EP0373983B1 - Verfahren zur gleichzeitigen Ausscheidung von CO2 und Bearin aus Methan, C2 und höheren Kohlenwasserstoffen und CO2 enthatenden gasförmigen Kohlenwasserstoffen - Google Patents

Verfahren zur gleichzeitigen Ausscheidung von CO2 und Bearin aus Methan, C2 und höheren Kohlenwasserstoffen und CO2 enthatenden gasförmigen Kohlenwasserstoffen Download PDF

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EP0373983B1
EP0373983B1 EP89403123A EP89403123A EP0373983B1 EP 0373983 B1 EP0373983 B1 EP 0373983B1 EP 89403123 A EP89403123 A EP 89403123A EP 89403123 A EP89403123 A EP 89403123A EP 0373983 B1 EP0373983 B1 EP 0373983B1
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Prior art keywords
solvent
rich
methane
gas
hydrocarbons
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EP89403123A
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English (en)
French (fr)
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EP0373983A1 (de
Inventor
Claude Blanc
Henri Paradowski
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Elf Exploration Production SAS
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Societe National Elf Aquitaine
Societe Nationale Elf Aquitaine Production SA
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Priority to EP93107550A priority Critical patent/EP0556875B1/de
Priority to AT89403123T priority patent/ATE100852T1/de
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C10G5/04—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas with liquid absorbents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1025—Natural gas

Definitions

  • the invention relates to a process for the simultaneous decarbonation and degassing of a gaseous mixture consisting mainly of hydrocarbons consisting of methane and C2 and higher hydrocarbons and also containing CO2 and optionally one or more non-sulfurized compounds with low boiling point such as H2, CO, N2 and argon.
  • decarbonation and degassing operations are generally carried out separately and are part of a succession of operations carried out on the gas mixture to be treated and mainly comprising an elimination of the acid gas CO2, drying, adsorption of water on an appropriate solid such as a molecular sieve, separation by cryogenic distillation between -30 ° C and - 90 ° C associated or not with extraction by a solvent in order to obtain the cut of natural gas liquid, and finally reheating the treated gas to ambient temperature in order to generally supply the commercial gas network.
  • the dehydrated and refrigerated natural gas is separated, in a first column (demethanizer) at the head of which is injected an additive consisting of a liquid fraction of C4 hydrocarbons and more, into a gas phase containing methane and lighter compounds and a liquid fraction containing C2 and higher hydrocarbons and CO2.
  • This liquid fraction is separated, in a second column (de-ethanizer) into which a certain amount of the additive is also introduced, into a top fraction consisting of CO2 and a bottom fraction containing the hydrocarbons in C2 and more.
  • Said tail fraction is then separated, in a third column, into an overhead fraction consisting of a liquid cut of C2 to C4 hydrocarbons and into a tail fraction consisting of a liquid cut of C4 and higher hydrocarbons, which contains the major part of the butanes and higher hydrocarbons present in the treated natural gas and of which the appropriate quantity is taken to constitute the additive injected in the first and second columns.
  • This additive avoids the crystallization of CO2 at the top of the demethanizer and ensures the rupture of the azeotrope which forms between ethane and CO2 and facilitates the separation of this compound in the deethanizer.
  • the aforementioned process is therefore essentially based on serial distillation operations.
  • the invention provides a process for simultaneous decarbonation and degassing of gas mixtures, which are available under an absolute pressure greater than 0.5 MPa and consist mainly of hydrocarbons consisting of methane and C2 and higher hydrocarbons and also contain CO2 and optionally one or more non-sulfurized compounds with low boiling point such as H2, CO, N2 and argon, such gas mixtures being for example of the natural gas type, said process making it possible to reach more easily and at lower cost, by comparison with known processes, the objective of separating the gaseous mixture into the three components, namely treated gas consisting mainly of methane, liquid cut of hydrocarbons with predominantly C3 and more hydrocarbons and containing as required a quantity more or less important ethane and CO2 current, which have the specifications defined above.
  • the process according to the invention is of the type of process which is described in the US-A-3770622 citation and in which the gas mixture is brought into contact, in a washing zone, with a solvent consisting of a liquid which preferentially dissolves CO2 and hydrocarbons in C2 and above and which has on the one hand, at atmospheric pressure, a boiling temperature greater than 40 ° C and on the other hand, at - 30 ° C, a viscosity less than 0.1 Pa .s, operating at a sufficiently low temperature and with a ratio of the flow rates of the gaseous mixture to be treated and of the solvent such that a treated gas consisting mainly of methane and having a molar CO2 content is produced at most equal to 2% and, on the other hand, a liquid phase called rich solvent and formed of the solvent enriched in CO2 and in a fraction of C en hydrocarbons and more containing at least 80 mol% of the C en hydrocarbons and more present in the mixture g nitrogenous to be treated, the rich solvent is
  • the process according to the invention differs from the process of the US-A-3770622 citation, and is therefore characterized in that the treatment of the demethanized rich solvent is carried out by subjecting said demethanized rich solvent, previously subjected to refrigeration, to a liquid / liquid extraction, in an extraction zone, using a refrigerated hydrocarbon solvent with production, on the one hand, of a purified solvent, which contains almost all of the CO2 present in the demethanized rich solvent and has a hydrocarbon content, expressed in methane equivalent, of less than 10 mol% relative to CO2, and, on the other hand, of a hydrocarbon solvent enriched in C2 hydrocarbons and more, by fractionating said enriched hydrocarbon solvent by distillation and a fraction of C2 and higher hydrocarbons, which constitutes the hydrocarbon fraction and contains at least 80 mol% of the C3 and more hydrocarbons present in the gas mixture to be treated, and in the regenerated hydrocarbon solvent, which is recycled after refrigeration, in the extraction zone, and by subjecting the purified solvent
  • methane equivalent is meant according to the invention as many pseudo-molecules with a single carbon atom as there are carbon atoms in the considered hydrocarbon molecule.
  • the solvent which is generally defined above for bringing it into contact with the gaseous mixture to be treated for the purpose of absorbing CO2 and C2 and higher hydrocarbons, preferably has a viscosity, at -30 ° C, of less than 0.05 Pa.s.
  • the solvent according to the invention may consist in particular of one or more liquid absorbents which are selective for CO2 and used in anhydrous form or in mixture with water, the said solvent (s) being chosen from the amides of formulas aldehydes of formula formula esters Ccan to C4 alkanols, diethers of formula diether alcohols of formula R9O-C2H4-O-C2H4-OH, lactones of formula and propylene carbonate, with in these formulas R1 and R2, identical or different, designating a hydrogen atom or a C1 or C2 alkyl radical, R3 being a C3 or C4 alkyl radical, R6 being a C2 alkyl radical to C4 or a radical with R8 denoting a C1 or C2 alkyl radical and n being equal to 1 or 2, R7 being a C1 or C2 alkyl radical or a radical R9 denoting a C radical to C4 alkyl radical and p being an integer ranging from 2 to 4.
  • Nonlimiting examples of liquid organic absorbents corresponding to the above formulas are such as N, N-dimethylformamide, N, N-dimethylacetamide, dimethoxymethane, diethoxymethane, dimethoxy-1,1 ethane, methanol, ethanol, ethylene dimethyl ether glycol, diethylene glycol dimethyl ether, ethylene glycol monomethyl ether, butyrolactone, propiolactone and propylene carbonate.
  • the contacting temperature of the gas mixture to be treated with the solvent, in the washing zone is preferably between 0 ° C and -45 ° C.
  • the washing zone advantageously consists of one or more washing columns containing the appropriate number of theoretical washing stages, said columns being, for example, of the type of tray columns or also packed columns.
  • the temperature in each of the washing columns is kept substantially constant by indirect heat exchange, carried out at one or more points of the column considered, between the fluid medium contained in this column and a cooling fluid.
  • the demethanization treatment applied to the rich solvent is carried out, in particular, in two stages, namely a first step in which said rich solvent is subjected to a first expansion capable of releasing a large fraction of the methane dissolved in said solvent to be demethanized and in producing a first methane-rich gas and a premethanized fluid and a second step in which the premethanized fluid is subjected to a second expansion and then to distillation producing a second methane-rich gas and the demethanized rich solvent, the second methane-rich gas being compressed to the pressure of the first methane-rich gas and then mixed with the latter to form the methane-rich gas phase.
  • the methane-rich gas phase resulting from the demethanization treatment applied to the rich solvent, is advantageously compressed to the pressure of the gas mixture to be treated, then it is cooled and mixed with the gas mixture to be treated before the latter is brought into contact. with the solvent in the washing area.
  • the regeneration of the purified solvent which leads to the production of the stream of acid gas rich in CO2 and having, expressed in methane equivalent, a hydrocarbon content of less than 10 mol% relative to CO2, can be carried out by any treatment making it possible to release gaseous compounds dissolved in a liquid.
  • the regeneration of the purified solvent can be carried out by expansion of said purified solvent to a pressure greater than 100 kPa and for example between 150 kPa and 300 kPa and by stripping using an inert gas such as nitrogen. possibly associated with a heating of the purified solvent in the regeneration zone.
  • the regeneration of the purified solvent can also be carried out by heating said purified solvent to a temperature close to ambient, by dividing the heated solvent into first and second streams, by directing the first stream directly to a regeneration zone, directing the second stream to this regeneration zone after having heated it by indirect heat exchange with the regenerated purified solvent, and by subjecting the solvent to distillation in the regeneration zone to produce the regenerated solvent and the stream of acid gas rich in CO2.
  • the gaseous mixture to be treated contains water and / or C5 and higher hydrocarbons, it is advantageously subjected to a pretreatment intended to remove all or part of these compounds before being brought into contact with the solvent in the zone of washing.
  • This pretreatment can consist of a distillation possibly carried out in the presence of solvent, taken from the solvent injected into the washing zone, to produce the pretreated gas mixture having a C6 hydrocarbon content and more than 0.1% by weight, a fraction of so-called heavy hydrocarbons containing almost all of the C6 and more hydrocarbons and all or part of the C5 hydrocarbons and, optionally, a liquid consisting of a mixture of solvent and water.
  • Said distillation of the gas mixture is carried out at a temperature at least equal to the temperature prevailing in the washing zone.
  • the gaseous mixture to be treated arriving via line 1 is introduced into the lower part of a distillation column 2, in which said gaseous mixture is optionally distilled in the presence of solvent withdrawn, through an opening pipe 41 in the upper part of column 2, on the regenerated solvent 38 brought to the washing column 5, before passage of said solvent in a refrigeration zone 39 mounted on the conduit 6 for injecting the regenerated solvent into said washing column 5, so as to produce on the one hand a dried gas mixture, evacuated from column 2 via a line 3 and whose C6 and higher hydrocarbon content is less than 0.1% by weight, and on the other hand a hydrocarbon fraction containing almost all of the C6 hydrocarbons and more and possibly all or part of the C5 hydrocarbons, withdrawn from column 2 by a conduit 4 and optionally a liquid withdrawn from column 2 by a conduit 54 and consisting of a mixture of solvent and water.
  • the dried gas mixture leaving column 2 through line 3 is introduced into the lower part of a washing column 5, for example of the plate column type, in which it is brought into contact, countercurrently, with cold solvent. regenerated injected into the upper part of column 5 through line 6, after passage through the coolant 39, this contacting being carried out at a temperature of, for example, between 0 ° C and -45 ° C, said temperature being controlled by passage of the liquid medium contained in column 5 in refrigerants 7.
  • a treated gas consisting mainly of methane and depleted in CO2, said treated gas being heated in a system 9 reheating and then directed, via a conduit 10, to a zone of use, while at the bottom of said column 5 is drawn off, via a conduit 11, a liquid phase consisting of the solvent enriched in CO2 and a other compounds absorbed and called rich solvent.
  • the dried gas mixture is brought into contact with the solvent in the washing column 5 at an appropriate temperature in the range O ° C to -45 ° C and with a ratio of the flow rates of the gas mixture to be treated and of solvent such that on the one hand the treated gas collected, through line 8, at the head of column 5 has a molar CO2 content of at most equal to 2% and that on the other hand the rich solvent, flowing through line 11 , contains at least 80 mol% of C3 and higher hydrocarbons present in the dried gas mixture introduced in column 5.
  • the rich solvent circulating in the conduit 11 is introduced, after passing through the expansion valve 12, into the upper part of an expansion tank 13 in which a first gas rich in methane separates, which is removed at the head of the flask 13 by a conduit 14, and a rich predemethanized solvent, which is drawn off at the bottom of the flask 13 by a conduit 15.
  • Said predemethanized rich solvent is subjected to a second expansion through an expansion valve 16 followed by a distillation in a distillation column 17 provided with a reboiler 18, so as to produce a second gas rich in methane, which is evacuated at the top of the column 17 by a conduit 19, and a liquid phase depleted in methane, called demethanized rich solvent, which is drawn off at the bottom of the column 17 by a pipe 27.
  • the second methane-rich gas circulating in the pipe 19 is caused to pass into a compressor 20 from which it leaves, via a pipe 21, to a pressure substantially equal to that of the first methane-rich gas passing through line 14, then these two methane-rich gases are mixed in line 22 and the gas phase resulting from this mixture is recycled, by means of a compressor 23 whose the outlet is extended by a line 24, a cooler 25 and a line 26, in the line 3 for supplying the dried gas mixture to the washing column 5.
  • the demethanized rich solvent, withdrawn from the column 17 through the conduit 27, is expanded by passing through an expansion valve 29, then is refrigerated in the refrigerant system 40 with the result of the demixing of said solvent into two liquid phases, namely a phase upper hydrocarbon and a lower phase consisting of the solvent containing the majority of CO2 and a certain amount of hydrocarbons.
  • the assembly is introduced into an extraction tower 56, in which it is brought into contact, against the current, with a refrigerated hydrocarbon solvent injected, through a conduit 57, into the lower part of the extraction tower and with a stream of regenerated solvent introduced into the tower 56 through a conduit 63, so as to produce, on the one hand, a purified solvent containing the almost all of the CO2 present in the demethanized rich solvent, said purified solvent being drawn off at the bottom of the extraction tower 56 by a conduit 58 on which is mounted an expansion valve 60, and, on the other hand, a hydrocarbon solvent enriched in C2 hydrocarbons and more containing little CO2, said solvent being discharged at the head of the extraction tower 56 through a conduit 59.
  • the enriched hydrocarbon solvent 59 is introduced into a regeneration column 49 in which said solvent is fractionated by distillation into a fraction of C2 and higher hydrocarbons, which is evacuated at the top of said column 49 by a conduit 48 and constitutes the cut d hydrocarbons in C plus and more containing at least 80 mol% of hydrocarbons in C3 and more contained in the gas to be treated brought to the washing column 5 by line 3, and in a regenerated hydrocarbon solvent withdrawn from column 49 by a line 50, which regenerated hydrocarbon solvent is recycled by the pump 51, through the refrigerant system 61 and the conduit 57, to the extraction tower 56.
  • the purified solvent circulating in the conduit 58 is introduced into the upper part of a regeneration column 62 provided with a heater 69, in which said purified solvent is subjected to a regeneration comprising a stripping using a stream of inert gas, for example a stream of nitrogen, injected into the lower part of the column 62 by a conduit 43.
  • a regeneration column 62 provided with a heater 69, in which said purified solvent is subjected to a regeneration comprising a stripping using a stream of inert gas, for example a stream of nitrogen, injected into the lower part of the column 62 by a conduit 43.
  • Said regeneration produces, on the one hand, a regenerated solvent 34, which is recycled by means of a pump 37 and a pipe 38 to the washing column 5 through the heat exchanger 39 and the pipe 6, and, on the other hand, a stream 44 of acid gas rich in CO2 , which contains almost all of the CO2 present in the demethanized rich solvent and has, expressed in methane equivalent, a hydrocarbon content of less than 10 mol% relative to CO2.
  • Part of the cold regenerated solvent passing through the conduit 38 is diverted through a conduit 63 to be injected into the extraction tower 56 at a point of this tower located above the injection point of the demethanized rich solvent circulating in the conduit 27.
  • the gaseous mixture to be treated arriving via line 1 with a flow rate of 10,000 kmol / h, a temperature of 30 ° C and a pressure of 5,000 kPa was introduced into column 2 for removal of C6 and higher hydrocarbons.
  • the gas mixture to be treated being dry, no addition of solvent was carried out via line 41.
  • the pretreated gas mixture was contacted with 11,500 kmol / h of solvent having a temperature of -20 ° C and a pressure of 5000 kPa and containing, by mole, 82.34% of methanol, 14.67% of water and 2.88 hexane, said contacting being carried out in a washing column 5 comprising 14 plates and operating at -20 ° C under a pressure of 4900 kPa.
  • the refrigerants 7 fitted to the washing column 5 made it possible to maintain the temperature in said column at the desired value.
  • the treated gas, discharged through line 8, was warmed up to room temperature in the heat exchanger system 9, the heated treated gas being directed, through line 10, to a shipping pipeline.
  • the demethanization of the rich solvent firstly involved a first expansion of said solvent at a pressure of 3000 kPa, the expanded relaxed solvent supplying the expansion tank 13 in which 401 kmol / h of a first gas containing 64% molar of methane, which was discharged at the head of the flask 13 through line 14, and a predemethanized rich solvent withdrawn from said flask through line 15 and whose molar methane content has been reduced from 3.70 to 2.01%.
  • the premethanized rich solvent the temperature of which was equal to -22.5 ° C., was expanded in valve 16 and then fed to the distillation column 17 comprising 10 plates and operating at 1800 kPa.
  • the second methane-rich gas was compressed in compressor 20 to the pressure of the first methane-rich gas, namely 3000 kPa.
  • the compressed gas leaving the compressor 20, via the conduit 21, was mixed with the first methane-rich gas to constitute the methane-rich gas phase 22, which was then compressed, in the compressor 23, until the pressure of the gas mixture a treating, namely 5000 kPa, said compressed gas phase being added through line 24, the refrigerant 25 and line 26, to the pretreated gas mixture circulating in line 3.
  • the compressed methane-rich gas phase passing through line 26 had a temperature of -20 ° C, a pressure of 5000 kPa and a flow rate of 1006 kmol / h.
  • the molar composition of said methane-rich gas phase flowing in line 26 was as follows: . CO2 34.31% . Methane 53.50% . Ethane 9.84% . Propane 1.70% . Butane 0.53% . Hexane 0.09% . Methanol 0.03%
  • the extraction tower 56 included 31 trays and was supplied on the first tray with 5000 kmol / h of regenerated solvent brought in through line 63 with a temperature of -40 ° C., on tray 21 by the demethanized rich solvent coming from the system refrigeration 40 and on the plate 31 by the refrigerated hydrocarbon solvent based on hexane supplied by line 57 with a flow rate of 1600 kmol / h.
  • This extraction produced 2079 kmol / h of a rich hydrocarbon solvent having a temperature of -40 ° C and a pressure of 1200 kPa, said rich hydrocarbon solvent being evacuated at the top of tower 56 via line 59, and 18069 kmol / h purified solvent withdrawn from the bottom of said tower, via line 58, at a temperature of -40 ° C. and under a pressure of 1200 kPa.
  • the molar composition of the rich hydrocarbon solvent passing through line 59 was as follows: . CO2 0.14% . Methane 0.13% . Ethane 9.19% . Propane 7.79% . Butane 6.62% . Hexane 73.72% . Methanol 2.40%
  • the molar composition of the purified solvent passing through line 58 was as follows: . CO2 9.16% . Methane 0.01% . Ethane 0.10% . Propane 0.01% . Hexane 2.42% . Methanol 74.91% . Water 13.40%
  • the C2 and higher hydrocarbon section evacuated via line 48, had the following molar composition: . CO2 0.59% . Methane 0.54% . Ethane 38.40% . Propane 32.58% . Butane 27.67% . Hexane 0.20% . Methanol 0.02%.
  • the regenerated hydrocarbon solvent passing through line 50 contained, by mole, 95.77% hexane, 1.11% butane and 3.12% methanol. Said solvent was brought, in the pump 51, to a pressure of 1200 kPa, then refrigerated at -40 ° C in the refrigerant system 61 before being recycled, via the conduit 57, to the extraction tower 56.
  • the purified solvent from line 58 of the extraction tower 56 is expanded to a pressure of 200 kPa in the expansion valve 60, then it is introduced into the regeneration column 62 for the purpose of regeneration.
  • Said column 62 comprising 14 plates and operating under a pressure of 200 kPa, is supplied to the first plate by the purified solvent to be regenerated and to the last plate by a stream of nitrogen supplied, via line 43, with a flow rate of 650 kmol / h.
  • the heater 69 which is provided with said column 62, was located on the seventh plate.
  • the stream of CO2-rich acid gas discharged through line 44 had a pressure of 200 kPa and a temperature of -47.5 ° C and it had the following molar composition: . CO2 71.64% . Methane 0.05% . Ethane 0.77% . Propane 0.04% . Hexane 0.40% . Methanol 0.06% . Nitrogen 27.04%.
  • the regenerated solvent circulating in the conduit 34 was brought to the pressure of 5000 kPa per passage through the pump 37, then divided into two parts, namely a major part recycled to the washing column 5 after passage through the heat exchanger system 39 and the conduit 6 and a part brought into the extraction tower 56 by the conduit 63.

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Claims (9)

  1. Verfahren zur gleichzeitigen Abtrennung von CO₂ und Benzin aus einem gasförmigen Gemisch, das einen absoluten Druck von über 0,5 MPa aufweist und in der Hauptsache aus Methan und Kohlenwasserstoffen mit zwei oder mehr C-Atomen bestehende Kohlenwasserstoffe und außerdem CO₂ und gegebenenfalls eine oder mehrere nicht schwefelhaltige Verbindungen mit niedrigem Siedepunkt wie H₂, CO, N₂ und Ar enthält, wobei man das Gasgemisch in einer Rieselzone (5) mit einem Lösungsmittel (6) kontaktiert, das eine Flüssigkeit darstellt, die vorzugsweise CO₂ und Kohlenwasserstoffe mit zwei oder mehr C-Atomen löst und einerseits bei Atmosphärendruck eine Siedetemperatur von über 40°C und andererseits bei -30°C eine Viskosität von unter 0,1 Pa.s aufweist, und zwar bei einer ausreichend tiefen Temperatur und bei einem solchen Durchsatzverhältnis von zu behandelndem Gasgemisch zum Lösungsmittel, daß einerseits ein behandeltes Gas (8) hergestellt wird, das in der Hauptsache aus Methan besteht und einen Molargehalt an CO₂ von höchstens 2 % aufweist, und andererseits eine flüssige Phase, die als "reiches Lösungsmittel" (11) bezeichnet wird und aus dem Lösungsmittel gebildet wird, das mit CO₂ und einer Fraktion von Kohlenwasserstoffen mit zwei und mehr C-Atomen, die wenigstens 80 Mol-% der in dem zu behandelnden Gasgemisch enthaltenen Kohlenwasserstoffe mit drei und mehr C-Atomen enthält, angereichert ist, das "reiche Lösungsmittel" wenigstens teilweise durch Entspannung entmethanisiert (12, 17) wird, wobei das "reiche Lösungsmittel" in eine an Methan verarmte und als "entmethanisiertes reiches Lösungsmittel" (27) bezeichnete Flüssigphase und eine mit Methan angereicherte (22) Gasphase aufgetrennt wird, und das "entmethanisierte reiche Lösungsmittel" so behandelt wird, daß ein Strom an saurem Gas (44) erzeugt wird, der das im "entmethanisierten reichen Lösungsmittel" vorliegende CO₂ enthält, außerdem ein als "Kohlenwasserstofffraktion" (48) bezeichnetes Kohlenwasserstoffgemisch erzeugt wird und schließlich ein regeneriertes Lösungsmittel (34) erhalten wird, das wieder der Rieselzone (5) zugeführt wird, dadurch gekennzeichnet, daß die Behandlung des "entmethanisierten reichen Lösungsmittels" so erfolgt, daß man das "entmethanisierte reiche Lösungsmittel" zuerst abkühlt (40) und dann mit Hilfe eines gekühlten Kohlenwasserstofflösungsmittels in einer Extraktionszone (56) einer Flüssig-Flüssig-Extraktion unterzieht, wodurch einerseits ein gereinigtes Lösungsmittel (58) erzeugt wird, das fast die gesamte Menge des im "entmethanisierten reichen Lösungsmittel" enthaltenen CO₂ enthält und einen Kohlenwasserstoffgehalt, ausgedrückt als Methanäquivalent, von unter 10 Mol-%, bezogen auf CO₂, aufweist und andererseits ein Kohlenwasserstofflösungsmittel (59) erzeugt wird, das mit Kohlenwasserstoffen mit zwei und mehr C-Atomen angereichert ist, indem man das angereicherte Kohlenwasserstofflösungsmittel (59) durch Destillation (49) in eine Fraktion von Kohlenwasserstoff mit zwei und mehr C-Atomen, welche die Kohlenwasserstofffraktion (48) bildet und wenigstens 80 Mol-% der in dem zu behandelnden Gasgemisch enthaltenen Kohlenwasserstoffe mit drei und mehr C-Atomen enthält, und in das regenerierte Kohlenwasserstofflösungsmittel (50), das nach Abkühlung wieder der Extraktionszone zugeführt wird, auftrennt und das gereinigte Lösungsmittel (58) durch Entspannung und Strippen (60, 62) regeneriert wird, wodurch das regenerierte Lösungsmittel (34) und der Strom an saurem Gas (44) gebildet werden, der fast zur Gänze aus dem CO₂ besteht, das im "entmethanisierten reichen Lösungsmittel" vorliegt, das einen Kohlenwasserstoffgehalt, ausgedrückt als Methanäquivalent, von unter 10 Mol-%, bezogen auf CO₂, aufweist.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das zur Kontaktierung mit dem zu behandelnden Gasgemisch verwendete Lösungsmittel eine Viskosität bei -30°C von unter 0,05 Pa.s aufweist.
  3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß das zur Kontaktierung mit dem in der Rieselzone (5) zu behandelnden Gasgemisch verwendete Lösungsmittel aus einem oder mehreren in wasserfreier Form oder als Gemisch mit Wasser verwendeten flüssigen organischen Absorbentien besteht, wobei dieses bzw. diese ausgewählt werden unter den Amiden der Formeln
    Figure imgb0023
     den Aldehyden der Formel
    Figure imgb0024
     den Estern der Formeln
    Figure imgb0025
     den C₁₋₄-Alkanolen, den Diethern der Formel
    Figure imgb0026
     den Dietheralkoholen der Formel R₉O - C₂H₄ - O C₂H₄-OH, den Lactonen der Formel
    Figure imgb0027
     und Propylencarbonat, wobei in diesen Formeln R₁ und R₂ gleich oder verschieden sind und ein Wasserstoffatom oder einen C₁₋₂-Alkylrest, R₃ einen C₃₋₄-Alkylrest, R₆ einen C₂₋₄-Alkylrest oder einen Rest
    Figure imgb0028
     bedeuten, wobei R₈ für einen C₁₋₂-Alkylrest steht und n 1 oder 2, R₇ einen C₁₋₂-Alkylrest oder einen Rest
    Figure imgb0029
     R₉ einen C₁₋₄-Alkylrest und p eine ganze Zahl zwischen 2 und 4 bedeuten.
  4. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß die Temperatur für die Kontaktierung des zu behandelnden Gasgemisches mit dem Lösungsmittel in der Rieselzone (5) zwischen 0 und -45°C liegt.
  5. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß die Entmethanisierung des "reichen Lösungsmittels" (11) in zwei Stufen durchgeführt wird, wobei auf der ersten Stufe das "reiche Lösungsmittel" einer ersten Entspannung (12, 13) unterworfen wird, die geeignet ist, eine starke Fraktion an im Lösungsmittel gelöstem Methan freizusetzen und ein erstes mit Methan angereichertes Gas (14) und eine vorentmethanisierte Flüssigkeit (15) zu erzeugen, und auf der zweiten Stufe die vorentmethanisierte Flüssigkeit einer zweiten Entspannung (16) und dann einer Destillation (17) unterworfen wird, wodurch ein zweites mit Methan angereichertes Gas (19) und das "entmethanisierte reiche Lösungsmittel " (27) erzeugt werden, wobei das zweite mit Methan angereicherte Gas bis zum Druck des ersten mit Methan angereicherten Gases komprimiert und dann mit diesem gemischt wird, um die mit Methan angereicherte Gasphase (22) zu bilden.
  6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß die mit Methan angereicherte Gasphase (22) bis zum Druck des zu behandelnden Gases komprimiert, dann abgekühlt (25) und mit dem zu behandelnden Gasgemisch vor der Kontaktierung des letzteren mit dem Lösungsmittel in der Rieselzone (5) gemischt wird.
  7. Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß die Regenerierung des gereinigten Lösungsmittels durch seine Entspannung bis zu einem Druck von über 100 kPa, insbesondere zwischen 150 und 300 kPa und durch Strippen (43) mit Hilfe eines Inertgases wie Stickstoff, gegebenenfalls in Verbindung mit einer erneuten Erwärmung (69) des gereinigten Lösungsmittels in der Regenerierungskolonne durchgeführt wird.
  8. Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß die Regenerierung des gereinigten Lösungsmittels (58) darin besteht, daß man das Lösungsmittel bis zu einer Temperatur im Bereich der Umgebungstemperatur erwärmt, das erwärmte Lösungsmittel in einen ersten Strom (30) und einen zweiten Strom (31) aufteilt, den ersten Strom (30) unmittelbar einer Regenerierungszone (33) zuführt, den zweiten Strom (31) dieser Regenerierungszone nach erneuter Erwärmung durch indirekten wärmeaustausch (35) mit dem regenerierten gereinigten Lösungsmittel (34) zuführt und das gereinigte Lösungsmittel in der Regenerierungszone (33) destilliert, um den mit CO₂ angereicherten Strom an Saurem Gas (44) und das regenerierte Lösungsmittel (34) zu erzeugen.
  9. Verfahren nach einem der Ansprüche 1 bis 8, dadurch gekennzeichnet, daß das zu behandelnde Gas, das Wasser und/oder Kohlenwasserstoffe mit fünf oder mehr C-Atomen enthält, einer Vorbehandlung unterworfen wird, die in einer Destillation (2) besteht, die bei einer Temperatur, die zumindest der in der Rieselzone (5) herrschenden Temperatur entspricht, und gegebenenfalls in Anwesenheit des Lösungsmittels durchgeführt wird, das aus dem der Rieselzone (5) zugeführten Lösungsmittel abgezogen wurde, wodurch eine Fraktion (4) aus sogenannten schweren Kohlenwasserstoffen erzeugt wird, welche fast die gesamte Menge an Kohlenwasserstoffen mit sechs und mehr C-Atomen und gegebenenfalls die gesamte Menge oder einen Teil der Kohlenwasserstoffe mit fünf C-Atomen enthalten, ein vorbehandeltes Gasgemisch (3) mit einem Gehalt an Kohlenwasserstoffen mit sechs und mehr C-Atomen von unter 0,1 Gew.-% und gegebenenfalls eine Flüssigkeit (54) erzeugt werden, die ein Gemisch aus Lösungsmittel und Wasser darstellt.
EP89403123A 1988-11-15 1989-11-14 Verfahren zur gleichzeitigen Ausscheidung von CO2 und Bearin aus Methan, C2 und höheren Kohlenwasserstoffen und CO2 enthatenden gasförmigen Kohlenwasserstoffen Expired - Lifetime EP0373983B1 (de)

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EP93107550A EP0556875B1 (de) 1988-11-15 1989-11-14 Verfahren zur gleichzeitigen Ausscheidung von CO2 und Benzin aus Methan, C2 und höheren Kohlenwasserstoffen und CO2 enthaltenden gasförmigen Kohlenwasserstoffen
AT89403123T ATE100852T1 (de) 1988-11-15 1989-11-14 Verfahren zur gleichzeitigen ausscheidung von co2 und bearin aus methan, c2 und hoeheren kohlenwasserstoffen und co2 enthatenden gasfoermigen kohlenwasserstoffen.
GR950402736T GR3017623T3 (en) 1988-11-15 1995-10-04 Process for the simultaneous elimination of CO2 and gasoline from a gaseous hydrocarbon mixture comprising methane, C2 and higher hydrocarbons and also CO2.

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FR8814784 1988-11-15
FR888814784A FR2641542B1 (fr) 1988-11-15 1988-11-15 Procede de decarbonatation et de degazolinage simultanes d'un melange gazeux constitue principalement d'hydrocarbures consistant en methane et hydrocarbures en c2 et plus et renfermant egalement co2

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EP93107550A Expired - Lifetime EP0556875B1 (de) 1988-11-15 1989-11-14 Verfahren zur gleichzeitigen Ausscheidung von CO2 und Benzin aus Methan, C2 und höheren Kohlenwasserstoffen und CO2 enthaltenden gasförmigen Kohlenwasserstoffen

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NO302567B1 (no) * 1994-02-14 1998-03-23 Norsk Hydro As Mateanordning
FR2743083B1 (fr) * 1995-12-28 1998-01-30 Inst Francais Du Petrole Procede de deshydratation, de desacidification et de degazolinage d'un gaz naturel, utilisant un melange de solvants
JP5383338B2 (ja) 2009-06-17 2014-01-08 三菱重工業株式会社 Ｃｏ２回収装置及びｃｏ２回収方法
GB201520405D0 (en) * 2015-11-19 2016-01-06 Isis Innovation Ltd And King Abdulaziz City For Science And Technology Hydrocarbon separation process

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NO903128D0 (no) 1990-07-13
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NO180687C (no) 1997-05-28
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JPH03503779A (ja) 1991-08-22
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AU627250B2 (en) 1992-08-20
FR2641542B1 (fr) 1994-06-24
DE68912746D1 (de) 1994-03-10
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NO903128L (no) 1990-09-11
CA2002826A1 (fr) 1990-05-15
US5298156A (en) 1994-03-29
CA2002826C (fr) 1999-06-29
EP0556875A2 (de) 1993-08-25
EP0556875A3 (en) 1993-11-10
JP2742328B2 (ja) 1998-04-22
BR8907193A (pt) 1991-03-05
NO180687B (no) 1997-02-17
EP0373983A1 (de) 1990-06-20
RU1836407C (ru) 1993-08-23
EP0556875B1 (de) 1995-07-12
FR2641542A1 (fr) 1990-07-13

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