EP0535752B1 - Method for liquefying natural gas - Google Patents

Method for liquefying natural gas Download PDF

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Publication number
EP0535752B1
EP0535752B1 EP92203009A EP92203009A EP0535752B1 EP 0535752 B1 EP0535752 B1 EP 0535752B1 EP 92203009 A EP92203009 A EP 92203009A EP 92203009 A EP92203009 A EP 92203009A EP 0535752 B1 EP0535752 B1 EP 0535752B1
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EP
European Patent Office
Prior art keywords
pressure
zone
gas
phase
methane
Prior art date
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EP92203009A
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German (de)
French (fr)
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EP0535752A1 (en
Inventor
Henri Paradowski
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Francaise dEtudes et de Construction Technip SA
Technip Energies France SAS
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Francaise dEtudes et de Construction Technip SA
Technip SA
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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
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • 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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    • 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
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    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
    • F25J1/0239—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling
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    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
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    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
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    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons

Definitions

  • the invention relates to a natural gas liquefaction process comprising the separation of hydrocarbons heavier than methane.
  • Natural gas and other methane-rich gas streams are commonly available at sites away from places of use, and it is therefore common to liquefy natural gas for transportation by land or sea. Liquefaction is widely practiced in the present day and the literature and patents describe numerous processes and apparatuses for liquefaction. US-A-3945 214, 4251 247, 4274 849, 4339 253 and 4539 028 are examples of such methods.
  • US Pat. No. 4,690,702 describes a process in which the charge of hydrocarbons under high pressure (P1) is cooled so as to cause the liquefaction of part of the hydrocarbons, a gas phase (G1) is separated from a liquid phase (L1), the gas phase is relaxed (G1) to lower its pressure to a value (P2) lower than (P1), the liquid phase (L1) and the gas phase (G1) are sent under pressure (P2) in a first fractionation zone, for example a purification column - contact refrigeration, a residual gas (G2) rich in methane is drawn off at the head, the pressure of which is then raised to a value (P3), it is withdrawn in melts a liquid phase (L2), the phase (L2) is sent to a second fractionation zone, for example a fractionation column, a liquid phase is drawn off at the bottom (L3), enriched in higher hydrocarbons, for example C3 +, a gas phase (G3) is drawn off at the head, at least part of the gas phase
  • the expansion of G1 takes place in a turboexpander which transmits at least part of the energy collected to a turbocharger which raises the pressure of G2 to the value P3.
  • the process of the invention is distinguished, for its fractionation part, from the process of US-A-4 690 702, in that the pressures used in the fractionation zones are higher than those previously used and in that the second fractionation zone operates at a lower pressure than the first fractionation zone.
  • US Pat. No. 4,657,571 discloses a process corresponding to the preamble of claim 1.
  • the gaseous charge of hydrocarbons containing methane and at least one hydrocarbon heavier than methane, under pressure P1 is cooled in one or more stages so as to form at least one gaseous phase G1, the gas phase G1 to lower its pressure from the value P1 to a value P2 lower than P1, the pressure reduction product P la is sent to a first contact fractionation zone, a residual gas G2 enriched in methane is drawn off at the head , a liquid phase L2 is drawn off at the bottom, the liquid phase L2 is sent to a second fractionation zone by distillation operating under a pressure P4 lower than the pressure P2 of the first fractionation zone, it is drawn off at the bottom thereof at least one liquid phase L3, enriched in hydrocarbons heavier than methane, a gas phase G3 is drawn off at the head and it is returned to the first fractionation zone as reflux.
  • At least part of the gas phase G3 is condensed, to produce a condensed phase L4 and the pressure of at least part of the condensed phase L4 is raised, which is sent to the first zone fractionation as reflux and the residual gas G2 is then further cooled under a pressure at least equal to P2; in a methane liquefaction zone, so as to obtain a methane-rich liquid.
  • the gas is initially available under a pressure P1 of at least 5 MPa, preferably at least 6 MPa.
  • P2 0.3 to 0.8 P1
  • P2 being chosen for example between 3.5 and 7 MPa, preferably between 4.5 and 6 MPa.
  • the expansion of G1 is done in one or more turboexpanders coupled (s) to one or more turbocharger (s) which recompresses (s) the waste gas G2 from the pressure P2 to a pressure P3.
  • At least one liquid phase L1 is formed in addition to the gas phase G1, and the liquid phase L1 is sent, after expansion, to said first fractionation zone by contact.
  • the gas phase G3 is completely condensed and a portion is sent to the second fractionation zone as internal reflux and the complement to the first fractionation zone as reflux.
  • the condensation can be completed by further compressing, with subsequent cooling of the said G3 phase.
  • the invention is illustrated by the attached figure.
  • the natural gas from line 1 passes through one or more exchangers 2, for example of the propane or C connection / C3 liquid mixture type, and advantageously one or more exchangers using cold process fluids.
  • the cold fluid comes from line 5 of the first contact column 7.
  • the gas which here is partially liquefied, is fractionated in the flask 4 into liquid conveyed to column 7 via line 6 equipped with a valve.
  • the expansion causes partial liquefaction of the gas and the product of the expansion is sent by line 10 to column 7.
  • This column is of a conventional type, for example at trays or filled. It includes a reboiling circuit 11.
  • the liquid effluent from the bottom of the column is expanded by the valve 12 and sent by line 13 to column 14.
  • This column which operates at a lower pressure than column 7, has a reboiler 15.
  • the vapors are partly or completely condensed in the condenser 17.
  • the phase resulting liquid is returned at least in part to column 14 as reflux by line 18.
  • the gas phase (line 19 and valve V2) is then condensed, preferably entirely, by cooling preferably in the exchanger 20 supplied by minus part of the residual gas at the top of column 7 (lines 21 and 22).
  • valve V2 is closed if all of the vapor phase has been condensed in 17.
  • the valve V3 is open and it is then the liquid phase which is sent to column 7 via line 19a. You can also open the 2 valves V2 and V3 and thus send a mixed phase.
  • the liquid phase resulting from the cooling in the exchanger 20 passes into the balloon 23, the recompression pump 24 and returns to column 7 via line 25 as reflux. If the condensation in the exchanger 20 is not total, which is less preferred, the residual gas can be evacuated by line 26.
  • the waste gas coming from the head of column 7 by line 21, in the form of the aforementioned embodiment, passes through the exchanger 20 before being sent to the turbocharger 27 via the lines 28 and 29.
  • the turbocharger is driven by the turboexpander 9.
  • At least part of the waste gas from line 21 is sent via line 30 to the exchanger 3 to cool the natural gas. It then joins the turbocharger 27 via lines 5 and 29.
  • the waste gas (line 21) passes successively through the exchangers 20 and 3, or vice versa, before joining the turbocharger 27.
  • the gas is sent via line 32, which may include one or more exchangers, not shown, to a conventional methane liquefaction unit, shown here in a simplified manner. It passes through a first cooling exchanger 33, then the expansion valve V4 and a second cooling exchanger 34 where the liquefaction and subcooling are completed.
  • the refrigerant circuit of conventional or improved type (one can for example use the circuit of US-A-4 274 849) is shown here by the use of a multi-component fluid for example a mixture of nitrogen, methane , ethane and propane, initially in the gaseous state (line 35), which is compressed by one or more compressors such as 36, cooled by the external medium, air or water, in one or more exchangers such as 37, further cooled in exchanger 38, for example with propane or a C2 / C3 liquid mixture.
  • a multi-component fluid for example a mixture of nitrogen, methane , ethane and propane, initially in the gaseous state (line 35), which is compressed by one or more compressors such as 36, cooled by the external medium, air or water, in one or more exchangers such as 37, further cooled in exchanger 38, for example with propane or a C2 / C3 liquid mixture.
  • the partially condensed mixture reaches the flask 40 through line 39.
  • the liquid phase passes through line 41 in the exchanger 33, is expanded by the valve 42 and returns to line 35 through the exchanger 33 where it heats up in cooling the streams 32 and 41.
  • the vapor phase of the tank 40 (line 43) passes through the exchangers 33 and 34, where it is condensed, then is expanded in the valve 44 and passes through the exchangers 34 and 33 via the lines 45 and 35.
  • the liquefaction of methane is carried out by indirect contact with one or more fractions of a multicomponent fluid during vaporization and circulating in a closed circuit comprising compression, cooling with liquefaction giving one or more condensates and vaporization. said condensates constituting said multicomponent fluid.
  • a natural gas having the following composition is treated, in mol%: Methane 90.03 Ethane 5.50 Propane 2.10 C4 - C6 2.34 Mercaptans 0.03 100.00 under a pressure of 8 MPa.
  • Reductory gas leaves column 7 at -63 ° C and it is directed partly towards the exchanger 3 and partly towards the exchanger 20. After recompression in 27 using only the energy of the turboexpander 9, the gas pressure is 5.93 MPa.
  • This gas the temperature of which is -28 ° C., has the following% molar composition: Methane 93.90 Ethane 5.51 Propane 0.53 C4 - C6 Mercaptans less than 10 ppm 0.06 100.00
  • This current represents 95.88 mol% of the load current of the installation.
  • Liquefaction takes place as follows: The gas is cooled and condensed to -126 ° C in a first bundle of the heat exchanger 33 then expanded to 1.4 MPa and sub-cooled in a second bundle of the heat exchanger 34 to at -160 ° C. From there it is sent to storage.
  • the refrigerant has the following molar composition: N2 7% Methane 38% Ethane 41% Propane 14%
  • This fluid is compressed to 4.97 MPa, cooled to 40 ° C in a water exchanger 37, then cooled to -25 ° C in the exchangers represented diagrammatically by 38 in indirect contact with a liquid mixture C2 / C3, then fractionated in the separator 40 giving the liquid 41 and gas 43 phases.
  • the gas phase is condensed and cooled to -126 ° C in a second bundle of the exchanger 33 then sub-cooled to -160 ° C in a bundle of the exchanger 34.
  • the pressure is 0.3 MPa and the temperature is -28 ° C.

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Description

L'invention concerne un procédé de liquéfaction de gaz naturel comportant la séparation d'hydrocarbures plus lourds que le méthane.The invention relates to a natural gas liquefaction process comprising the separation of hydrocarbons heavier than methane.

Le gaz naturel et les autres courants gazeux riches en méthane sont couramment disponibles en des sites éloignés des lieux d'utilisation, et il est donc courant de liquéfier le gaz naturel afin de le transporter par terre ou par mer. La liquéfaction est largement pratiquée à l'heure actuelle et la littérature et les brevets décrivent de nombreux procédés et appareils de liquéfaction. Les brevets US-A-3945 214, 4251 247, 4274 849, 4339 253 et 4539 028 sont des exemples de tels procédés.Natural gas and other methane-rich gas streams are commonly available at sites away from places of use, and it is therefore common to liquefy natural gas for transportation by land or sea. Liquefaction is widely practiced in the present day and the literature and patents describe numerous processes and apparatuses for liquefaction. US-A-3945 214, 4251 247, 4274 849, 4339 253 and 4539 028 are examples of such methods.

Il est également connu de fractionner les courants d'hydrocarbures légers, renfermant par exemple du méthane et au moins un hydrocarbure supérieur tel que éthane à hexane ou supérieur, par cryogénie.It is also known to fractionate the streams of light hydrocarbons, containing for example methane and at least one higher hydrocarbon such as ethane to hexane or higher, by cryogenics.

Ainsi le brevet US-A-4690 702 décrit un procédé dans lequel la charge d'hydrocarbures sous pression élevée (P₁) est refroidie de manière à provoquer la liquéfaction d'une partie des hydrocarbures, on sépare une phase gazeuse (G₁) d'une phase liquide (L₁), on détend la phase gazeuse (G₁) pour abaisser sa pression à une valeur (P₂) plus basse que (P₁), on envoie la phase liquide (L₁) et la phase gazeuse (G₁) sous la pression (P₂) dans une première zone de fractionnement, par exemple une colonne de purification - réfrigération par contact, on soutire en tête un gaz résiduaire (G₂) riche en méthane dont on élève ensuite la pression à une valeur (P₃), on soutire en fond une phase liquide (L₂), on envoie la phase (L₂) dans une seconde zone de fractionnement, par exemple une colonne de fractionnement, on soutire en fond une phase liquide (L₃), enrichie en hydrocarbures supérieurs par exemple C₃+, on soutire en tête une phase gazeuse (G₃), on condense au moins une partie de la phase gazeuse (G₃) et on envoie au moins une partie de la phase liquide condensée résultante (L₄) comme alimentation supplémentaire en tête de la première zone de fractionnement. Dans ce procédé, la seconde zone de fractionnement fonctionne à une pression (P₄) supérieure à la pression de la première zone de fractionnement, par exemple 0,5 MPa pour la première zone et 0,66 MPa pour la seconde zone.Thus, US Pat. No. 4,690,702 describes a process in which the charge of hydrocarbons under high pressure (P₁) is cooled so as to cause the liquefaction of part of the hydrocarbons, a gas phase (G₁) is separated from a liquid phase (L₁), the gas phase is relaxed (G₁) to lower its pressure to a value (P₂) lower than (P₁), the liquid phase (L₁) and the gas phase (G₁) are sent under pressure (P₂) in a first fractionation zone, for example a purification column - contact refrigeration, a residual gas (G₂) rich in methane is drawn off at the head, the pressure of which is then raised to a value (P₃), it is withdrawn in melts a liquid phase (L₂), the phase (L₂) is sent to a second fractionation zone, for example a fractionation column, a liquid phase is drawn off at the bottom (L₃), enriched in higher hydrocarbons, for example C₃ +, a gas phase (G₃) is drawn off at the head, at least part of the gas phase (G₃) is condensed and at least part of the resulting condensed liquid phase is sent (L₄) as additional feed at the head of the first fractionation zone. In this method, the second fractionation zone operates at a pressure (P₄) greater than the pressure of the first fractionation zone, for example 0.5 MPa for the first zone and 0.66 MPa for the second zone.

Avantageusement, dans le procédé précité, la détente de G₁ se fait dans un turbodétendeur qui transmet au moins une partie de l'énergie recueillie à un turbocompresseur qui élève la pression de G₂ jusqu'à la valeur P₃.Advantageously, in the aforementioned method, the expansion of G₁ takes place in a turboexpander which transmits at least part of the energy collected to a turbocharger which raises the pressure of G₂ to the value P₃.

L'intérêt d'un tel procédé est de recueillir, avec un rendement élevé, des condensats tels que C₃, C₄, essence, etc... qui sont des produits de valeur.The advantage of such a process is to collect, with a high yield, condensates such as C₃, C₄, petrol, etc. which are valuable products.

On a déjà proposé d'associer une unité de fractionnement de gaz naturel à une unité de liquéfaction, de manière à pouvoir recueillir à la fois du méthane liquide et des condensats tels que C₃, C₄ et/ou supérieurs. De telles propositions sont faites par exemple dans US-A-3 763 658 et US-A-4 065 278, l'unité de liquéfaction pouvant être d'un type conventionnel.It has already been proposed to associate a natural gas fractionation unit with a liquefaction unit, so as to be able to collect both liquid methane and condensates such as C₃, C₄ and / or higher. Such proposals are made for example in US-A-3,763,658 and US-A-4,065,278, the liquefaction unit can be of a conventional type.

La difficulté à surmonter, dans ce type d'installation, est d'obtenir un coût de fonctionnement réduit. En particulier, il est inévitable de recueillir le gaz recomprimé sous une pression (P₃) plus faible que celle (P₁) sous laquelle il se trouvait initialement, à moins de consommer de l'énergie supplémentaire. Or la liquéfaction ultérieure du méthane est d'autant plus aisée que sa pression est plus élevée.The difficulty to be overcome in this type of installation is to obtain a reduced operating cost. In particular, it is inevitable to collect the recompressed gas under a pressure (P₃) lower than that (P₁) under which it was initially, unless consuming additional energy. Now the subsequent liquefaction of methane is all the easier as its pressure is higher.

Il y a donc place dans la technique pour un procédé économique de fractionnement d'hydrocarbures du gaz naturel et liquéfaction subséquente du méthane.There is therefore room in the art for an economical process for fractionating hydrocarbons from natural gas and subsequent liquefaction of methane.

Le procédé de l'invention se distingue, pour sa partie fractionnement, du procédé de US-A-4 690 702, en ce que les pressions mises en oeuvre dans les zones de fractionnement sont plus élevées que celles précédemment utilisées et en ce que la seconde zone de fractionnement opère sous une pression plus faible que la première zone de fractionnement.The process of the invention is distinguished, for its fractionation part, from the process of US-A-4 690 702, in that the pressures used in the fractionation zones are higher than those previously used and in that the second fractionation zone operates at a lower pressure than the first fractionation zone.

Par ailleurs, le brevet US-A-4 657 571 révèle un procédé correspondant au préambule de la revendication 1.Furthermore, US Pat. No. 4,657,571 discloses a process corresponding to the preamble of claim 1.

Selon l'invention, la charge gazeuse d'hydrocarbures renfermant du méthane et au moins un hydrocarbure plus lourd que le méthane, sous pression P₁, est refroidie en une ou plusieurs étapes de manière à former au moins une phase gazeuse G₁, on détend la phase gazeuse G₁ pour abaisser sa pression de la valeur P₁ à une valeur P₂ plus basse que P₁, on envoie le produit de la détente sous pression P₂ dans une première zone de fractionnement par contact, on soutire en tête un gaz résiduaire G₂ enrichi en méthane, on soutire en fond une phase liquide L₂, on envoie la phase liquide L₂ dans une seconde zone de fractionnement par distillation opérant sous une pression P₄ plus basse que la pression P₂ de la première zone de fractionnement, on soutire en fond de celle-ci au moins une phase liquide L₃, enrichie en hydrocarbures plus lourds que le méthane, on soutire en tête une phase gazeuse G₃ et on le renvoie à la première zone de fractionnement comme reflux.According to the invention, the gaseous charge of hydrocarbons containing methane and at least one hydrocarbon heavier than methane, under pressure P₁, is cooled in one or more stages so as to form at least one gaseous phase G₁, the gas phase G₁ to lower its pressure from the value P₁ to a value P₂ lower than P₁, the pressure reduction product P la is sent to a first contact fractionation zone, a residual gas G₂ enriched in methane is drawn off at the head , a liquid phase L₂ is drawn off at the bottom, the liquid phase L₂ is sent to a second fractionation zone by distillation operating under a pressure P₄ lower than the pressure P₂ of the first fractionation zone, it is drawn off at the bottom thereof at least one liquid phase L₃, enriched in hydrocarbons heavier than methane, a gas phase G₃ is drawn off at the head and it is returned to the first fractionation zone as reflux.

Selon la caractéristique de l'invention, on condense au moins une partie de la phase gazeuse G₃, pour produire une phase condensée L₄ et on élève la pression d'au moins une partie de la phase condensée L₄ qu'on envoie à la première zone de fractionnement comme reflux et on refroidit ensuite davantage le gaz résiduaire G₂ sous une pression au moins égale à P₂; dans une zone de liquéfaction du méthane, de manière à obtenir un liquide riche en méthane.According to the characteristic of the invention, at least part of the gas phase G₃ is condensed, to produce a condensed phase L₄ and the pressure of at least part of the condensed phase L₄ is raised, which is sent to the first zone fractionation as reflux and the residual gas G₂ is then further cooled under a pressure at least equal to P₂; in a methane liquefaction zone, so as to obtain a methane-rich liquid.

A titre d'exemple, le gaz est initialement disponible sous une pression P₁ d'au moins 5 MPa, de préférence au moins 6 MPa.By way of example, the gas is initially available under a pressure P₁ of at least 5 MPa, preferably at least 6 MPa.

Lors de la détente, on amène utilement sa pression à une valeur P₂ telle que P₂ = 0,3 à 0,8 P₁, P₂ étant choisi par exemple entre 3,5 et 7 MPa, de préférence entre 4,5 et 6 MPa. La pression P₄ de la seconde zone de fractionnement est avantageusement telle que P₄ = 0,3 à 0,9 P₂, P₄ ayant une valeur comprise par exemple entre 0,5 et 4,5 MPa, de préférence entre 2,5 et 3,5 MPa.During expansion, its pressure is usefully brought to a value P₂ such that P₂ = 0.3 to 0.8 P₁, P₂ being chosen for example between 3.5 and 7 MPa, preferably between 4.5 and 6 MPa. The pressure P₄ of the second fractionation zone is advantageously such that P₄ = 0.3 to 0.9 P₂, P₄ having a value for example between 0.5 and 4.5 MPa, preferably between 2.5 and 3, 5 MPa.

Plusieurs modes de réalisation peuvent être mis en oeuvre.Several embodiments can be implemented.

Selon un mode de réalisation préféré, la détente de G₁ se fait dans un ou plusieurs turbodétendeurs accouplé(s) à un ou plusieurs turbocompresseur(s) qui recomprime(nt) le gaz résiduaire G₂ de la pression P₂ à une pression P₃.According to a preferred embodiment, the expansion of G₁ is done in one or more turboexpanders coupled (s) to one or more turbocharger (s) which recompresses (s) the waste gas G₂ from the pressure P₂ to a pressure P₃.

Selon un autre mode de réalisation préféré, au cours du refroidissement initial du gaz, on forme au moins une phase liquide L₁ en plus de la phase gazeuse G₁, et on envoie la phase liquide L₁, après détente, dans ladite première zone de fractionnement par contact.According to another preferred embodiment, during the initial cooling of the gas, at least one liquid phase L₁ is formed in addition to the gas phase G₁, and the liquid phase L₁ is sent, after expansion, to said first fractionation zone by contact.

Selon une autre variante, on condense en totalité la phase gazeuse G₃ et on envoie une partie à la seconde zone de fractionnement comme reflux interne et le complément à la première zone de fractionnement comme reflux. Pour arriver à ce résultat, on peut agir sur le rebouilleur de la première zone de fractionnement, de manière à contrôler le rapport C₁/C₂ de la phase liquide L₃.According to another variant, the gas phase G₃ is completely condensed and a portion is sent to the second fractionation zone as internal reflux and the complement to the first fractionation zone as reflux. To achieve this result, one can act on the reboiler of the first fractionation zone, so as to control the ratio C rapport / C₂ of the liquid phase L₃.

Si le refroidissement de la phase G₃ n'est pas suffisant pour condenser totalement cette phase, ce qui est préféré, on peut compléter la condensation en comprimant davantage, avec refroidissement subséquent ladite phase G₃.If the cooling of the G₃ phase is not sufficient to fully condense this phase, which is preferred, the condensation can be completed by further compressing, with subsequent cooling of the said G₃ phase.

L'invention est illustrée par la figure jointe. Le gaz naturel de la conduite 1 traverse un ou plusieurs échangeurs 2, par exemple du type à propane ou mélange liquide C₂/C₃, et avantageusement un ou plusieurs échangeurs utilisant des fluides froids du procédé. De préférence, le fluide froid provient par la ligne 5 de la première colonne de contact 7. Le gaz, qui est ici partiellement liquéfié, est fractionné dans le ballon 4 en liquide acheminé à la colonne 7 par la ligne 6 équipée d'une vanne V₁ et en gaz acheminé par la ligne 8 au turbodétendeur 9. La détente provoque une liquéfaction partielle du gaz et le produit de la détente est envoyé par la ligne 10 à la colonne 7. Cette colonne est d'un type classique, par exemple à plateaux ou à garnissage. Elle comporte un circuit de rebouillage 11. L'effluent liquide du fond de colonne est détendu par la vanne 12 et envoyé par la ligne 13 à la colonne 14. Cette colonne, qui fonctionne à pression plus basse que la colonne 7, possède un rebouilleur 15. L'effluent liquide, enrichi en hydrocarbures supérieurs au méthane, par exemple C₃+, sort par la ligne 16. En tête, les vapeurs sont condensées en partie ou totalité dans le condensateur 17. La phase liquide résultante est renvoyée au moins en partie à la colonne 14 comme reflux par la ligne 18. La phase gazeuse (ligne 19 et vanne V₂) est condensée ensuite, de préférence en totalité, par refroidissement de préférence dans l'échangeur 20 alimenté par au moins une partie du gaz résiduaire de tête de la colonne 7 (lignes 21 et 22).The invention is illustrated by the attached figure. The natural gas from line 1 passes through one or more exchangers 2, for example of the propane or C mélange / C₃ liquid mixture type, and advantageously one or more exchangers using cold process fluids. Preferably, the cold fluid comes from line 5 of the first contact column 7. The gas, which here is partially liquefied, is fractionated in the flask 4 into liquid conveyed to column 7 via line 6 equipped with a valve. V₁ and in gas supplied by line 8 to the turboexpander 9. The expansion causes partial liquefaction of the gas and the product of the expansion is sent by line 10 to column 7. This column is of a conventional type, for example at trays or filled. It includes a reboiling circuit 11. The liquid effluent from the bottom of the column is expanded by the valve 12 and sent by line 13 to column 14. This column, which operates at a lower pressure than column 7, has a reboiler 15. The liquid effluent, enriched in hydrocarbons higher than methane, for example C₃ +, leaves via line 16. At the top, the vapors are partly or completely condensed in the condenser 17. The phase resulting liquid is returned at least in part to column 14 as reflux by line 18. The gas phase (line 19 and valve V₂) is then condensed, preferably entirely, by cooling preferably in the exchanger 20 supplied by minus part of the residual gas at the top of column 7 (lines 21 and 22).

En variante, la vanne V₂ est fermée si la totalité de la phase vapeur a été condensée dans 17. La vanne V₃ est ouverte et c'est alors la phase liquide qui est envoyée vers la colonne 7 par la ligne 19a. On peut aussi ouvrir les 2 vannes V₂ et V₃ et envoyer ainsi une phase mixte.As a variant, the valve V₂ is closed if all of the vapor phase has been condensed in 17. The valve V₃ is open and it is then the liquid phase which is sent to column 7 via line 19a. You can also open the 2 valves V₂ and V₃ and thus send a mixed phase.

La phase liquide résultant du refroidissement dans l'échangeur 20 passe dans le ballon 23, la pompe de recompression 24 et retourne à la colonne 7 par la ligne 25 comme reflux. Si la condensation dans l'échangeur 20 n'est pas totale, ce qui est moins préféré, le gaz résiduel peut être évacué par la ligne 26. Le gaz résiduaire issu de la tête de la colonne 7 par la ligne 21, dans la forme de réalisation précitée, passe par l'échangeur 20 avant d'être envoyé au turbocompresseur 27 par les lignes 28 et 29. Le turbocompresseur est entraîné par le turbodétendeur 9.The liquid phase resulting from the cooling in the exchanger 20 passes into the balloon 23, the recompression pump 24 and returns to column 7 via line 25 as reflux. If the condensation in the exchanger 20 is not total, which is less preferred, the residual gas can be evacuated by line 26. The waste gas coming from the head of column 7 by line 21, in the form of the aforementioned embodiment, passes through the exchanger 20 before being sent to the turbocharger 27 via the lines 28 and 29. The turbocharger is driven by the turboexpander 9.

Selon une variante, une partie au moins du gaz résiduaire de la ligne 21 est envoyé par la ligne 30 à l'échangeur 3 pour refroidir le gaz naturel. Il rejoint alors le turbocompresseur 27 par les lignes 5 et 29.Alternatively, at least part of the waste gas from line 21 is sent via line 30 to the exchanger 3 to cool the natural gas. It then joins the turbocharger 27 via lines 5 and 29.

Dans une autre variante non-représentée, le gaz résiduaire (ligne 21) passe successivement dans les échangeurs 20 et 3, ou inversement, avant de rejoindre le turbocompresseur 27.In another variant not shown, the waste gas (line 21) passes successively through the exchangers 20 and 3, or vice versa, before joining the turbocharger 27.

D'autres arrangements peuvent être prévus, ainsi que le comprendront les spécialistes, permettant d'assurer le refroidissement nécessaire au gaz des lignes 1 et 19. On peut par exemple envoyer directement le gaz de la ligne 21 au compresseur 27 par la ligne 31 et assurer différemment le refroidissement des échangeurs 3 et 20.Other arrangements can be provided, as will be understood by specialists, making it possible to ensure the necessary cooling of the gas from lines 1 and 19. It is possible, for example, to directly send the gas from line 21 to the compressor 27 via line 31 and provide different cooling for exchangers 3 and 20.

Après recompression dans le turbocompresseur 27, le gaz est envoyé par la ligne 32, pouvant comporter un ou plusieurs échangeurs non-représentés, à une unité conventionnelle de liquéfaction du méthane, représentée ici de façon simplifiée. Il traverse un premier échangeur de refroidissement 33, puis la vanne de détente V₄ et un second échangeur de refroidissement 34 où s'achèvent la liquéfaction et le sous-refroidissement. Le circuit frigorigène, de type conventionnel ou perfectionné (on peut par exemple utiliser le circuit de US-A-4 274 849) est schématisé ici par l'emploi d'un fluide multi-composants par exemple un mélange d'azote, de méthane, éthane et propane, initialement à l'état gazeux (ligne 35), qui est comprimé par un ou plusieurs compresseurs tels que 36, refroidi par le milieu extérieur, air ou eau, dans un ou plusieurs échangeurs tels que 37, refroidi davantage dans l'échangeur 38, par exemple par du propane ou un mélange C₂/C₃ liquide. Le mélange partiellement condensé parvient au ballon 40 par la ligne 39. La phase liquide passe par la ligne 41 dans l'échangeur 33, est détendue par la vanne 42 et retourne vers la ligne 35 en traversant l'échangeur 33 où elle se réchauffe en refroidissant les courants 32 et 41. La phase vapeur du ballon 40 (ligne 43) traverse les échangeurs 33 et 34, où elle est condensée, puis est détendue dans la vanne 44 et traverse les échangeurs 34 et 33 par les lignes 45 et 35.After recompression in the turbocharger 27, the gas is sent via line 32, which may include one or more exchangers, not shown, to a conventional methane liquefaction unit, shown here in a simplified manner. It passes through a first cooling exchanger 33, then the expansion valve V₄ and a second cooling exchanger 34 where the liquefaction and subcooling are completed. The refrigerant circuit, of conventional or improved type (one can for example use the circuit of US-A-4 274 849) is shown here by the use of a multi-component fluid for example a mixture of nitrogen, methane , ethane and propane, initially in the gaseous state (line 35), which is compressed by one or more compressors such as 36, cooled by the external medium, air or water, in one or more exchangers such as 37, further cooled in exchanger 38, for example with propane or a C₂ / C₃ liquid mixture. The partially condensed mixture reaches the flask 40 through line 39. The liquid phase passes through line 41 in the exchanger 33, is expanded by the valve 42 and returns to line 35 through the exchanger 33 where it heats up in cooling the streams 32 and 41. The vapor phase of the tank 40 (line 43) passes through the exchangers 33 and 34, where it is condensed, then is expanded in the valve 44 and passes through the exchangers 34 and 33 via the lines 45 and 35.

Sous forme résumée, la liquéfaction du méthane est réalisée par mise en contact indirect avec une ou plusieurs fractions d'un fluide multicomposants en cours de vaporisation et circulant en circuit fermé comprenant une compression, un refroidissement avec liquéfaction donnant un ou plusieurs condensats et la vaporisation desdits condensats constituant ledit fluide multicomposants.In summary form, the liquefaction of methane is carried out by indirect contact with one or more fractions of a multicomponent fluid during vaporization and circulating in a closed circuit comprising compression, cooling with liquefaction giving one or more condensates and vaporization. said condensates constituting said multicomponent fluid.

A titre d'exemple non limitatif, on traite un gaz naturel ayant la composition suivante, en % molaire : Méthane 90,03 Ethane 5,50 Propane 2,10 C₄ - C₆ 2,34 Mercaptans 0,03 100,00
   sous une pression de 8 MPa.By way of nonlimiting example, a natural gas having the following composition is treated, in mol%: Methane 90.03 Ethane 5.50 Propane 2.10 C₄ - C₆ 2.34 Mercaptans 0.03 100.00
under a pressure of 8 MPa.

Après refroidissement par du propane liquide et par l'effluent de tête de la colonne 7, le gaz parvient au ballon 4 à la température de -42°C. La phase liquide est envoyée par la ligne 6 à la colonne 7, et la phase gazeuse détendue par le turbodétendeur jusqu'à 5 MPa. La phase liquide collectée (ligne 13) à la température de + 25°C est détendue jusqu'à 3,4 MPa dans la vanne 12 puis fractionnée dans la colonne 14 qui reçoit le reflux de la ligne 18. Cette colonne 14 a une température de fond de 130°C et une température tête de -13°C.After cooling with liquid propane and with the top effluent from column 7, the gas reaches the flask 4 at the temperature of -42 ° C. The liquid phase is sent via line 6 to column 7, and the gaseous phase expanded by the turboexpander up to 5 MPa. The liquid phase collected (line 13) at the temperature of + 25 ° C. is expanded to 3.4 MPa in the valve 12 and then fractionated in column 14 which receives the reflux from line 18. This column 14 has a temperature bottom temperature of 130 ° C and a head temperature of -13 ° C.

Le gaz rédisuaire sort de la colonne 7 à -63°C et il est dirigé en partie vers l'échangeur 3 et en partie vers l'échangeur 20. Après recompression dans 27 utilisant uniquement l'énergie du turbodétendeur 9, la pression du gaz est de 5,93 MPa. Ce gaz, dont la température est de -28°C, présente la composition molaire % suivante : Méthane 93,90 Ethane 5,51 Propane 0,53 C₄ - C₆ Mercaptans inférieur à 10 ppm 0,06 100,00 Reductory gas leaves column 7 at -63 ° C and it is directed partly towards the exchanger 3 and partly towards the exchanger 20. After recompression in 27 using only the energy of the turboexpander 9, the gas pressure is 5.93 MPa. This gas, the temperature of which is -28 ° C., has the following% molar composition: Methane 93.90 Ethane 5.51 Propane 0.53 C₄ - C₆ Mercaptans less than 10 ppm 0.06 100.00

Ce courant représente 95,88% molaire du courant de charge de l'installation.This current represents 95.88 mol% of the load current of the installation.

On constate que l'installation a permis d'éliminer la quasi-totalité des mercaptans du gaz à liquéfier.It can be seen that the installation made it possible to eliminate almost all of the mercaptans from the gas to be liquefied.

La liquéfaction a lieu comme suit :
   Le gaz est refroidi et condensé jusqu'à -126°C dans un premier faisceau de l'échangeur de chaleur 33 puis détendu jusqu'à 1,4 MPa et sous-refroidi dans un second faisceau de l'échangeur de chaleur 34 jusqu'à -160°C. De là il est envoyé au stockage.Liquefaction takes place as follows:
The gas is cooled and condensed to -126 ° C in a first bundle of the heat exchanger 33 then expanded to 1.4 MPa and sub-cooled in a second bundle of the heat exchanger 34 to at -160 ° C. From there it is sent to storage.

Le fluide réfrigérant a la composition molaire suivante : N2 7% Méthane 38% Ethane 41% Propane 14% The refrigerant has the following molar composition: N2 7% Methane 38% Ethane 41% Propane 14%

Ce fluide est comprimé jusqu'à 4,97 MPa, refroidi à 40°C dans un échangeur à eau 37, puis refroidi jusqu'à -25°C dans les échangeurs représentés schématiquement par 38 au contact indirect d'un mélange liquide C₂/C₃, puis fractionné dans le séparateur 40 en donnant les phases liquide 41 et gazeuse 43. La phase gazeuse est condensée et refroidie à -126°C dans un second faisceau de l'échangeur 33 puis sous-refroidie jusqu'à -160°C dans un faisceau de l'échangeur 34. Après détente à 0,34 MPa, elle sert à refroidir le gaz naturel et revient au compresseur 36 après avoir traversé la calandre de chacun des échangeurs 34 et 33 et avoir reçu le courant liquide de la ligne 41 qui a traversé la vanne 42 après avoir été sous-refroidi à -126°C dans 33.This fluid is compressed to 4.97 MPa, cooled to 40 ° C in a water exchanger 37, then cooled to -25 ° C in the exchangers represented diagrammatically by 38 in indirect contact with a liquid mixture C₂ / C₃, then fractionated in the separator 40 giving the liquid 41 and gas 43 phases. The gas phase is condensed and cooled to -126 ° C in a second bundle of the exchanger 33 then sub-cooled to -160 ° C in a bundle of the exchanger 34. After expansion to 0.34 MPa, it is used to cool the natural gas and returns to the compressor 36 after having passed through the shell of each of the exchangers 34 and 33 and having received the liquid current from the line 41 which passed through the valve 42 after being sub-cooled to -126 ° C in 33.

A l'entrée du compresseur (ligne 35), la pression est de 0,3 MPa et la température de -28°C.At the compressor inlet (line 35), the pressure is 0.3 MPa and the temperature is -28 ° C.

A titre de comparaison, toutes choses sensiblement égales par ailleurs, quand on fait fonctionner la colonne 7 à 3,3 MPa avec une température de +1°C en fond et -64°C en tête et la colonne 14 à 3,5 MPa, avec une température de 131°C en fond et -11,7°C en tête, c'est-à-dire dans des conditions qui se déduisent de l'enseignement du brevet US-A-4 690 702, déjà nommé, la pression du gaz à la sortie du turbocompresseur 27 atteint seulement 5,33 MPa, et la température -24°C, ce qui est beaucoup moins avantageux pour la liquéfaction subséquente et nécessitera une dépense d'énergie nettement plus importante.By way of comparison, all other things being substantially equal, when column 7 is operated at 3.3 MPa with a temperature of + 1 ° C at the bottom and -64 ° C at the head and column 14 at 3.5 MPa , with a temperature of 131 ° C. at the bottom and -11.7 ° C. at the head, that is to say under conditions which are deduced from the teaching of the patent US Pat. No. 4,690,702, already named, the gas pressure at the outlet of the turbocharger 27 reaches only 5.33 MPa, and the temperature -24 ° C, which is much less advantageous for the subsequent liquefaction and will require a much higher energy expenditure.

Claims (9)

  1. Method for liquefying natural gas, according to which said gas including methane and a hydrocarbon heavier than the methane under a pressure P₁, is cooled in view to form at least a gaseous phase G₁, one decreases the pressure of the gaseous phase G₁ to lower its pressure and to bring it to a value P₂ which is smaller than P₁, one sends the product of the pressure decrease at a pressure P₂ in a first zone of fractionation by contact, one draws off at the head a rest gas G₂ enriched with methane, one draws off at the bottom a liquid phase L₂, one sends the liquid phase L₂ in a second zone for fractionation by distillation working at a pressure P₄ lower than the pressure P₂ of the first fractionation zone, one draws off at the bottom of the second fractionation zone at least a liquid phase L₃ enriched with hydrocarbons which are heavier than the methane, one draws off at the head of the second fractionation zone a gaseous phase G₃ and send it back to the first fractionation zone as flow back, characterized in that one performs said flow-back by condensating at least a part of the gaseous phase G₃ in view to produce a condensated phase L₄ and by increasing the pressure of at least a part of the condensated phase L₄ one sends as flow-back to the first fractionation zone, and in that one cools then further the residual gas G₂ at a pressure at least equal to P₂, in a methane liquefaction zone, in view to get a liquid enriched with methane.
  2. Method according to claim 1, wherein one performs the pressure decrease of the gaseous phase G₁ in a turbo pressure reducing means and performs the pressure increase of the residual gas from the value P₂ to a value P₃ in a turbocompressor and uses the energy furnished by the pressure decrease for actioning the turbocompressor.
  3. Method according to claim 1 or 2, wherein the pressure P₁ is at least equal to 5 MPa, the pressure P₂ is such that P₂ = 0.3 to 0.8 P₁ with P₂ between 3.5 and 7 MPa, and the pressure P₄ is such that P₄ = 0.3 to 0.9 P₂, with P₄ between 0.5 and 4.5 MPa.
  4. Method according to claim 3, wherein P₁ is at least equal to 6 MPa, P₂ being between 4.5 and 6 MPa and P₄ being between 2.5 and 3.5 MPa.
  5. Method according to any of claims 1 to 4, wherein at least a part of the residual gas G₂ exchanges heat with the natural gas in view to contribute to the cooling thereof, before the increase of the pressure of the gas G₂ from P₂ to P₃.
  6. Method according to any of claims 1 to 5, wherein at least a part of the residual gas G₂ exchanges heat with at least a part of the gaseous phase G₃ for cooling the same and produce the condensed phase L₄.
  7. Method according to any of claims 1 to 6, wherein the liquefying of the methane is performed by putting into indirect contact with one or a multitude of fractions of a multicomponent fluid during the vaporization and circulation in a closed circuit comprising a compression zone, a cooling zone with liquefaction producing one or a multitude of condensates and a vaporization zone of said condensates for reconstituting said multicomponent fluid.
  8. Method according to any of claims 1 to 7, wherein during the initial cooling of the gas, one forms at least one liquid phase L₁ supplementary to the gaseous phase G₁ and sends the liquid phase L₁ after pressure decrease in said first fractionation zone.
  9. Method according to any of claims 1 to 8, wherein one condenses completely the gaseous phase G₃ and sends a part thereof to the second fractionation zone as internal flow-back and the complement to the first fractionation zone as flow-back.
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NO923783D0 (en) 1992-09-29
NO177840B (en) 1995-08-21
EG20248A (en) 1998-05-31
DE69206232T2 (en) 1996-07-18
SA92130161B1 (en) 2004-05-29
JP3187160B2 (en) 2001-07-11
RU2093765C1 (en) 1997-10-20
AU2612792A (en) 1993-04-01
NZ244542A (en) 1994-07-26
JPH05240576A (en) 1993-09-17
AR247945A1 (en) 1995-04-28
DZ1625A1 (en) 2002-02-17
CA2079407A1 (en) 1993-03-31
MY107837A (en) 1996-06-29
FR2681859A1 (en) 1993-04-02
CA2079407C (en) 2001-05-15
FR2681859B1 (en) 1994-02-11
NO177840C (en) 1995-11-29
US5291736A (en) 1994-03-08
EP0535752A1 (en) 1993-04-07
AU648695B2 (en) 1994-04-28
ES2089373T3 (en) 1996-10-01
NO923783L (en) 1993-03-31
DE69206232D1 (en) 1996-01-04

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