NO20111212A1 - Condensation of natural gas - Google Patents
Condensation of natural gas Download PDFInfo
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- NO20111212A1 NO20111212A1 NO20111212A NO20111212A NO20111212A1 NO 20111212 A1 NO20111212 A1 NO 20111212A1 NO 20111212 A NO20111212 A NO 20111212A NO 20111212 A NO20111212 A NO 20111212A NO 20111212 A1 NO20111212 A1 NO 20111212A1
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- Prior art keywords
- heat exchanger
- nitrogen
- feed fraction
- condensed
- fraction
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 14
- 239000003345 natural gas Substances 0.000 title claims abstract description 6
- 230000005494 condensation Effects 0.000 title claims description 22
- 238000009833 condensation Methods 0.000 title claims description 22
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 114
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 57
- 238000000034 method Methods 0.000 claims abstract description 46
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 13
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims abstract description 13
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 12
- 238000000926 separation method Methods 0.000 claims abstract description 5
- 238000009835 boiling Methods 0.000 claims description 12
- 238000005057 refrigeration Methods 0.000 claims 1
- 238000001816 cooling Methods 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 9
- 230000001105 regulatory effect Effects 0.000 description 4
- 239000003507 refrigerant Substances 0.000 description 3
- 239000002826 coolant Substances 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 230000035882 stress Effects 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000010943 off-gassing Methods 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008646 thermal stress Effects 0.000 description 1
Classifications
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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
- F25J1/005—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
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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
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/007—Primary atmospheric gases, mixtures thereof
- F25J1/0072—Nitrogen
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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
- F25J1/0203—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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- 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
- F25J1/0221—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 the cold stored in an external cryogenic component in an open refrigeration loop
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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
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
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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
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
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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
- F25J1/0262—Details of the cold heat exchange system
- F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
- F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
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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.
- F25J1/0285—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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- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
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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
- 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
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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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
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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
- 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
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
- F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
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- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Fremgangsmåte for å kondensere en hydrokarbonrik tilførselsfraksjon, fortrinnsvis naturgass, mot en nitrogenkjølesyklus, hvor tilførselsfraksjonen avkjøles mot gassformig nitrogen som skal oppvarmes, og tilførselsfraksjonen kondenseres mot flytende nitrogen som skal fordampes. Oppfinnelsen er kjennetegnet ved at tilførselsfraksjonen blir avkjølt og kondensert i en minst tretrinns varmevekslerprosess (E1a-E1c); i den første seksjon av varmevekslerprosessen (E1a) blir tilførselsfraksjonen (1) avkjølt mot overhetet, gassformig nitrogen (9) i et slikt omfang at det oppnås en hovedsakelig fullstendig fraskillelse (D2) av de relativt tunge komponentene (2'); i den andre seksjon av varmevekslerprosessen blir tilførselsfraksjonen (2) som er befridd for relativt tunge komponenter, delvis kondensert mot gassformig nitrogen som skal overhetes; og i den tredje seksjon av varmevekslerprosessen (E1c) blir tilførselsfraksjonen (2) kondensert mot nitrogen som skal bli delvis fordampet (8).A process for condensing a hydrocarbon-rich feed fraction, preferably natural gas, against a nitrogen cooling cycle, wherein the feed fraction is cooled against gaseous nitrogen to be heated and the feed fraction condensed against liquid nitrogen to be evaporated. The invention is characterized in that the feed fraction is cooled and condensed in a at least three-stage heat exchanger process (E1a-E1c); in the first section of the heat exchanger process (E1a), the feed fraction (1) is cooled against superheated gaseous nitrogen (9) to such an extent that a substantially complete separation (D2) of the relatively heavy components (2 ') is achieved; in the second section of the heat exchanger process, the feed fraction (2) liberated for relatively heavy components is partially condensed against gaseous nitrogen to be superheated; and in the third section of the heat exchanger process (E1c), the feed fraction (2) is condensed against nitrogen to be partially evaporated (8).
Description
Oppfinnelsen angår en fremgangsmåte for kondensasjon av en hydrokarbonrik tilførselsfraksjon, fortrinnsvis naturgass, mot en nitrogenkjølesyklus hvor tilførsels-fraksjonen avkjøles mot gassformig nitrogen som skal oppvarmes, og tilførselsfraksjonen kondenseres mot flytende nitrogen som skal fordampes. The invention relates to a method for condensing a hydrocarbon-rich feed fraction, preferably natural gas, against a nitrogen cooling cycle where the feed fraction is cooled against gaseous nitrogen to be heated, and the feed fraction is condensed against liquid nitrogen to be evaporated.
Hydrokarbonrike gasser, særlig naturgasser, kondenseres kommersielt i et kapasitetsområde fra 10 til 30 000 tonn LNG pr. døgn (tato). I anlegg med middels kapasitet - med dette menes kondensasjonsprosesser med en kapasitet mellom 300 og 3000 tato LNG - og stor kapasitet - med dette menes kondensasjonsprosesser med en kapasitet mellom 3000 og 30 000 tato LNG - forsøker fagfolk på området å optimalisere driftskostnadene ved hjelp av høy effektivitet. I tilfellet mindre anlegg - med dette menes kondensasjonsprosesser med en kapasitet mellom 10 og 300 tato LNG - er derimot lave kapitalkostnader i forgrunnen. I slike anlegg er kapitalkostnadsandelen for et dedikert kjøleanlegg hvor arbeidsmediet som anvendes er f.eks. nitrogen eller en nitrogen-hydro-karbonblanding, betydelig. Derfor blir generering av kulde i kondensasjonsanlegget om mulig utelatt, og et egnet kjølemedium blir importert. Vanligvis anvendes i dette tilfellet flytende nitrogen som etter anvendelse som kjølemiddel slippes ut i atmosfæren i gassformig tilstand. Dersom et nærliggende separasjonsanlegg kan levere billige ubrukte produktmengder flytende nitrogen, er dette konseptet for små kondensasjonsanlegg absolutt kommersielt brukbart. Hydrocarbon-rich gases, especially natural gases, are commercially condensed in a capacity range from 10 to 30,000 tonnes of LNG per year. day (tato). In facilities with medium capacity - by this is meant condensation processes with a capacity between 300 and 3,000 tato LNG - and large capacity - by this is meant condensation processes with a capacity between 3,000 and 30,000 tato LNG - professionals in the area try to optimize operating costs using high efficiency. In the case of smaller plants - by this is meant condensation processes with a capacity of between 10 and 300 tato LNG - low capital costs are, on the other hand, in the foreground. In such plants, the capital cost share is for a dedicated cooling plant where the working medium used is e.g. nitrogen or a nitrogen-hydrocarbon mixture, significantly. Therefore, the generation of cold in the condensation plant is omitted if possible, and a suitable refrigerant is imported. Liquid nitrogen is usually used in this case, which after use as a refrigerant is released into the atmosphere in a gaseous state. If a nearby separation plant can supply cheap unused product quantities of liquid nitrogen, this concept for small condensing plants is certainly commercially viable.
Av kostnadsårsaker blir det i små flytende, nitrogenavkjølte anlegg generelt anvendt varmevekslere av slagloddede aluminiumsplater. Disse innretninger er imidlertid følsomme for slike termiske spenninger som kan oppstå ved f.eks. en for stor tilførsel av kjølemiddel og/eller store temperaturforskjeller mellom varme og kalde prosesstrømmer. De resulterende mekaniske spenninger kan lede til skade på disse innretninger. For cost reasons, heat exchangers made of brazed aluminum plates are generally used in small liquid, nitrogen-cooled plants. These devices are, however, sensitive to such thermal stresses as may arise from e.g. an excessive supply of coolant and/or large temperature differences between hot and cold process streams. The resulting mechanical stresses can lead to damage to these devices.
I tillegg må det under driften av kondensasjonsprosessen passes nøye på at tilførselsfraksjonen ikke faller under frysetemperaturen. Stivnepunktet for metan på -182 °C er klart høyere enn kokepunktstemperaturen for nitrogen ved atmosfæretrykk, som er -196 °C. Dersom anlegget fryser, medfører det alltid en uønsket driftsfeil og kan i tillegg ha en varig skade som konsekvens. In addition, during operation of the condensation process, care must be taken to ensure that the feed fraction does not fall below the freezing temperature. The solidification point of methane at -182 °C is clearly higher than the boiling point temperature of nitrogen at atmospheric pressure, which is -196 °C. If the system freezes, it always causes an unwanted operating error and can also have permanent damage as a consequence.
En fremgangsmåte av den aktuelle type for kondensasjon av en hydrokarbonrik tilførselsfraksjon, er kjent fra US 5 390 499. Denne fremgangsmåten er særlig egnet for anlegg med liten kapasitet, som forklart innledningsvis. Ved kondensasjons-metoden beskrevet i US 5 390 499 blir gassen som skal kondenseres, avkjølt og kondensert mot nitrogen i to separate varmevekslere. I dette tilfellet blir det flytende, lavtkokende nitrogen fullstendig fordampet i den andre varmeveksleren og oppvarmet til en temperatur hvor forholdsvis tunge rågasskomponenter kan tas ut i flytende tilstand ved hjelp av en separator fra gassen som skal kondenseres. I en utførelse av fremgangsmåten beskrevet i US 5 390 499, kan imidlertid punktet hvor nitrogenet fordamper fullstendig variere be tydelig avhengig av belastning. Dette kan lede til uønskede prosessbetingelser som har de ovennevnte ulemper som konsekvens. A method of the relevant type for the condensation of a hydrocarbon-rich feed fraction is known from US 5 390 499. This method is particularly suitable for plants with a small capacity, as explained at the beginning. In the condensation method described in US 5 390 499, the gas to be condensed is cooled and condensed against nitrogen in two separate heat exchangers. In this case, the liquid, low-boiling nitrogen is completely vaporized in the second heat exchanger and heated to a temperature where relatively heavy raw gas components can be removed in a liquid state by means of a separator from the gas to be condensed. In an embodiment of the method described in US 5,390,499, however, the point at which the nitrogen evaporates completely can vary significantly depending on the load. This can lead to undesirable process conditions which have the above-mentioned disadvantages as a consequence.
Det er et mål med den foreliggende oppfinnelse å spesifisere en fremgangsmåte av aktuell type for kondensasjon av en hydrokarbonrik tilførselsfraksjon, hvor det med fremgangsmåten unngås de ovennevnte ulemper og det spesielt tilveiebringes en fremgangsmåte som er robust mot driftsfeil og skade. It is an aim of the present invention to specify a method of the current type for the condensation of a hydrocarbon-rich feed fraction, where the method avoids the above-mentioned disadvantages and in particular provides a method which is robust against operating errors and damage.
For å nå dette mål foreslås en fremgangsmåte for kondensasjon av en hydrokarbonrik tilførselsfraksjon, kjennetegnet ved at In order to achieve this goal, a method is proposed for the condensation of a hydrocarbon-rich feed fraction, characterized by that
- tilførselsfraksjonen blir avkjølt og kondensert i en minst tretrinns varmevekslerprosess, - i den første seksjon av varmevekslerprosessen blir tilførselsfraksjonen avkjølt mot overhetet, gassformig nitrogen i et slikt omfang at det oppnås en hovedsakelig fullstendig separasjon av de relativt tunge komponentene, - i den andre seksjon av varmevekslerprosessen blir tilførselsfraksjonen, som er befridd for de relativt tunge komponentene, delvis kondensert mot gassformig nitrogen som skal overhetes, og - i den tredje seksjon av varmevekslerprosessen blir tilførselsfraksjonen kondensert mot nitrogen som skal bli delvis fordampet. - the feed fraction is cooled and condensed in at least a three-stage heat exchanger process, - in the first section of the heat exchanger process, the feed fraction is cooled against superheated, gaseous nitrogen to such an extent that an essentially complete separation of the relatively heavy components is achieved, - in the second section of the heat exchanger process, the feed fraction, which is freed of the relatively heavy components, is partially condensed to gaseous nitrogen to be superheated, and - in the third section of the heat exchanger process, the feed fraction is condensed to nitrogen to be partially vaporized.
Uttrykket "tunge komponenter" vil heretter bety hydrokarboner fra etan. The term "heavy components" will hereafter mean hydrocarbons from ethane.
Ytterligere fordelaktige utførelsesformer av fremgangsmåten ifølge oppfinnelsen for kondensasjon av en hydrokarbonrik tilførselsfraksjon, er kjennetegnet ved at Further advantageous embodiments of the method according to the invention for condensation of a hydrocarbon-rich feed fraction are characterized in that
- tretrinnsvarmevekslerprosessen oppnås i én eller flere varmevekslere, - the three-stage heat exchanger process is achieved in one or more heat exchangers,
- kondensasjonstrykket i tilførselsfraksjonen som er befridd for relativt tunge komponenter, justeres til verdier mellom 1 og 15 bara, fortrinnsvis mellom 1 og 8 bara, og - kokepunktstrykket for gassformig nitrogen som skal overhetes, justeres til verdier mellom 5 og 30 bara, fortrinnsvis mellom 10 og 20 bara. - the condensation pressure in the feed fraction which is freed from relatively heavy components is adjusted to values between 1 and 15 bara, preferably between 1 and 8 bara, and - the boiling point pressure for gaseous nitrogen to be superheated is adjusted to values between 5 and 30 bara, preferably between 10 and 20 bara.
Fremgangsmåten ifølge oppfinnelsen for kondensasjon av en hydrokarbonrik tilførselsfraksjon, og andre fordelaktige utførelsesformer av den samme, skal beskrives mer detaljert nedenfor med henvisning til den eksemplifiserte utførelsesformen vist på figuren. The method according to the invention for the condensation of a hydrocarbon-rich feed fraction, and other advantageous embodiments of the same, shall be described in more detail below with reference to the exemplified embodiment shown in the figure.
Den hydrokarbonrike tilførselsfraksjon som skal kondenseres, tilføres via ledning 1 til en varmeveksler El. Denne er oppdelt i tre seksjoner eller trinn a til c. Grensene mellom disse seksjoner eller trinn er vist med de to stiplede linjene. I den varmeste seksjon a av varmeveksleren El blir den hydrokarbonrike tilførselsfraksjon avkjølt mot overhetet, gassformig nitrogen som tilføres via ledning 9 til varmeveksleren El i et slikt omfang at det er mulig å skille de tunge komponentene fra tilførselsfraksjonen i en separator D2 nedstrøms varmeveksleren El. For dette formål blir den avkjølte tilførselsfraksjon tilført fra varmeveksleren El via ledning 1' til separatoren D2. Fra bunnfasen i denne blir via ledning 2', hvor det er anordnet en ventil VI, uønskede tunge komponenter tatt ut i væskeform og frigjort fra prosessen. The hydrocarbon-rich feed fraction to be condensed is supplied via line 1 to a heat exchanger El. This is divided into three sections or stages a to c. The boundaries between these sections or stages are shown with the two dashed lines. In the hottest section a of the heat exchanger El, the hydrocarbon-rich feed fraction is cooled against superheated, gaseous nitrogen which is supplied via line 9 to the heat exchanger El to such an extent that it is possible to separate the heavy components from the feed fraction in a separator D2 downstream of the heat exchanger El. For this purpose, the cooled supply fraction is supplied from the heat exchanger El via line 1' to the separator D2. From the bottom phase in this, via line 2', where a valve VI is arranged, unwanted heavy components are taken out in liquid form and released from the process.
I stedet for separatoren D2 vist på figuren, kan det anvendes en rektifika-sjonskolonne for å oppnå en presis separasjon av relativt tunge komponenter eller høyere hydrokarboner fra tilførselsfraksjonen. Instead of the separator D2 shown in the figure, a rectification column can be used to achieve a precise separation of relatively heavy components or higher hydrocarbons from the feed fraction.
Ved toppen av separatoren D2 blir, via ledning 2, tilførselsfraksjonen som er befridd for tunge komponenter, tatt ut og tilført til den andre seksjon b i varmeveksleren El. I denne blir tilførselsfraksjonen som er befridd for tunge komponenter, delvis kondensert mot gassformig nitrogen som skal overhetes 9. Deretter blir, i det tredje trinn c av varmeveksleren El, tilførselsfraksjonen fullstendig kondensert mot nitrogen som skal bli delvis fordampet, hvilket tilføres til varmeveksleren El via ledning 8. At the top of the separator D2, via line 2, the supply fraction that is freed of heavy components is taken out and supplied to the second section b of the heat exchanger El. In this, the feed fraction freed from heavy components is partially condensed against gaseous nitrogen to be superheated 9. Then, in the third stage c of the heat exchanger El, the feed fraction is completely condensed against nitrogen to be partially evaporated, which is fed to the heat exchanger El via wire 8.
Den kondenserte tilførselsfraksjon blir etter passering gjennom varmeveksleren El via ledning 3, hvori en kontrollventil V3 er anordnet, tilført til en lagrings-beholder D4. Det kondenserte produkt (LNG) kan føres ut derfra via ledning 4. Reguleringsventilen V3 tjener til å ekspandere den kondenserte tilførselsfraksjonen til produktets avleveringstrykk, som i det minste korresponderer omtrentlig med atmosfæretrykket. The condensed supply fraction is, after passing through the heat exchanger El via line 3, in which a control valve V3 is arranged, supplied to a storage container D4. The condensed product (LNG) can be discharged from there via line 4. The control valve V3 serves to expand the condensed supply fraction to the product's delivery pressure, which corresponds at least approximately to the atmospheric pressure.
Dersom nitrogenet fordampes i den tredje seksjon c i varmeveksler El ved et trykk som er høyere enn 15 bara, vil nitrogenets kokepunktstemperatur ikke lenger være lavt nok til å underkjøle den kondenserte tilførselsfraksjon i en slik grad at det kan for-hindres utgassing etter ekspansjonen av denne i reguleringsventilen V3.1 dette tilfellet blir gassen som koker av i lagringsbeholderen D4 med fordel tatt ut via ledning 5, komprimert i kompressoren C3 og ført tilbake til tilførselsfraksjonen 2 som er befridd for tunge komponenter, før kondensasjon av denne og rekondensasjon i varmeveksleren El. Denne utførelsen av fremgangsmåten bør velges særlig i det tilfellet at det er en signifikant temporær lagring av LNG-produktet i en atmosfærisk, flatbunnet tank D4, siden den resulterende gassen som har kokt av derved også blir prosessert. If the nitrogen is evaporated in the third section c in the heat exchanger El at a pressure higher than 15 bara, the boiling point temperature of the nitrogen will no longer be low enough to subcool the condensed feed fraction to such an extent that outgassing can be prevented after the expansion of this in the control valve V3.1 in this case the gas that boils off in the storage container D4 is advantageously taken out via line 5, compressed in the compressor C3 and returned to the supply fraction 2 which is freed of heavy components, before condensation of this and recondensation in the heat exchanger El. This embodiment of the method should be chosen in particular in the case that there is a significant temporary storage of the LNG product in an atmospheric, flat-bottomed tank D4, since the resulting gas that has boiled off thereby is also processed.
Nitrogenet som kreves for å oppnå kulde, tilføres til kondensasjonsprosessen via ledning 6. Med fordel anordnes en buffertank D3 som tjener til å kompensere for kvantitative fluktuasjoner i tilførselsfraksjonen som skal kondenseres og/eller i kjøle-midlet nitrogen. Ved hjelp av en pumpe Pl blir flytende nitrogen tilført i nødvendig mengde til en separator Dl via ledning 7. Fra bunnfasen i separatoren Dl blir kokende nitrogen tatt ut og ledet via ledning 8 gjennom den kaldeste seksjon c i varmeveksleren El. Nitrogenet som i dette tilfellet er delvis fordampet, blir så ført via ledning 8' tilbake til separatoren Dl. The nitrogen required to obtain cold is supplied to the condensation process via line 6. Advantageously, a buffer tank D3 is arranged which serves to compensate for quantitative fluctuations in the supply fraction to be condensed and/or in the refrigerant nitrogen. By means of a pump Pl, liquid nitrogen is supplied in the required amount to a separator Dl via line 7. From the bottom phase in the separator Dl, boiling nitrogen is taken out and led via line 8 through the coldest section c in the heat exchanger El. The nitrogen, which in this case is partially evaporated, is then led via line 8' back to the separator D1.
Dersom rekondensasjonsprosessen, som ennå ikke er beskrevet, blir utført, kan i det minste genereringen av kulde ved rekondensasjonen av nitrogenet overskride kjølebehovet ved kondensasjon av naturgassen. En for stor tilførsel av flytende nitrogen som et resultat av dette kan avleveres i buffertanken D3 via ledning 8" og ventil V6. If the recondensation process, which has not yet been described, is carried out, at least the generation of cold by the recondensation of the nitrogen may exceed the cooling demand by condensation of the natural gas. An excessive supply of liquid nitrogen as a result of this can be delivered into the buffer tank D3 via line 8" and valve V6.
Ved toppen av separatoren Dl blir gassformig nitrogen tatt ut via ledning 9 og tilført til midtseksjonen b i varmeveksleren El. Det gassformige nitrogen ledes gjennom den andre og første seksjon i varmeveksleren El i motstrøm til tilførsels-fraksjonen 2 som skal bli avkjølt og delvis kondensert, og blir oppvarmet og overhetet i denne prosessen. Det overhetede nitrogen blir deretter tatt ut fra prosessen via lednings-seksj onene 10 og 11. At the top of the separator Dl, gaseous nitrogen is taken out via line 9 and supplied to the middle section b of the heat exchanger El. The gaseous nitrogen is passed through the second and first sections in the heat exchanger El in countercurrent to the supply fraction 2 which is to be cooled and partially condensed, and is heated and superheated in this process. The superheated nitrogen is then withdrawn from the process via line sections 10 and 11.
Ved hjelp av reguleringsventilen V4 reguleres kokepunktstrykket for det gassformige nitrogen som skal overhetes 9. Dette kokepunktstrykket blir fordelaktig justert til verdier mellom 5 og 30 bara, fortrinnsvis mellom 10 og 20 bara. By means of the control valve V4, the boiling point pressure for the gaseous nitrogen to be superheated 9 is regulated. This boiling point pressure is advantageously adjusted to values between 5 and 30 bara, preferably between 10 and 20 bara.
Likeledes kan kondensasjonstrykket i tilførselsfraksjonen 2 som er befridd for relativt tunge komponenter, reguleres ved hjelp av reguleringsventilen V2. Dette kondensasjonstrykket blir fortrinnsvis justert til verdier mellom 1 og 15 bara, fortrinnsvis mellom 1 og 8 bara. Likewise, the condensation pressure in the supply fraction 2, which is freed from relatively heavy components, can be regulated by means of the control valve V2. This condensation pressure is preferably adjusted to values between 1 and 15 bara, preferably between 1 and 8 bara.
Ved hjelp av reguleringsventilene V2 og/eller V4 kan temperaturprofilen i den tredje seksjon c av varmeveksleren El reguleres. Mens kondensasjonstrykket for tilførselsfraksjonen blir etablert i seksjonen mellom reguleringsventilene V2 og V3 ved hjelp av reguleringsventilen V2, blir kokepunktstrykket for nitrogenet i separatoren Dl og den tredje seksjon c av varmeveksleren El regulert ved hjelp av reguleringsventilen V4. Som følge av den ovenfor beskrevne oppdeling av varmevekslerprosessen i en andre og tredje seksjon, og med faseseparasjonen i separator Dl, kan det så bli nøyaktig bestemt i hvilken seksjon av varmeveksleren El det finner sted en (delvis) fordampning eller over-heting av nitrogenet. By means of the control valves V2 and/or V4, the temperature profile in the third section c of the heat exchanger El can be regulated. While the condensation pressure for the feed fraction is established in the section between the control valves V2 and V3 by means of the control valve V2, the boiling point pressure of the nitrogen in the separator Dl and the third section c of the heat exchanger El is regulated by means of the control valve V4. As a result of the above-described division of the heat exchanger process into a second and third section, and with the phase separation in separator Dl, it can then be precisely determined in which section of the heat exchanger El a (partial) evaporation or overheating of the nitrogen takes place.
Ved hjelp av oppdelingen av varmevekslerprosessen El i tre seksjoner a til c er det mulig sikkert å forhindre at fasegrensen mellom flytende og gassformig kjøle-middel vandrer inne i varmeveksleren El og derved forårsaker uønskede termiske og mekaniske spenninger inne i varmeveksleren El. By dividing the heat exchanger process El into three sections a to c, it is possible to safely prevent the phase boundary between liquid and gaseous coolant from wandering inside the heat exchanger El and thereby causing unwanted thermal and mechanical stresses inside the heat exchanger El.
Dersom nitrogenets kokepunktstrykk (pN2) og rågassens kondensasjonstrykk (pRG) velges i henhold til ulikheten pRG (bara) > 0,3 pN2(bara) -1, kan en termisk over-belastning av varmeveksleren El på grunn av utillatelig høye temperaturforskjeller unngås på sikker måte. If the nitrogen boiling point pressure (pN2) and the raw gas condensation pressure (pRG) are chosen according to the inequality pRG (bara) > 0.3 pN2(bara) -1, a thermal overload of the heat exchanger El due to unacceptably high temperature differences can be safely avoided manner.
Ved å begrense kokepunktstrykket for flytende nitrogen i den tredje seksjon c av varmeveksleren El og i separatoren Dl til minst 5 bara - den tilhørende kokepunktstemperatur er -179 °C - er det mulig sikkert å forhindre at det forekommer en temperatur under frysetemperaturen for metan i varmeveksleren El. Driftsproblemer og mulig skade på grunn av dannelse av faste stoffer er derved utelukket. By limiting the boiling point pressure of liquid nitrogen in the third section c of the heat exchanger El and in the separator Dl to at least 5 bar - the corresponding boiling point temperature is -179 °C - it is possible to safely prevent the occurrence of a temperature below the freezing temperature of methane in the heat exchanger El. Operational problems and possible damage due to the formation of solids are thereby ruled out.
Det overhetede nitrogen tatt ut fra varmeveksleren El via ledning 10, kan alternativt til fjerning via ledning 11 bli minst delvis rekondensert. For dette formål til-føres nitrogenet via ledningsseksjoner 12 og 13 til komprimering - vist på figuren som en totrinns kompressorenhet C1/C2, hvor en varmeveksler, henholdsvis E3 eller E4, er for- bundet nedstrøms i forhold til hver kompressorenhet - og deretter ført via ledning 14 til en varmeveksler E2. Der blir nitrogenet rekondensert og deretter ført til separator Dl via ledning 15. Trykkregulering av kompressor C2 utføres med reguleringsventil V5. For det formål å fremskaffe kulde i varmeveksleren E2, blir en delstrøm av den komprimerte nitrogenstrømmen tatt ut via ledning 16, fortrinnsvis ekspandert på en flertrinnsmåte - vist som gassekspandere XI og X2 - og deretter ledet via ledning 17 gjennom varmeveksleren E2 i motstrøm til nitrogenstrømmen som skal kondenseres. Akslingene på kompressorer Cl og C2 er fortrinnsvis koblet til akslingene på gassekspanderne X2 og The superheated nitrogen taken out from the heat exchanger El via line 10 can, as an alternative to removal via line 11, be at least partially recondensed. For this purpose, the nitrogen is supplied via line sections 12 and 13 for compression - shown in the figure as a two-stage compressor unit C1/C2, where a heat exchanger, respectively E3 or E4, is connected downstream in relation to each compressor unit - and then carried via wire 14 to a heat exchanger E2. There, the nitrogen is recondensed and then led to separator Dl via line 15. Pressure regulation of compressor C2 is carried out with control valve V5. For the purpose of providing cold in the heat exchanger E2, a partial flow of the compressed nitrogen flow is withdrawn via line 16, preferably expanded in a multi-stage manner - shown as gas expanders XI and X2 - and then led via line 17 through the heat exchanger E2 in countercurrent to the nitrogen flow which must be condensed. The shafts of compressors Cl and C2 are preferably connected to the shafts of gas expanders X2 and
XI. XI.
Dersom den ovenfor beskrevne rekondensasjonsprosessen utføres, er det fordelaktig å tilføre til varmeveksleren El via ledning 9 bare den mengden gassformig nitrogen som er nødvendig for en liten positiv temperaturforskjell på ca. 3 °C mellom strømmer 1 og 10 i den varme enden av varmeveksleren El. Overskuddsmengden av kaldt, gassformig nitrogen anvendes via ledning 9' forholdsmessig for rekondensasjon i varmeveksleren E2. If the recondensation process described above is carried out, it is advantageous to supply to the heat exchanger El via line 9 only the amount of gaseous nitrogen that is necessary for a small positive temperature difference of approx. 3 °C between streams 1 and 10 in the hot end of the heat exchanger El. The excess amount of cold, gaseous nitrogen is used via line 9' proportionally for recondensation in the heat exchanger E2.
I prinsippet kan kondensasjonsprosessen utføres ved hjelp av "importert" nitrogen - i dette tilfellet blir overhetet nitrogen tatt ut fra varmeveksleren El via ledningsseksjoner 10 og 11 - ved hjelp av rekondensert nitrogen eller enhver ønsket kombinasjon av begge driftsmåter. In principle, the condensation process can be carried out by means of "imported" nitrogen - in this case superheated nitrogen is withdrawn from the heat exchanger El via line sections 10 and 11 - by means of recondensed nitrogen or any desired combination of both modes of operation.
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| DE4440401A1 (en) * | 1994-11-11 | 1996-05-15 | Linde Ag | Process for liquefying natural gas |
| DE69523437T2 (en) * | 1994-12-09 | 2002-06-20 | Kabushiki Kaisha Kobe Seiko Sho (Kobe Steel, Ltd.) | Gas liquefaction plant and method |
| FR2743140B1 (en) * | 1995-12-28 | 1998-01-23 | Inst Francais Du Petrole | METHOD AND DEVICE FOR TWO-STEP LIQUEFACTION OF A GAS MIXTURE SUCH AS A NATURAL GAS |
| DE19612173C1 (en) * | 1996-03-27 | 1997-05-28 | Linde Ag | Procedure for liquefaction of hydrocarbon rich process flow, especially natural gas |
| NO328493B1 (en) * | 2007-12-06 | 2010-03-01 | Kanfa Aragon As | System and method for regulating the cooling process |
-
2010
- 2010-09-09 DE DE102010044869A patent/DE102010044869A1/en not_active Withdrawn
-
2011
- 2011-09-06 CN CN201110294097.8A patent/CN102410702B/en not_active Expired - Fee Related
- 2011-09-07 CH CH01475/11A patent/CH703773B1/en not_active IP Right Cessation
- 2011-09-07 US US13/226,633 patent/US20120060553A1/en not_active Abandoned
- 2011-09-07 AR ARP110103264A patent/AR082919A1/en active IP Right Grant
- 2011-09-07 NO NO20111212A patent/NO20111212A1/en not_active Application Discontinuation
- 2011-09-08 BR BRPI1104609-0A patent/BRPI1104609A2/en not_active Application Discontinuation
- 2011-09-09 AU AU2011221424A patent/AU2011221424B2/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| AU2011221424A1 (en) | 2012-03-29 |
| DE102010044869A1 (en) | 2012-03-15 |
| CH703773A2 (en) | 2012-03-15 |
| CN102410702B (en) | 2016-01-20 |
| AR082919A1 (en) | 2013-01-16 |
| CN102410702A (en) | 2012-04-11 |
| US20120060553A1 (en) | 2012-03-15 |
| CH703773B1 (en) | 2015-02-27 |
| AU2011221424B2 (en) | 2016-03-31 |
| BRPI1104609A2 (en) | 2013-04-24 |
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