NO20111495A1 - Process for condensing a hydrocarbon-rich fraction - Google Patents
Process for condensing a hydrocarbon-rich fraction Download PDFInfo
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- NO20111495A1 NO20111495A1 NO20111495A NO20111495A NO20111495A1 NO 20111495 A1 NO20111495 A1 NO 20111495A1 NO 20111495 A NO20111495 A NO 20111495A NO 20111495 A NO20111495 A NO 20111495A NO 20111495 A1 NO20111495 A1 NO 20111495A1
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- Prior art keywords
- circuit
- refrigerant mixture
- refrigerant
- condensation
- hydrocarbon
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- 238000000034 method Methods 0.000 title claims description 26
- 239000004215 Carbon black (E152) Substances 0.000 title claims description 18
- 229930195733 hydrocarbon Natural products 0.000 title claims description 18
- 150000002430 hydrocarbons Chemical class 0.000 title claims description 18
- 239000003507 refrigerant Substances 0.000 claims description 71
- 239000000203 mixture Substances 0.000 claims description 62
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 34
- 238000009833 condensation Methods 0.000 claims description 32
- 230000005494 condensation Effects 0.000 claims description 32
- 238000001816 cooling Methods 0.000 claims description 20
- 230000006835 compression Effects 0.000 claims description 15
- 238000007906 compression Methods 0.000 claims description 15
- 239000002826 coolant Substances 0.000 claims description 11
- 239000000126 substance Substances 0.000 claims description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 239000003345 natural gas Substances 0.000 description 14
- 239000007788 liquid Substances 0.000 description 7
- 238000001035 drying Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 150000001412 amines Chemical class 0.000 description 3
- 230000001419 dependent effect Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000007789 gas Substances 0.000 description 1
- 238000012432 intermediate storage Methods 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
- F25J1/02—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
- F25J1/0002—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
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/008—Hydrocarbons
- F25J1/0085—Ethane; Ethylene
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J1/0087—Propane; Propylene
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0214—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
- F25J1/0211—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
- F25J1/0216—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 using a C3 pre-cooling cycle
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Compression-Type Refrigeration Machines With Reversible Cycles (AREA)
Description
Oppfinnelsen angår en fremgangsmåte for kondensasjon av en hydrokarbonrik fraksjon. The invention relates to a method for the condensation of a hydrocarbon-rich fraction.
Fra US 3 763 358 er det kjent en fremgangsmåte for kondensasjon av en hydrokarbonrik fraksjon som særlig finner anvendelse ved kondensasjonsprosesser for naturgass. Herved anvendes et kretsløp med kjølemiddelblanding for kondensasjon og under-kjøling av naturgassen, mens det i tillegg er anordnet et rentstoff-kjølekretsløp som så vel forkjøler naturgassen som skal kondenseres som også forkjøler og delvis kondenserer kjølemiddelblandingen i kjølemiddelblandingskretsløpet. En slik kondensasjonsutførelse egner seg særlig for kondensasjonsprosesser for naturgass med en kapasitet mellom 1 og 6 millioner årstonn LNG. From US 3,763,358, a method for the condensation of a hydrocarbon-rich fraction is known, which is particularly useful in condensation processes for natural gas. Hereby, a circuit with a refrigerant mixture is used for condensation and sub-cooling of the natural gas, while there is also a clean-substance cooling circuit which pre-cools the natural gas to be condensed, which also pre-cools and partially condenses the refrigerant mixture in the refrigerant mixture circuit. Such a condensation design is particularly suitable for condensation processes for natural gas with a capacity of between 1 and 6 million tonnes of LNG per year.
Naturgassen som skal kondenseres, blir før den egentlige avkjølingen og kondenseringen som regel tilført en vandig aminvask, og etter denne er det anordnet en tørke-enhet. Særlig i varme klimasoner kan det anvendes en delstrøm fra det foran beskrevne rentstoff-kjølekretsløpet for kondensasjon av vann inneholdt i naturgassen, hvorved tørkeren anordnet etter aminvasken avlastes. The natural gas to be condensed is usually fed with an aqueous amine wash before the actual cooling and condensation, and after this a drying unit is arranged. Particularly in warm climate zones, a partial flow from the previously described pure substance cooling circuit can be used for condensation of water contained in the natural gas, whereby the dryer arranged after the amine wash is relieved.
Denne kondensasjonsprosessen krever imidlertid en forholdsvis omstendelig apparatur. Således er det alt etter utførelse inntil ni rentstoffordampere av kjeletype samt to sammenkoblede, viklede varmevekslere. Særlig ved mindre kondensasjonskapasiteter - her forstås kapasiteter på mindre enn 3 millioner årstonn LNG - har den foran beskrevne prosessutførelsen ulemper i forhold til de såkalte SMR(Single Mixed Refrigerant)-kondensasjonsprosessene hvor det ikke kreves noe separat forkjølingskretsløp, da den foran beskrevne kondensasjonsprosessen betinger høyere investeringskostnader, som heller ikke kan kompenseres med det mindre energiforbruket. This condensation process, however, requires a relatively cumbersome apparatus. Thus, depending on the design, there are up to nine boiler-type pure gas evaporators as well as two connected, coiled heat exchangers. Especially with smaller condensation capacities - here we mean capacities of less than 3 million tonnes of LNG per year - the above-described process design has disadvantages compared to the so-called SMR (Single Mixed Refrigerant) condensation processes where no separate pre-cooling circuit is required, as the above-described condensation process requires higher investment costs, which cannot be compensated with the lower energy consumption either.
Oppgaven for den foreliggende oppfinnelse er å tilveiebringe en fremgangsmåte på området fremgangsmåte for kondensasjon av en hydrokarbonrik fraksjon, hvor de foran beskrevne ulemper unngås. The task of the present invention is to provide a method in the area of method for condensation of a hydrocarbon-rich fraction, where the disadvantages described above are avoided.
For løsning av denne oppgaven foreslås en fremgangsmåte på området for kondensasjon av hydrokarbonrik fraksjon, hvor To solve this task, a method is proposed in the area of condensation of hydrocarbon-rich fraction, where
a) avkjølingen og kondenseringen av den hydrokarbonrike fraksjon skjer i indirekte varmeveksling mot kjølemiddelblandingen i et kjølemiddel-blandingskretsløp, b) avkjølingen av den hydrokarbonrike fraksjon skjer i indirekte varmeveksling mot den fullstendig fordampede kjølemiddelblanding i kjølemiddelblandings-kretsløpet, c) den komprimerte kjølemiddelblanding i kjølemiddelblandingskretsløpet for-kjøles ved hjelp av et rentstoff-kjølekretsløp, og d) sammensetningen av kjølemiddelblandingen og/eller komprimeringstrykket for kjølemiddelblandingskretsløpet velges eller blir valgt slik at kjølemiddel-blandingen blir fullstendig kondensert ved hjelp av rentstoff-kjølekretsløpet. a) the cooling and condensation of the hydrocarbon-rich fraction occurs in indirect heat exchange against the refrigerant mixture in a refrigerant mixture circuit, b) the cooling of the hydrocarbon-rich fraction occurs in indirect heat exchange against the completely vaporized refrigerant mixture in the refrigerant mixture circuit, c) the compressed refrigerant mixture in the refrigerant mixture circuit for - is cooled by means of a pure substance refrigerant circuit, and d) the composition of the refrigerant mixture and/or the compression pressure of the refrigerant mixture circuit is selected or is selected so that the refrigerant mixture is completely condensed by means of the pure substance refrigerant circuit.
Med begrepet "rentstoff-kjølekretsløp" skal forstås et kjølekretsløp hvor kjøle-midlet foreligger i en konsentrasjon på minst 95 vol%. The term "pure refrigerant circuit" is to be understood as a cooling circuit where the refrigerant is present in a concentration of at least 95 vol%.
I motsetning til den foran beskrevne kondensasjonsutførelse skjer avkjølingen og kondenseringen av den hydrokarbonrike fraksjon utelukkende i indirekte varmeveksling In contrast to the condensation design described above, the cooling and condensation of the hydrocarbon-rich fraction takes place exclusively in indirect heat exchange
mot kjølemiddelblandingen i et kjølemiddelblandingskretsløp. Det videre anordnede rent-stoff-kjølekretsløpet tjener ifølge oppfinnelsen utelukkende til å forkjøle den komprimerte kjølemiddelblanding i kjølemiddelblandingskretsløpet. For dette må sammensetningen av kjølemiddelblandingen og/eller komprimeringstrykket i kjølemiddelblandingskretsløpet velges slik at kjølemiddelblandingen blir så mye avkjølt med rentstoff-kjølekretsløpet at den foreligger fullstendig kondensert. against the refrigerant mixture in a refrigerant mixture circuit. According to the invention, the further arranged pure-substance cooling circuit serves exclusively to pre-cool the compressed refrigerant mixture in the refrigerant mixture circuit. For this, the composition of the refrigerant mixture and/or the compression pressure in the refrigerant mixture circuit must be selected so that the refrigerant mixture is cooled so much by the pure substance refrigerant circuit that it is completely condensed.
Som følge av dette kan kjølemiddelblandingen umiddelbart tilføres til en varmeveksler som tjener til å kondensere og underkjøle den hydrokarbonrike fraksjon uten at det må kobles inn en fraskiller foran varmeveksleren. As a result, the coolant mixture can be immediately supplied to a heat exchanger which serves to condense and subcool the hydrocarbon-rich fraction without having to connect a separator in front of the heat exchanger.
Ved fremgangsmåten ifølge oppfinnelsen kan likevel fordelen med en forkjøling ved hjelp av et rentstoff-kjølekretsløp i det vesentlige bibeholdes med hensyn til energi-forbruk og egnethet for avlastning av en eventuell anordnet tørkeenhet. Den nødvendige apparaturen for kondensasjonsutførelsen ifølge oppfinnelsen er imidlertid vesentlig mindre sammenlignet med den foran beskrevne kondensasjonsutførelsen, da antallet varmevekslere reduseres betydelig. With the method according to the invention, the advantage of a pre-cooling by means of a pure-substance cooling circuit can still be essentially maintained with regard to energy consumption and suitability for relieving the load of a possibly arranged drying unit. The necessary apparatus for the condensation embodiment according to the invention is, however, significantly smaller compared to the condensation embodiment described above, as the number of heat exchangers is significantly reduced.
Riktignok fører fremgangsmåten ifølge oppfinnelsen til en mindre høyning av energiforbruket - høyningen utgjør maksimalt 5 %. Imidlertid forbedres totaløkonomien ved kondensasjonsprosessen fordi fremgangsmåten ifølge oppfinnelsen er mer økonomisk enn kjente kondensasjonsprosesser, særlig i kapasitetsområdet mellom 0,5 og 3 millioner årstonn LNG. Admittedly, the method according to the invention leads to a minor increase in energy consumption - the increase amounts to a maximum of 5%. However, the overall economy of the condensation process is improved because the method according to the invention is more economical than known condensation processes, particularly in the capacity range between 0.5 and 3 million tonnes of LNG per year.
Ytterligere fordelaktige utførelsesformer av fremgangsmåten ifølge oppfinnelsen for kondensasjon av en hydrokarbonrik fraksjon er gjenstand for de avhengige patentkrav, og er kjennetegnet ved at Further advantageous embodiments of the method according to the invention for condensation of a hydrocarbon-rich fraction are the subject of the dependent patent claims, and are characterized in that
kjølemidlet i rentstoff-kjølekretsløpet består av minst 95 vol% av C3H8, the coolant in the clean-liquid cooling circuit consists of at least 95 vol% of C3H8,
C3H6, C2H6, C2H4eller C02, C3H6, C2H6, C2H4 or C02,
kjølemiddelblandingen i kjølemiddelblandingskretsløpet inneholder nitrogen, the refrigerant mixture in the refrigerant mixture circuit contains nitrogen,
metan og minst to komponenter valgt blant C2H4, C2H6, C3H8, C3H6, C4H10og C5H12, og methane and at least two components selected from C2H4, C2H6, C3H8, C3H6, C4H10 and C5H12, and
kjølemiddelblandingen i kjølemiddelblandingskretsløpet fordamper the refrigerant mixture in the refrigerant mixture circuit evaporates
fullstendig ved kondensasjon av den hydrokarbonrike fraksjon. completely by condensation of the hydrocarbon-rich fraction.
Fremgangsmåten ifølge oppfinnelsen for kondensasjon av en hydrokarbonrik fraksjon, samt ytterligere fordelaktige utførelsesformer av denne, som er gjenstand for de avhengige patentkrav, skal i det følgende forklares nærmere ved hjelp av utførelses-eksemplene vist på figuren. The method according to the invention for the condensation of a hydrocarbon-rich fraction, as well as further advantageous embodiments thereof, which are the subject of the dependent patent claims, shall be explained in more detail in the following with the aid of the embodiment examples shown in the figure.
Via ledning 1 blir den hydrokarbonrike fraksjon som skal kondenseres, som i det etterfølgende dreier seg om en naturgasstrøm, tilført en aminvasking A. Etter denne er det innkoblet en tørkeenhet T, med en forankoblet varmeveksler El. I denne skjer en delvis kondensasjon av vann inneholdt i naturgassen for å avlaste tørkeenhet T. Via line 1, the hydrocarbon-rich fraction to be condensed, which subsequently turns to a natural gas stream, is supplied to an amine wash A. After this, a drying unit T is connected, with a pre-connected heat exchanger El. In this, a partial condensation of water contained in the natural gas takes place to relieve drying unit T.
Naturgasstrømmen forbehandlet på denne måten, blir via ledning 2 tilført til en varmeveksler E6, og i denne avkjølt mot den fullstendig fordampede kjølemiddelblanding i kjølemiddelblandingskretsløpet, hvilket skal forklares nærmere i det følgende. Varmeveksler E6 er fortrinnsvis utført som en platevarmeveksler. The natural gas stream, pretreated in this way, is supplied via line 2 to a heat exchanger E6, and in this cooled against the completely evaporated refrigerant mixture in the refrigerant mixture circuit, which will be explained in more detail below. Heat exchanger E6 is preferably designed as a plate heat exchanger.
Via ledning 3 blir den avkjølte naturgasstrømmen tilført til en varmeveksler E7 som fortrinnsvis er en viklet varmeveksler. I denne skjer kondensasjon og underkjøling av naturgasstrømmen i indirekte varmeveksling med kjølemiddelblandingen i kjølemiddel-blandingskretsløpet. Via ledning 4 blir den underkjølte LNG-produktstrømmen tatt ut og tilført til et mellomlager eller umiddelbart til videre anvendelse. Via line 3, the cooled natural gas stream is supplied to a heat exchanger E7 which is preferably a coiled heat exchanger. In this, condensation and subcooling of the natural gas flow takes place in indirect heat exchange with the refrigerant mixture in the refrigerant mixture circuit. Via line 4, the subcooled LNG product stream is taken out and supplied to an intermediate storage or immediately for further use.
Kjølemiddelblandingen i kjølemiddelblandingskretsløpet blir i en ett- eller flere-trinnskomprimeringsenhet komprimert til det ønskede komprimeringstrykk; på figuren er det vist to komprimeringstrinn V2 og V2', og mellom komprimeringstrinnene er det fortrinnsvis anordnet en mellomkjøler som ikke er vist på figuren. Etter avkjøling i etter-kjøler E9 blir den komprimerte kjølemiddelblanding ført via ledning 5 gjennom fire varmevekslere E2 til E5 som er koblet etter hverandre. I disse blir kjølemiddelblandingen i indirekte varmeveksling med kjølemidlet i rentstoff-kjølekretsløpet, hvilket skal forklares nærmere nedenfor, avkjølt så mye at den ved utgangen av den siste varmeveksler E5 er flytende og dermed foreligger enfasig. The refrigerant mixture in the refrigerant mixture circuit is compressed to the desired compression pressure in a one- or multi-stage compression unit; two compression stages V2 and V2' are shown in the figure, and between the compression stages an intercooler is preferably arranged which is not shown in the figure. After cooling in after-cooler E9, the compressed coolant mixture is led via line 5 through four heat exchangers E2 to E5 which are connected one after the other. In these, the refrigerant mixture is cooled in indirect heat exchange with the refrigerant in the pure refrigerant circuit, which will be explained in more detail below, so much that it is liquid at the exit of the last heat exchanger E5 and is thus single-phase.
For å oppnå denne totale kondensasjon av kjølemiddelblandingen i kjølemiddel-blandingskretsløpet ved utgangen av den siste varmeveksler E5 må sammensetningen av kjølemiddelblandingen og/eller komprimeringstrykket i kjølemiddelblandingskretsløpet velges tilsvarende. In order to achieve this total condensation of the refrigerant mixture in the refrigerant mixture circuit at the output of the last heat exchanger E5, the composition of the refrigerant mixture and/or the compression pressure in the refrigerant mixture circuit must be selected accordingly.
Som kjølemiddel for rentstoff-kjølekretsløpet anvendes fortrinnsvis C3H8, C3H6, C2H6, C2H4eller CO2. Kjølemiddelblandingen i kjølemiddelblandingskretsløpet inneholder fortrinnsvis nitrogen, metan og minst to komponenter fra gruppen C2H4, C2H6, C3Hg, C4H10og C5H12. C3H8, C3H6, C2H6, C2H4 or CO2 is preferably used as a coolant for the pure substance cooling circuit. The coolant mixture in the coolant mixture circuit preferably contains nitrogen, methane and at least two components from the group C2H4, C2H6, C3Hg, C4H10 and C5H12.
Kjølemiddelblandingen kondensert med rentstoff-kjølekretsløpet kan nå via ledning 6 umiddelbart tilføres til varmeveksler E7. Å anordne en avskiller foran varmeveksler E7 kan derved spares. I varmeveksler E7 blir den flytende kjølemiddelblanding underkjølt før den tas ut via ledning 7 og i ventil A trykkavlastes til det laveste trykket. The coolant mixture condensed with the pure refrigerant circuit can now via line 6 be immediately supplied to heat exchanger E7. Arranging a separator in front of heat exchanger E7 can thereby be saved. In heat exchanger E7, the liquid coolant mixture is subcooled before it is taken out via line 7 and in valve A the pressure is relieved to the lowest pressure.
Som alternativ til ventil a vist på figuren, kan det anordnes en væskeekspanderer som tjener som den arbeidsytende trykkavlastning for kjølemiddelblandingen i den kalde enden av varmeveksler E7. As an alternative to valve a shown in the figure, a liquid expander can be arranged which serves as the effective pressure relief for the refrigerant mixture in the cold end of heat exchanger E7.
Den trykkavlastede kjølemiddelblanding som via ledning 7 på ny tilføres til varmeveksler E7, tjener i varmeveksler E7 til å kondensere og underkjøle natur-gasstrømmen. På fordelaktig måte fordamer kjølemiddelblandingen fullstendig ved kondensering og underkjøling av naturgasstrømmen, slik at en fullstendig fordampet kjølemiddelstrøm tas ut fra varmeveksler E7 via ledning 8 og tilføres til varmeveksler E6. I denne blir kjølemiddelblandingen overhetet mot naturgasstrømmen som skal avkjøles, før den på ny via ledning 9 føres til inngangen av kretsløpskomprimeringsenhet V2/V2'. The depressurized refrigerant mixture, which via line 7 is again supplied to heat exchanger E7, serves in heat exchanger E7 to condense and subcool the natural gas flow. Advantageously, the refrigerant mixture completely vaporizes by condensing and subcooling the natural gas stream, so that a completely vaporized refrigerant stream is taken out of heat exchanger E7 via line 8 and supplied to heat exchanger E6. In this, the refrigerant mixture is superheated against the natural gas flow to be cooled, before it is led again via line 9 to the input of circuit compression unit V2/V2'.
Det allerede forklarte rentstoff-kjølekretsløp har likeledes en flertrinns komprimeringsenhet VI, til hvilken det er anordnet en kondensator E8. Kjølemidlet komprimert til det ønskede sluttrykket blir via ledning 10 tilført til et forgreningspunkt hvor en del-strøm av kjølemidlet trykkavlastes via ventil b i den allerede forklarte varmeveksler El, og fra denne via ledninger 11 og 13 igjen tilført til komprimeringsenhet VI. En andre delstrøm blir via ledning 12 og ventil c trykkavlastet i varmeveksleren E2. The already explained pure substance cooling circuit likewise has a multi-stage compression unit VI, to which a condenser E8 is arranged. The refrigerant compressed to the desired final pressure is fed via line 10 to a branching point where a partial flow of the refrigerant is pressure relieved via valve b in the already explained heat exchanger El, and from this via lines 11 and 13 again fed to compression unit VI. A second partial flow is depressurized via line 12 and valve c in the heat exchanger E2.
Mens den gassformige andel av kjølemidlet tas ut via ledning 13 fra varmeveksler E2 og tilføres til komprimeringsenhet VI på et mellomtrykkstrinn, blir den flytende andel av kjølemidlet tatt ut via ledning 14 fra varmeveksler E2 og trykkavlastet over ventil d i varmeveksleren E3. På ny skjer en oppdeling i en gassformig kjølemiddelandel som via ledning 15 tilføres komprimeringsenhet VI og et mellomtrykkstrinn, mens den flytende kjølemiddelandel tas ut via ledning 16 og trykkavlastes over ventil e i varmeveksler E4. Også fra denne blir den gassformige kjølemiddelandel tilført via ledning 17 til komprimeringsenhet VI på et mellomtrykkstrinn, mens den flytende kjølemiddelandel tas ut via ledning 18 og trykkavlastes over ventil f i den siste varmeveksler E5. Via ledning 19 blir det fullstendig fordampede kjølemiddel tilført til komprimeringsenhet VI på det laveste trykktrinnet. While the gaseous portion of the refrigerant is withdrawn via line 13 from heat exchanger E2 and supplied to compression unit VI at an intermediate pressure stage, the liquid portion of the refrigerant is withdrawn via line 14 from heat exchanger E2 and pressure relieved via valve d in heat exchanger E3. Again, a division takes place into a gaseous refrigerant portion which is supplied via line 15 to compression unit VI and an intermediate pressure stage, while the liquid refrigerant portion is withdrawn via line 16 and pressure is relieved via valve e in heat exchanger E4. Also from this, the gaseous refrigerant portion is supplied via line 17 to compression unit VI at an intermediate pressure stage, while the liquid refrigerant portion is withdrawn via line 18 and pressure is relieved via valve f in the last heat exchanger E5. Via line 19, the completely evaporated refrigerant is supplied to compression unit VI at the lowest pressure stage.
I stedet for avkjølingen av kjølemiddelblandingen i varmeveksler E2 til E5 vist på figuren, kan det i praksis også bli realisert færre, så som fire, varmevekslere. Antallet varmevekslere bestemmes i det vesentlige av omgivende temperatur og tallet på løpehjul i turbokomprimerer VI. Instead of the cooling of the refrigerant mixture in heat exchangers E2 to E5 shown in the figure, fewer, such as four, heat exchangers can also be realized in practice. The number of heat exchangers is essentially determined by the ambient temperature and the number of impellers in turbocompressors VI.
Fremgangsmåten ifølge oppfinnelsen for kondensasjon av en hydrokarbonrik fraksjon tilveiebringer en kondensasjonsprosess med redusert mengde apparatur og en forbedret totaløkonomi, hvilket må betales med en mindre høyning av energiforbruket. Fremgangsmåten ifølge oppfinnelsen egner seg særlig for kapasitetsområder mellom The method according to the invention for the condensation of a hydrocarbon-rich fraction provides a condensation process with a reduced amount of equipment and an improved overall economy, which must be paid for with a smaller increase in energy consumption. The method according to the invention is particularly suitable for capacity ranges between
0,5 og 3 millioner årstonn LNG. 0.5 and 3 million annual tonnes of LNG.
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| DE102009018248A DE102009018248A1 (en) | 2009-04-21 | 2009-04-21 | Process for liquefying a hydrocarbon-rich fraction |
| PCT/EP2010/002326 WO2010121752A2 (en) | 2009-04-21 | 2010-04-15 | Method for liquefying a hydrocarbon-rich fraction |
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| NO346539B1 NO346539B1 (en) | 2022-09-26 |
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| CN104792113B (en) * | 2014-01-22 | 2018-09-28 | 北京中科富海低温科技有限公司 | Helium liquefier and its control method |
| DE102015002822A1 (en) * | 2015-03-05 | 2016-09-08 | Linde Aktiengesellschaft | Process for liquefying a hydrocarbon-rich fraction |
| WO2017093377A1 (en) * | 2015-12-03 | 2017-06-08 | Shell Internationale Research Maatschappij B.V. | Method of liquefying a co2 contaminated hydrocarbon-containing gas stream |
| US10663220B2 (en) * | 2016-10-07 | 2020-05-26 | Air Products And Chemicals, Inc. | Multiple pressure mixed refrigerant cooling process and system |
| GB2582763A (en) * | 2019-04-01 | 2020-10-07 | Linde Ag | Method and device for the recovery of waste energy from refrigerant compression systems used in gas liquefaction processes |
| DE102020006394A1 (en) | 2020-10-17 | 2022-04-21 | Linde Gmbh | Process and plant for producing a liquified hydrocarbon product |
| DE102020006396A1 (en) | 2020-10-17 | 2022-04-21 | Linde Gmbh | Process and plant for producing a liquified hydrocarbon product |
| EP4230937A1 (en) | 2022-02-21 | 2023-08-23 | Linde GmbH | Method and system for generating a liquefied hydrocarbon product |
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| US3763658A (en) | 1970-01-12 | 1973-10-09 | Air Prod & Chem | Combined cascade and multicomponent refrigeration system and method |
| FR2292203A1 (en) * | 1974-11-21 | 1976-06-18 | Technip Cie | METHOD AND INSTALLATION FOR LIQUEFACTION OF A LOW BOILING POINT GAS |
| US4525185A (en) * | 1983-10-25 | 1985-06-25 | Air Products And Chemicals, Inc. | Dual mixed refrigerant natural gas liquefaction with staged compression |
| CN1004228B (en) * | 1985-04-01 | 1989-05-17 | 气体产品与化学公司 | To liquidize natural gas by two mixed refrigerants |
| DE29823450U1 (en) * | 1998-01-19 | 1999-06-02 | Linde Ag, 65189 Wiesbaden | Device for liquefying a hydrocarbon-rich stream |
| US6119479A (en) * | 1998-12-09 | 2000-09-19 | Air Products And Chemicals, Inc. | Dual mixed refrigerant cycle for gas liquefaction |
| US6324867B1 (en) * | 1999-06-15 | 2001-12-04 | Exxonmobil Oil Corporation | Process and system for liquefying natural gas |
| US6438994B1 (en) * | 2001-09-27 | 2002-08-27 | Praxair Technology, Inc. | Method for providing refrigeration using a turboexpander cycle |
| DE60207689T3 (en) * | 2002-05-27 | 2013-01-24 | Air Products And Chemicals, Inc. | Heat exchanger with wound coils |
| CA2676177A1 (en) * | 2007-01-25 | 2008-07-31 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for cooling a hydrocarbon stream |
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| CN102575897A (en) | 2012-07-11 |
| DE102009018248A1 (en) | 2010-10-28 |
| WO2010121752A2 (en) | 2010-10-28 |
| MY173948A (en) | 2020-02-28 |
| RU2568697C2 (en) | 2015-11-20 |
| WO2010121752A3 (en) | 2012-10-11 |
| CN102575897B (en) | 2014-11-26 |
| RU2011147065A (en) | 2013-05-27 |
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