickstoff, Methan und/oder Ethan aufweist.A process for liquefying a hydrocarbon-rich fraction, in particular natural gas, is described, in which - the hydrocarbon-rich fraction (AB) to be liquefied in indirect heat exchange against a multi-stage pre-cooling circuit (1-9, 30-37, 40 –47) is cooled down (E1B – E4B), - the refrigerant in the pre-cooling circuit consists of at least 95% by volume of carbon dioxide, - the cooled hydrocarbon-rich fraction (C) is liquefied in indirect heat exchange against a mixture circuit (10–19) and is supercooled (E7, E8, E10), and - the refrigerant mixture of the mixture circuit only contains the component (s) nitrogen, methane and / or ethane.
Description
Die Erfindung betrifft ein Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion, insbesondere von Erdgas.The invention relates to a process for liquefying a hydrocarbon-rich fraction, in particular of natural gas.
Klassische Erdgasverflüssigungsanlagen im Kapazitätsbereich von 1 bis 5 Millionen Jahrestonnen (mtpa) LNG (Liquefied Natural Gas) basieren überwiegend auf einem Verfahren mit einer Propanvorkühlung und einem Gemischkreislauf zur Verflüssigung und Unterkühlung des Erdgases. Ein derartiges Verflüssigungsverfahren ist bspw. im
Es ist zudem bekannt, Kohlendioxid als Kältemittel zur Vorkühlung bei der Erdgasverflüssigung zu verwenden. Die tiefste einfach erreichbare Temperatur wird allerdings durch den Tripelpunkt des Kohlendioxids auf etwa –56°C beschränkt, da Kohlendioxid unterhalb dieser Temperatur in fester Form vorliegt und eine kontinuierliche Verfahrensführung erschwert.It is also known to use carbon dioxide as a refrigerant for pre-cooling in natural gas liquefaction. The lowest achievable temperature, however, is limited by the triple point of carbon dioxide to about -56 ° C, since carbon dioxide is below this temperature in solid form and makes continuous process management difficult.
Das für Landanlagen hervorragend geeignete, vorbeschriebene Verflüssigungsverfahren enthält sowohl in der Reinstoff-Vorkühlung als auch im Gemischkreislauf höhere Kohlenwasserstoffe, insbesondere Propan. Diese höheren Kohlenwasserstoffe bilden bei Leckagen in der Anlage Gaswolken mit einer Dichte größer als Luft. Dadurch kann es unter Umständen zur Bildung von gefährlichen, zündfähigen Luft-Kohlenwasserstoff-Gemischen kommen, die als erhebliches Sicherheitsrisiko eingestuft werden.The above-described liquefaction process, which is extremely suitable for land installations, contains higher hydrocarbons, in particular propane, both in the pure substance precooling and in the mixture circulation. These higher hydrocarbons form gas clouds with a density greater than air in the event of system leaks. This may result in the formation of hazardous, ignitable air-hydrocarbon mixtures, which are classified as a significant safety risk.
Bei schwimmenden Erdgasverflüssigungsanlagen (FLNG) versucht man daher, auf brennbare Kältemittel ganz zu verzichten – bspw. durch die Verwendung von Stickstoff, Kohlendioxid oder HFKWs – oder die Ausbreitung von lokalen Anlagenstörungen durch geeignete Sicherheitsabstände zwischen potentiellen Schadensquellen zu begrenzen. In allen Fällen steigen jedoch der Platzbedarf der Verflüssigungsanlage und damit die Investitionskosten durch die erforderliche Vergrößerung des vergleichsweise teuren Schiffsrumpfes. Dies ist beispielhaft bei sog. N2-Expander-Verfahren auf den vergleichsweise niedrigen thermodynamischen Wirkungsgrad zurückzuführen, der für eine gegebene Verflüssigungsleistung größere Verdichter und Antriebe erfordert.Floating natural gas liquefaction plants (FLNGs) therefore try to completely dispense with flammable refrigerants - for example, by using nitrogen, carbon dioxide or HFCs - or to limit the spread of local plant faults by means of suitable safety margins between potential sources of damage. In all cases, however, increase the space required by the liquefaction plant and thus the investment costs by the required increase in the relatively expensive hull. This is exemplified by the so-called N 2 expander method due to the comparatively low thermodynamic efficiency, which requires larger compressors and drives for a given liquefaction performance.
Aufgabe der vorliegenden Erfindung ist es, ein gattungsgemäßes Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion anzugeben, das aufgrund einer kompakteren Bauweise einen gegenüber den gegenwärtig bei FLNG-Anlagen realisierten Verflüssigungsverfahren geringeren Platzbedarf aufweist. Zudem soll das Verfahren den vorgegebenen Sicherheitsanforderungen genügen.Object of the present invention is to provide a generic method for liquefying a hydrocarbon-rich fraction, which has a smaller compared to the currently implemented in FLNG plants liquefaction due to a more compact design. In addition, the method should meet the specified safety requirements.
Zur Lösung dieser Aufgabe wird ein Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion vorgeschlagen, bei dem
- – die zu verflüssigende Kohlenwasserstoff-reiche Fraktion im indirekten Wärmetausch gegen einen mehrstufigen Vorkühlkreislauf abgekühlt wird, das Kältemittel des Vorkühlkreislaufes zu wenigstens 95 Vol.-% aus Kohlendioxid besteht,
- – die abgekühlte Kohlenwasserstoff-reiche Fraktion im indirekten Wärmetausch gegen einen Gemischkreislauf verflüssigt und unterkühlt wird, und das Kältemittelgemisch des Gemischkreislaufes ausschließlich die Komponenten Stickstoff, Methan und/oder Ethan aufweist.
- - The hydrocarbon-rich fraction to be liquefied is cooled in indirect heat exchange against a multi-stage precooling, the refrigerant of the precooling circuit consists of at least 95 vol .-% of carbon dioxide,
- - The cooled hydrocarbon-rich fraction is liquefied and subcooled in indirect heat exchange against a mixture cycle, and the refrigerant mixture of the mixture cycle exclusively the components nitrogen, methane and / or ethane.
Das erfindungsgemäße Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion zeichnet sich dadurch aus, dass ein mehrstufiger Einkomponenten-Vorkühlkreislauf und ein Gemischkreislauf, der der Verflüssigung und Unterkühlung der Kohlenwasserstoff-reichen Fraktion dient, kombiniert werden, wobei das Kältemittel des Vorkühlkreislaufes zu wenigstens 95 Vol.-%, vorzugsweise zu wenigstens 99 Vol.-%, aus Kohlendioxid besteht, während das Kältemittelgemisch des Gemischkreislaufes ausschließlich die Komponenten Stickstoff, Methan und/oder Ethan aufweist. Auf die Verwendung von höheren Kohlenwasserstoffen – hierunter seien C3+-Kohlenwasserstoffe zu verstehen – wird vollständig verzichtet. Mittels der erfindungsgemäßen Verfahrensweise können FLNG-Anlagen – ohne Abstriche bei der Sicherheit in Kauf nehmen zu müssen – kompakter und damit kostengünstiger realisiert werden.The process according to the invention for liquefying a hydrocarbon-rich fraction is characterized in that a multistage one-component pre-cooling circuit and a mixture circuit, which serves the liquefaction and subcooling of the hydrocarbon-rich fraction, are combined, wherein the refrigerant of the precooling circuit to at least 95 vol. -%, preferably at least 99 vol .-%, consists of carbon dioxide, while the refrigerant mixture of the mixture cycle exclusively the components nitrogen, methane and / or ethane. The use of higher hydrocarbons - this is C 3+ hydrocarbons to understand - is completely eliminated. By means of the procedure according to the invention, FLNG installations can be realized more compactly and thus more cost-effectively without having to compromise on safety.
Im Vergleich zu optimierten Verflüssigungsverfahren, die üblicherweise bei Landanlagen zur Anwendung kommen, weist das erfindungsgemäße Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion einen höheren Energieverbrauch auf. Der Energiemehrverbrauch beträgt ca. 7%, in ungünstigen Anwendungsfällen maximal 10%.In comparison to optimized liquefaction processes, which are usually used in land installations, the inventive method for liquefying a hydrocarbon-rich fraction has a higher energy consumption. The energy consumption is about 7%, in unfavorable applications, a maximum of 10%.
Weitere vorteilhafte Ausgestaltungen des erfindungsgemäßen Verfahrens zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion sind dadurch gekennzeichnet, dass
- – das in dem Vorkühlkreislauf zirkulierende Kohlendioxid in zwei getrennten Verdichtergehäusen komprimiert wird, wobei der Ausgangsdruck des Niederdruckgehäuses unterhalb des kritischen Drucks von Kohlendioxid liegt,
- – der Ausgangsdruck des Hochdruckgehäuses bei einem Enddruck von wenigstens 90 bar, vorzugsweise wenigstens 100 bar betrieben wird,
- – das in dem Gemischkreislauf zirkulierende Kältemittelgemisch auf einen Druck oberhalb seines kritischen Druckes verdichtet wird,
- – die Temperatur(en) der zu verflüssigenden Kohlenwasserstoff-reichen Fraktion, des Kohlendioxids und/oder des Kältemittelgemisches derart eingestellt werden, dass sich die Antriebsleistungen der Verdichter des Vorkühlkreislaufes und des oder der Verdichter des Gemischkreislaufes um maximal 10%, vorzugsweise um maximal 5% unterscheiden,
- – sofern die zu verflüssigende Kohlenwasserstoff-reiche Fraktion vor ihrer Abkühlung und Verflüssigung einer adsorptiven Wasser-Abtrennung unterworfen wird, die verflüssigte Kohlenwasserstoff-reiche Fraktion entspannt, die dabei entstehende gasförmige Fraktion auf den Druck der zu verflüssigenden Kohlenwasserstoff-reichen Fraktion verdichtet und dieser zugeführt wird, wobei die verdichtete gasförmige Fraktion vor ihrer Zuführung der Regenerierung des oder der Trockner der adsorptiven Wasser-Abtrennung dient,
- – das Kältemittel des Vorkühlkreislaufes zu wenigstens 99 Vol.-% aus Kohlendioxid besteht, und
- – aus der vorgekühlten, zu verflüssigenden Kohlenwasserstoff-reichen Fraktion höhere und ggf. gefriergefährdete Kohlenwasserstoffe, wie bspw. Benzol, abgetrennt werden.
- The carbon dioxide circulating in the precooling circuit is compressed in two separate compressor housings, the outlet pressure of the low-pressure housing being below the critical pressure of carbon dioxide,
- The outlet pressure of the high-pressure housing is operated at a final pressure of at least 90 bar, preferably at least 100 bar,
- The refrigerant mixture circulating in the mixture circuit is compressed to a pressure above its critical pressure,
- - The temperature (s) of the hydrocarbon-rich fraction to be liquefied, the carbon dioxide and / or the refrigerant mixture such that the driving powers of the compressors of the precooling circuit and of the compressor (s) of the mixture circuit are differentiated by a maximum of 10%, preferably by a maximum of 5%,
- - If the liquefied hydrocarbon-rich fraction is subjected before being cooled and liquefied adsorptive water separation, the liquefied hydrocarbon-rich fraction relaxed, the resulting gaseous fraction is compressed to the pressure of the liquefied hydrocarbon-rich fraction and this is supplied wherein the compressed gaseous fraction prior to its delivery serves for the regeneration of the adsorptive water separator (s),
- - The refrigerant of the pre-cooling circuit consists of at least 99 vol .-% of carbon dioxide, and
- - From the precooled, to be liquefied hydrocarbon-rich fraction higher and possibly gefriergefährdete hydrocarbons, such as, benzene, are separated.
Das erfindungsgemäße Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion sowie weitere vorteilhafte Ausgestaltungen desselben seien nachfolgend anhand der in den
Bei der in der
Die derart vorbehandelte Kohlenwasserstoff-reiche Fraktion B wird anschließend in den Wärmetauschern E1B bis E4B gegen das Kältemittel des Vorkühlkreislaufes, auf den im Folgenden näher eingegangen werden wird, abgekühlt. Im Wärmetauscher E7/E8 wird die abgekühlte Kohlenwasserstoff-reiche Fraktion C im indirekten Wärmetausch gegen das Kältemittelgemisch des Gemischkreislaufes, auf den im Folgenden noch näher eingegangen werden wird, verflüssigt (Wärmetauscherabschnitt E7) und unterkühlt (Wärmetauscherabschnitt E8). Am kalten Ende des Wärmetauschers E7/E8 wird die verflüssigte und unterkühlte Kohlenwasserstoff-reiche Fraktion D abgezogen und beispielsweise einem atmosphärischen Lagertank, der in der
Der bereits erwähnte Vorkühlkreislauf, in dem als Kältemittel erfindungsgemäß Kohlendioxid zirkuliert, weist bei der in der
Das auf den gewünschten Enddruck verdichtete Kohlendioxid
Der Hauptteil des flüssigen Kohlendioxids
Dazu werden die beiden Teilströme über die Leitungsabschnitte
Das mittels des Verdichters bzw. der Verdichtereinheit C2 auf den gewünschten Kreislaufdruck verdichtete Kältemittelgemisch des Gemischkreislaufes
Die im Abscheider D2 anfallende gasförmige Fraktion des Kältemittelgemisches
Das Inventar flüssiger Kohlenwasserstoffe im Gemischkreislauf beschränkt sich im Wesentlichen auf den Abscheider D2, die Leitungen
Das erfindungsgemäße Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion weiterbildend wird vorgeschlagen, dass die Temperatur(en) der zu verflüssigenden Kohlenwasserstoff-reichen Fraktion, des Kohlendioxids und/oder des Kältemittelgemisches derart eingestellt werden, dass sich die Antriebsleistungen der Verdichter des Vorkühlkreislaufes und des oder der Verdichter des Gemischkreislaufes um maximal 10%, vorzugsweise um maximal 5% unterscheiden. Mittels dieser vorteilhaften Verfahrensweise wird erreicht, dass die für den Betrieb der Verdichter bzw. Verdichtereinheiten C1A/C1B und C2 erforderlichen Antriebe GT identisch sein können.The inventive method for further liquefying a hydrocarbon-rich fraction is proposed that the temperature (s) of the hydrocarbon-rich fraction to be liquefied, the carbon dioxide and / or the refrigerant mixture are adjusted such that the drive power of the compressors of the pre-cooling circuit and the or the compressor of the mixture cycle by a maximum of 10%, preferably differ by a maximum of 5%. By means of this advantageous procedure it is achieved that the drives GT required for the operation of the compressors or compressor units C1A / C1B and C2 can be identical.
Gemäß einer weiteren vorteilhaften Ausgestaltung des erfindungsgemäßen Verfahrens zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion wird das in dem Gemischkreislauf zirkulierende Kältemittelgemisch auf einen Druck oberhalb seines kritischen Druckes verdichtet. Somit können unerwünschte Verteilungsprobleme der Phasen Gas und Flüssigkeit vermieden werden, die insbesondere bei einer schwimmenden Anlage (FLNG) aufgrund des Seeganges auftreten können.According to a further advantageous embodiment of the method according to the invention for liquefying a hydrocarbon-rich fraction, the refrigerant mixture circulating in the mixture cycle is compressed to a pressure above its critical pressure. Thus, unwanted distribution problems of the phases of gas and liquid can be avoided, which can occur in particular in a floating system (FLNG) due to the sea state.
Aufgrund der vorbeschriebenen, vorteilhaften Verfahrensweise erübrigt sich der in der
In der
Das gegen das Kältemittel des Vorkühlkreislaufes abgekühlte Kältemittelgemisch
ZITATE ENTHALTEN IN DER BESCHREIBUNG QUOTES INCLUDE IN THE DESCRIPTION
Diese Liste der vom Anmelder aufgeführten Dokumente wurde automatisiert erzeugt und ist ausschließlich zur besseren Information des Lesers aufgenommen. Die Liste ist nicht Bestandteil der deutschen Patent- bzw. Gebrauchsmusteranmeldung. Das DPMA übernimmt keinerlei Haftung für etwaige Fehler oder Auslassungen.This list of the documents listed by the applicant has been generated automatically and is included solely for the better information of the reader. The list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions.
Zitierte PatentliteraturCited patent literature
- US 3763658 [0002] US 3763658 [0002]
Claims (8)
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
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DE102012017653.8A DE102012017653A1 (en) | 2012-09-06 | 2012-09-06 | Process for liquefying a hydrocarbon-rich fraction |
AU2013211458A AU2013211458A1 (en) | 2012-09-06 | 2013-07-30 | Process for liquefying a hydrocarbon-rich fraction |
BR102013022719-6A BR102013022719A2 (en) | 2012-09-06 | 2013-09-05 | PROCESS TO LIQUIDATE HYDROCARBON FRACTION |
US14/019,998 US20140060111A1 (en) | 2012-09-06 | 2013-09-06 | Process for liquefying a hydrocarbon-rich fraction |
Applications Claiming Priority (1)
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DE102012017653.8A DE102012017653A1 (en) | 2012-09-06 | 2012-09-06 | Process for liquefying a hydrocarbon-rich fraction |
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DE102012017653A1 true DE102012017653A1 (en) | 2014-03-06 |
Family
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DE102012017653.8A Withdrawn DE102012017653A1 (en) | 2012-09-06 | 2012-09-06 | Process for liquefying a hydrocarbon-rich fraction |
Country Status (4)
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US (1) | US20140060111A1 (en) |
AU (1) | AU2013211458A1 (en) |
BR (1) | BR102013022719A2 (en) |
DE (1) | DE102012017653A1 (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2017051021A1 (en) | 2015-09-24 | 2017-03-30 | Linde Aktiengesellschaft | Method for cooling, liquefying or processing a gas and corresponding refrigerant mixture |
EP3489594A1 (en) * | 2017-11-27 | 2019-05-29 | Air Products And Chemicals, Inc. | Method and system for cooling a hydrocarbon stream |
EP3489601A1 (en) * | 2017-11-27 | 2019-05-29 | Air Products And Chemicals, Inc. | Method and system for cooling a hydrocarbon stream |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CA3000821A1 (en) * | 2015-10-06 | 2017-04-13 | Exxonmobil Upstream Research Company | Consolidated refrigeration and liquefaction module in a hydrocarbon processing plant |
CN110173959B (en) * | 2019-05-15 | 2021-04-02 | 挪威极地航运公司 | Boil-off gas reliquefaction recovery system |
US11827317B1 (en) * | 2022-05-04 | 2023-11-28 | Storeco2 Uk Limited | Carbon dioxide transport and sequestration marine vessel |
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US3763658A (en) | 1970-01-12 | 1973-10-09 | Air Prod & Chem | Combined cascade and multicomponent refrigeration system and method |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB0006265D0 (en) * | 2000-03-15 | 2000-05-03 | Statoil | Natural gas liquefaction process |
WO2005028975A2 (en) * | 2003-09-23 | 2005-03-31 | Statoil Asa | Natural gas liquefaction process |
GB2462125B (en) * | 2008-07-25 | 2012-04-04 | Dps Bristol Holdings Ltd | Production of liquefied natural gas |
-
2012
- 2012-09-06 DE DE102012017653.8A patent/DE102012017653A1/en not_active Withdrawn
-
2013
- 2013-07-30 AU AU2013211458A patent/AU2013211458A1/en not_active Abandoned
- 2013-09-05 BR BR102013022719-6A patent/BR102013022719A2/en not_active Application Discontinuation
- 2013-09-06 US US14/019,998 patent/US20140060111A1/en not_active Abandoned
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
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US3763658A (en) | 1970-01-12 | 1973-10-09 | Air Prod & Chem | Combined cascade and multicomponent refrigeration system and method |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2017051021A1 (en) | 2015-09-24 | 2017-03-30 | Linde Aktiengesellschaft | Method for cooling, liquefying or processing a gas and corresponding refrigerant mixture |
EP3489594A1 (en) * | 2017-11-27 | 2019-05-29 | Air Products And Chemicals, Inc. | Method and system for cooling a hydrocarbon stream |
EP3489601A1 (en) * | 2017-11-27 | 2019-05-29 | Air Products And Chemicals, Inc. | Method and system for cooling a hydrocarbon stream |
RU2748319C2 (en) * | 2017-11-27 | 2021-05-24 | Эр Продактс Энд Кемикалз, Инк. | Method for cooling the hydrocarbon feed stream and installation for cooling the hydrocarbon feed stream cooling the hydrocarbon stream |
US11624555B2 (en) | 2017-11-27 | 2023-04-11 | Air Products And Chemicals, Inc. | Method and system for cooling a hydrocarbon stream |
Also Published As
Publication number | Publication date |
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US20140060111A1 (en) | 2014-03-06 |
AU2013211458A1 (en) | 2014-03-20 |
BR102013022719A2 (en) | 2014-10-29 |
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