EP0556875A2 - Process for the simultaneous elimination of CO2 and gasoline from a gaseous hydrocarbon mixture comprising methane, C2 and higher hydrocarbons and also CO2 - Google Patents

Process for the simultaneous elimination of CO2 and gasoline from a gaseous hydrocarbon mixture comprising methane, C2 and higher hydrocarbons and also CO2 Download PDF

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Publication number
EP0556875A2
EP0556875A2 EP93107550A EP93107550A EP0556875A2 EP 0556875 A2 EP0556875 A2 EP 0556875A2 EP 93107550 A EP93107550 A EP 93107550A EP 93107550 A EP93107550 A EP 93107550A EP 0556875 A2 EP0556875 A2 EP 0556875A2
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EP
European Patent Office
Prior art keywords
solvent
rich
gas
methane
hydrocarbons
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EP93107550A
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German (de)
French (fr)
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EP0556875A3 (en
EP0556875B1 (en
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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    • 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 hydrocarbons of C 2 and more and also containing C0 2 and optionally one or more non-sulfurized compounds at low point of boiling such as H 2 , CO, N 2 and argon.
  • decarbonation and degassing operations are generally carried out separately and are part of a succession of operations carried out on the gaseous mixture to be treated and mainly comprising an elimination of the acid gas C0 2 , drying, adsorption of the water on a suitable solid such as a molecular sieve, a separation by cryogenic distillation between -30 ° C and -90 ° C associated or not with a solvent extraction 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 C 4 and higher hydrocarbons, in one phase gas containing methane and lighter compounds and a liquid fraction containing C 2 and higher hydrocarbons and C0 2 .
  • This liquid fraction is separated, in a second column (de-ethanizer) into which a certain amount of the additive is also introduced, into an overhead fraction consisting of C0 2 and a bottom fraction containing the C 2 hydrocarbons and more.
  • Said tail fraction is then separated, in a third column, into an overhead fraction consisting of a liquid cut of C 2 to C 4 hydrocarbons and into a tail fraction consisting of a liquid cut of C 4 to C hydrocarbons and plus, which contains most of the butanes and higher hydrocarbons present in the treated natural gas and from which the appropriate quantity is taken to constitute the additive injected in the first and second columns.
  • This additive avoids the crystallization of C0 2 at the top of the demethanizer and ensures the rupture of the azeotrope which forms between ethane and C0 2 and facilitates the separation of these compounds 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 C 2 and more hydrocarbons and also contain C0 2 and optionally one or more low-boiling non-sulfur compounds such as H 2 , CO, N 2 and argon, such gaseous mixtures being for example of the natural gas type, said process making it possible to achieve more easily and at lower cost, in comparison with known processes, the objective of gas mixture in the three components, namely treated gas consisting mainly of methane, liquid cut of hydrocarbons with predominantly C 3 and more hydrocarbons and containing, as required, a more or less significant quantity of ethane and current of C0 2 , 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 quotation and in which the gas mixture is brought into contact, in a washing zone, with a solvent consisting of a liquid which preferentially dissolves C0 2 and C 2 and higher hydrocarbons 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, on the one hand, a treated gas consisting mainly of methane and having a molar content is produced in C0 2 at most equal to 2% and, on the other hand, a liquid phase called rich solvent and formed of the solvent enriched in C0 2 and in a fraction of hydrocarbons in C 2 and more containing at least 80 mol% of the hydrocarbons in C 3 and more present in the gauze mixture
  • 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
  • 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 into contact with the gaseous mixture to be treated for the purpose of absorbing C0 2 and C 2 and higher hydrocarbons, preferably has a viscosity of less than 0.05 Pa. s.
  • the solvent according to the invention may consist in particular of one or more liquid absorbents selective for CO 2 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 alkanols Ci -C 4 diethers of formula diether alcohols of formula R 9 O- C 2 H 4 - O - C 2 H 4 - OH lactones of formula and propylene carbonate, with in these formulas R 1 and R 2 , identical or different, denoting a hydrogen atom or an alkyl radical in Ci or C 2 , R 3 being an alkyl radical in C 3 or C 4 , R 6 being a C 2 -C 4 alkyl radical or a radical with R 8 denoting an alkyl radical Ci or C 2 and n is 1 or 2, R 7 being an alkyl radical in C 1 -C 2 or a radical Rg denotes an alkyl to C 4 and p is an integer from 2 to 4.
  • Non-limiting 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 even 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 in question, between the fluid medium contained in this column and a refrigerating 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 at an intermediate pressure capable of releasing a large fraction of the methane dissolved in said solvent to demethanize and produce a first gas rich in methane and a premethanized fluid and a second step in which the premethanized fluid is subjected to a second expansion then to a distillation of so as to produce 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 demethanized rich solvent is carried out by reheating said solvent to a temperature close to ambient, by dividing the reheated solvent into first and second streams, directing the first stream directly to a regeneration zone by directing the second stream to said regeneration zone after having heated it by indirect heat exchange with the regenerated solvent, and by subjecting the solvent to distillation in the regeneration zone.
  • Said distillation can be carried out in the presence of a stream of inert gas, for example nitrogen, injected into the regeneration zone.
  • the gaseous mixture to be treated contains water and / or C 5 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 washing area.
  • 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 C 6 hydrocarbon content and more than 0.1% by weight, a fraction of so-called heavy hydrocarbons containing almost all of the C 6 and higher hydrocarbons and all or part of the C 5 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 gaseous mixture, evacuated from column 2 by a line 3 and whose hydrocarbon content in C 6 and more is less than 0.1% by weight, and on the other hand a cut hydrocarbon containing almost all of the C 6 and more hydrocarbons and possibly all or part of the C s hydrocarbons, withdrawn from column 2 by a conduit 4 and optionally a liquid withdrawn from the column 2 via a conduit 54 and consisting of a mixture of solvent and water.
  • the dried gaseous mixture leaving column 2 via 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 C0 2 is discharged, via a conduit 8, said treated gas being heated in a system 9 for 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 C0 2 e t 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 content of C0 2 at most equal to 2% and that on the other hand the rich solvent, flowing through the line 11, contains at least 80 mol% of the C 3 and higher hydrocarbons present in the dried gas mixture introduced into column 5.
  • the rich solvent circulating in the conduit 11 is introduced, after passage through the expansion valve 12, into the upper part of an expansion tank 13 in which a first methane-rich gas separates, which is removed at the head of the flask 13 by a conduit 14, and a predemethanized rich solvent, which is withdrawn from 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 discharged at the head of column 17 through a pipe 19, and a methane-depleted liquid phase, called demethanized rich solvent, which is drawn off at the bottom of the column 17 through a pipe 27.
  • the second methane-rich gas circulating in the pipe 19 is caused to pass into a compressor 20 from which it exits, via a conduit 21, at a pressure substantially equal to that of the first gas rich in methane passing through the conduit 14, then these two gases rich in methane are mixed in the conduit 22 and the gas phase resulting from this mixture is recycled, by means of a compressor 23, the outlet of which is extended by a conduit 24, a coolant 25 and a conduit 26, in the conduit 3 for supplying the dried gaseous mixture to washing column 5.
  • the regeneration can be carried out in the presence of a stream of inert gas, in particular a stream of nitrogen, injected into the lower part of the column 33 through a conduit 43.
  • Said regeneration produces, on the one hand, a regenerated solvent withdrawn from the bottom of the column 33, through a pipe 34, and used in the heat exchanger 35, to heat the second stream 31 of demethanized rich solvent to be regenerated, before being recycled, by the pump 37 and the conduit 38, towards the washing column 5, and on the other hand a gas mixture discharged at the head of the column 33, by a conduit 42, and containing the C0 2 as well as the C 2 and higher hydrocarbons present in the rich demethanized solvent.
  • the gaseous mixture passing through the conduit 42 is washed against the current, in a washing tower 47 provided with a condenser 46 at the head and a reboiler 70 at the bottom and operating at low temperature, using a hydrocarbon solvent in C 5 and over brought to the washing tower 47 by a conduit 53, said washing producing, on the one hand, a stream 44 of acid gas rich in C0 2 , which contains almost all of the C0 2 present in the solvent rich demethanized and has, expressed in methane equivalent, a hydrocarbon content of less than 10 mol% relative to C0 2 , and, on the other hand, a rich hydrocarbon solvent 45 practically free of C0 2 and containing almost all of the hydrocarbons in C 2 and more present in the gas mixture arriving via line 42.
  • the rich hydrocarbon solvent 45 is brought to a regeneration column 49 in which said solvent 45 is subjected to distillation to produce, on the one hand, a fraction of hydrocarbons 48 constituting the cut of C 2 hydrocarbons and more containing the minus 80 mol% of the C 3 hydrocarbons and more contained in the gas to be treated brought to the washing column 5 by the line 3, and, on the other hand, a regenerated hydrocarbon solvent 50, which is recycled, by the pump 51 , to the washing tower column 47 after refrigeration in the system 52 and passage in the conduit 53.
  • 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 elimination of C 6 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 brought into contact with 6000 kmol / h of solvent consisting of a mixture of methanol and water in a molar ratio equal to 95: 5 and having a pressure of 5000 kPa and a temperature equal to -30 ° C. , said contacting being carried out in a washing column 5 comprising 14 plates and operating at - 30 ° 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 heated treated gas is directed through line 10 to an expedition 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 362 kmol / h of a first gas containing 68 mol% of methane were produced. , 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 was reduced from 6.11% to 3.57%.
  • the premethanized rich solvent the temperature of which was equal to -33.6 ° C., was expanded in valve 16 and then fed to the distillation column 17 comprising 10 plates and operating at 1800 kPa.
  • the demethanized rich solvent had the following molar composition:
  • 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 gaseous phase passing through line 26 had a temperature of -20 ° C, a pressure of 5,000 kPa and a flow rate of 938 kmol / h.
  • the demethanized rich solvent after expansion in the valve 29 and heating in the heating system 28, had a temperature of 10 ° C and a pressure of 800 kpa. Said heated solvent was then divided into a first stream 30 having a flow rate of 4533 kmol / h, which was directed directly to the regeneration column 33, and into a second stream 31, which was heated to 70 ° C. in the heat exchanger. heat 35 before being conveyed to the regeneration column 33.
  • This column operated under a pressure of 700 kPa and included 18 plates, the currents 30 and 31 being injected respectively at the plates 8 and 12, counted from the top of the column.
  • the regeneration column 33 produced at the head a gaseous mixture containing C0 2 and the hydrocarbons in C 2 and more, which was evacuated via line 42 with a temperature of -14 ° C, a pressure of 700 kPa and a flow rate of 2244 kmol / h and at the bottom a regenerated solvent withdrawn from the regeneration column 33 through the pipe 34.
  • the gas mixture passing through line 42 had the following molar composition:
  • the regenerated solvent is cooled by passage through the heat exchanger 35, then recompressed to a pressure of 5000 kPa by the pump 37, and it is then directed through the conduit 38 on the one hand in a major quantity to the washing column 5 , through the refrigerant 39 and the conduit 6.
  • Tower 47 had 35 platforms and operated under a pressure of 700 kPa with a temperature of -30 ° C at the head at the level of the refrigerant 46.
  • the washing tower 47 produced at the head an acid gas stream 44 rich in C0 2 and having a hydrocarbon content, expressed in methane equivalent, of less than 10 mol% with respect to C0 2 , said acid gas stream having a temperature of -30 ° C, a pressure of 650 kPa and a flow rate of 1685 kmol / h, and in the background a hydrocarbon solvent 45 with reduced C0 2 content having a temperature of 95.8 ° C, a pressure of 730 kPa and a flow rate 5059 kmol / h.
  • the molar composition of the acid gas stream 44 was as follows:
  • the rich hydrocarbon solvent 45 had the following molar composition:
  • the fractionation of the rich hydrocarbon solvent 45 in the column 49 provided with 28 trays and operating under a pressure of 600 kPa produced at the head 561 kmol / h of a cut of hydrocarbons 48 in C 2 and more having a temperature of 18 ° C and a pressure of 600 kPa and at the bottom 4500 kmol / h of regenerated hydrocarbon solvent having a temperature of 142.7 ° C and a pressure of 670 kPa, said solvent containing, in mole, 98.89% of hexane and 1, 11% butane.

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  • Gas Separation By Absorption (AREA)
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  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The gas mixture to be treated (1) is washed (5) between 0 DEG C and -45 DEG C by means of a solvent (6) for CO2 and C3 and higher hydrocarbons to produce a methane stream (8) containing not more than 2 mol% of CO2 and a CO2-rich liquid phase (11) containing at least 80 mol% of C3 and higher hydrocarbons from the gas mixture (1). The liquid phase (11) is subjected to a demethanization (12, 17) producing a demethanized rich solvent (27) and a methane-rich gas phase (22), and then the rich solvent (27) is subjected to a regeneration producing a regenerated solvent (34) which is recycled into the washing zone (5), and a gas mixture (42) containing the CO2 and the C2 and higher hydrocarbons which are present in the methanized rich solvent, the said gas mixture being separated by regenerative washing with a C5 and higher hydrocarbon solvent, into a CO2-rich acidic gas stream containing, expressed as methane equivalent, less than 10 mol% of hydrocarbons, and into a C2 and higher hydrocarbon cut (48) containing at least 80 mol% of the C3 and higher hydrocarbons present in the gas to be treated (1).

Description

L'invention concerne un procédé de décarbonatation et de dégazolinage simultanés d'un mélange gazeux constitué principalement d'hydrocarbures consistant en méthane et hydrocarbures en C2 et plus et renfermant également C02 et éventuellement un ou plusieurs composés non sulfurés à bas point d'ébullition tels que H2, CO,N2 et argon.The invention relates to a process for the simultaneous decarbonation and degassing of a gaseous mixture consisting mainly of hydrocarbons consisting of methane and hydrocarbons of C 2 and more and also containing C0 2 and optionally one or more non-sulfurized compounds at low point of boiling such as H 2 , CO, N 2 and argon.

Le procédé selon l'invention permet de séparer directement un mélange gazeux du type précité en trois composantes, à savoir :

  • - un gaz traité consistant principalement en méthane et hydrocarbures en C2 et dont la teneur molaire en C02 est au plus égale à 2 %,
  • - une coupe d'hydrocarbures contenant au moins 80 % molaire des hydrocarbures en C3 et plus présents dans le mélange gazeux à traiter, et
  • - un courant de gaz acide consistant en C02 renfermant moins de 10 % molaire d'hydrocarbures, exprimés en équivalent méthane, par rapport au C02.
The method according to the invention makes it possible to directly separate a gas mixture of the aforementioned type into three components, namely:
  • - a treated gas consisting mainly of methane and C 2 hydrocarbons and whose molar C0 2 content is at most equal to 2%,
  • a section of hydrocarbons containing at least 80 mol% of C 3 and higher hydrocarbons present in the gas mixture to be treated, and
  • - a stream of acid gas consisting of C0 2 containing less than 10 mol% of hydrocarbons, expressed in methane equivalent, relative to C0 2 .

On connait plusieurs procédés, utilisés industriellement, pour le traitement de mélanges gazeux tels que définis plus haut et dont les principaux exemples sont représentés par les divers gaz naturels, qui comportent une opération de décarbonatation, c'est-à-dire une élimination du C02, et une opération de dégazolinage, c'est-à-dire une séparation des hydrocarbures lourds par exemple en C3 et plus, du mélange gazeux et permettent de réaliser le fractionnement dudit mélange gazeux en les trois composantes mentionnées ci-dessus.Several processes are known, used industrially, for the treatment of gas mixtures as defined above and the main examples of which are represented by the various natural gases, which include a decarbonation operation, that is to say elimination of the CO 2 , and a degassing operation, that is to say a separation of heavy hydrocarbons, for example C 3 and above, from the gas mixture and make it possible to carry out the fractionation of said gas mixture into the three components mentioned above.

Ces opérations de décarbonatation et de dégazolinage sont généralement mises en oeuvre de manière séparée et font partie d'une succession d'opérations réalisées sur le mélange gazeux à traiter et comportant principalement une élimination du gaz acide C02 un séchage, une adsorption de l'eau sur un solide approprié tel qu'un tamis moléculaire, une séparation par distillation cryogénique entre -30 ° C et -90 ° C associée ou non à une extraction par un solvant afin d'obtenir la coupe de liquide de gaz naturel, et enfin un réchauffage du gaz traité jusqu'à la température ambiante pour, généralement, alimenter le réseau de gaz commercial.These decarbonation and degassing operations are generally carried out separately and are part of a succession of operations carried out on the gaseous mixture to be treated and mainly comprising an elimination of the acid gas C0 2 , drying, adsorption of the water on a suitable solid such as a molecular sieve, a separation by cryogenic distillation between -30 ° C and -90 ° C associated or not with a solvent extraction 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.

Dans un tel schéma de traitement d'un mélange gazeux du type gaz naturel renfermant les constituants précités, l'abaissement de la température du mélange gazeux est imposé par la seule production de la coupe de liquide de gaz naturel, aucune autre opération n'étant effectuée à ce niveau de température.In such a treatment scheme for a gas mixture of the natural gas type containing the above-mentioned constituents, the lowering of the temperature of the gas mixture is imposed by the sole production of the cut of natural gas liquid, no other operation being performed at this temperature level.

Dans ce type de schéma de traitement, la réalisation en série d'opérations, qui s'appuient sur des principes très différents et sont conduites à des niveaux de température divers, présente de sérieux inconvénients. Il n'y a que peu de possibilité d'intégration thermique, ce qui rend ledit schéma de traitement extrêmement onéreux au plan énergétique et au plan des investissements.In this type of treatment scheme, carrying out series of operations, which are based on very different principles and are carried out at different temperature levels, has serious drawbacks. There is little possibility of thermal integration, which makes said treatment scheme extremely costly from an energy and investment point of view.

On connait également des procédés de traitement de mélanges gazeux du type des gaz naturels, qui permettent de réaliser simultanément l'élimination du C02 contenu dans le mélange gazeux et la production d'hydrocarbures gazeux et d'hydrocarbures liquides et dont le type est le procédé connu sous le nom de procédé RYAN-HOLMES et décrit, notamment, par J. RYAN et F. SCHAFFERT dans la revue CHEMICAL ENGINEERING PROGRESS, Octobre 1984, pages 53 à 56. Dans un tel procédé, le gaz naturel à traiter, après avoir été déshydraté de manière conventionnelle puis réfrigéré, est soumis à une distillation à basse température mise en oeuvre en trois ou quatre étapes successives.There are also known processes for treating gaseous mixtures of the natural gas type, which make it possible to simultaneously carry out the elimination of the C0 2 contained in the gaseous mixture and the production of gaseous hydrocarbons and liquid hydrocarbons, the type of which is process known as the RYAN-HOLMES process and described, in particular, by J. RYAN and F. SCHAFFERT in the journal CHEMICAL ENGINEERING PROGRESS, October 1984, pages 53 to 56. In such a process, the natural gas to be treated, after having been dehydrated in a conventional manner and then refrigerated, is subjected to a low temperature distillation carried out in three or four successive stages.

Dans le mode de réalisation en trois étapes, le gaz naturel déshydraté et réfrigéré est séparé, dans une première colonne (déméthaniseur) en tête de laquelle est injecté un additif consistant en une fraction liquide d'hydrocarbures en C4 et plus, en une phase gazeuse renfermant le méthane et les composés plus légers et une fraction liquide contenant les hydrocarbures en C2 et plus et le C02. Cette fraction liquide est séparée, dans une deuxième colonne (dé-éthaniseur) dans laquelle on introduit également une certaine quantité de l'additif, en une fraction de tête consistant en C02 et en une fraction de queue renfermant les hydrocarbures en C2 et plus.In the three-stage embodiment, 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 C 4 and higher hydrocarbons, in one phase gas containing methane and lighter compounds and a liquid fraction containing C 2 and higher hydrocarbons and C0 2 . This liquid fraction is separated, in a second column (de-ethanizer) into which a certain amount of the additive is also introduced, into an overhead fraction consisting of C0 2 and a bottom fraction containing the C 2 hydrocarbons and more.

Ladite fraction de queue est ensuite séparée, dans une troisième colonne, en une fraction de tête consistant en une coupe liquide d'hydrocarbures en C2 à C4 et en une fraction de queue consistant en une coupe liquide d'hydrocarbures en C4 et plus, qui contient la majeure partie des butanes et des hydrocarbures supérieurs présents dans le gaz naturel traité et dont on prélève la quantité appropriée pour constituer l'additif injecté dans les première et seconde colonnes. L'utilisation de cet additif évite la cristallisation de C02 en tête du déméthaniseur et assure la rupture de l'azéotrope qui se forme entre l'éthane et C02 et facilite la séparation de ces composés dans le dééthaniseur. Le procédé précité repose donc pour l'essentiel sur des opérations de distillation en série.Said tail fraction is then separated, in a third column, into an overhead fraction consisting of a liquid cut of C 2 to C 4 hydrocarbons and into a tail fraction consisting of a liquid cut of C 4 to C hydrocarbons and plus, which contains most of the butanes and higher hydrocarbons present in the treated natural gas and from which the appropriate quantity is taken to constitute the additive injected in the first and second columns. The use of this additive avoids the crystallization of C0 2 at the top of the demethanizer and ensures the rupture of the azeotrope which forms between ethane and C0 2 and facilitates the separation of these compounds in the deethanizer. The aforementioned process is therefore essentially based on serial distillation operations.

L'invention propose un procédé de décarbonatation et de dégazolinage simultanés de mélanges gazeux, qui sont disponibles sous une pression absolue supérieure à 0,5 MPa et sont constitués principalement d'hydrocarbures consistant en méthane et hydrocarbures en C2 et plus et renferment également C02 et éventuellement un ou plusieurs composés non sulfurés à bas point d'ébullition tels que H2, CO, N2 et argon, de tels mélanges gazeux étant par exemple du type des gaz naturels, ledit procédé permettant d'atteindre plus facilement et à moindre coût, en comparaison aux procédés connus, l'objectif d'une séparation du mélange gazeux en les trois composantes, à savoir gaz traité consistant principalement en méthane, coupe liquide d'hydrocarbures à majorité d'hydrocarbures en C3 et plus et renfermant selon les besoins une quantité plus au moins importante d'éthane et courant de C02, qui ont les spécifications définies plus haut.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 C 2 and more hydrocarbons and also contain C0 2 and optionally one or more low-boiling non-sulfur compounds such as H 2 , CO, N 2 and argon, such gaseous mixtures being for example of the natural gas type, said process making it possible to achieve more easily and at lower cost, in comparison with known processes, the objective of gas mixture in the three components, namely treated gas consisting mainly of methane, liquid cut of hydrocarbons with predominantly C 3 and more hydrocarbons and containing, as required, a more or less significant quantity of ethane and current of C0 2 , which have the specifications defined above.

Le procédé selon l'invention est du type du procède qui est décrit dans la citation US-A-3770622 et dans lequel on met le mélange gazeux en contact, dans une zone de lavage, avec un solvant consistant en un liquide qui dissout préférentiellement C02 et les hydrocarbures en C2 et plus et qui possède d'une part, à la pression atmosphérique, une température d'ébullition supérieure à 40 ° C et d'autre part, à - 30 ° C, une viscosité inférieure à 0,1 Pa.s, en opérant à une température suffisamment basse et avec un rapport des débits de mélange gazeux à traiter et de solvant tel que l'on produise, d'une part, un gaz traité consistant principalement en méthane et présentant une teneur molaire en C02 au plus égale à 2 % et, d'autre part, une phase liquide appelée solvant riche et formée du solvant enrichi en C02 et en une fraction d'hydrocarbures en C2 et plus renfermant au moins 80 % molaire des hydrocarbures en C3 et plus présents dans le mélange gazeux à traiter, on soumet le solvant riche à un traitement de déméthanisation au moins partielle, par détente séparant ledit solvant riche en une phase liquide appauvrie en méthane et appelée solvant riche déméthanisé et en une phase gazeuse riche en méthane, qui peut être éventuellement réunie au mélange gazeux à traiter avant la mise en contact de ce dernier avec le solvant, et on soumet le solvant riche déméthanisé à un traitement produisant un courant de gaz acide, qui renferme le C02 présent dans le solvant riche déméthanisé, produisant également un mélange d'hydrocarbures appelé coupe d'hydrocarbures et produisant enfin un solvant régénéré, qui est recyclé vers la zone de lavage.The process according to the invention is of the type of process which is described in the US-A-3770622 quotation and in which the gas mixture is brought into contact, in a washing zone, with a solvent consisting of a liquid which preferentially dissolves C0 2 and C 2 and higher hydrocarbons 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, on the one hand, a treated gas consisting mainly of methane and having a molar content is produced in C0 2 at most equal to 2% and, on the other hand, a liquid phase called rich solvent and formed of the solvent enriched in C0 2 and in a fraction of hydrocarbons in C 2 and more containing at least 80 mol% of the hydrocarbons in C 3 and more present in the gauze mixture ux to be treated, the rich solvent is subjected to an at least partial demethanization treatment, by expansion separating said rich solvent into a liquid phase depleted in methane and called demethanized rich solvent and into a gaseous phase rich in methane, which can be optionally combined to the gaseous mixture to be treated before the latter is brought into contact with the solvent, and the demethanized rich solvent is subjected to a treatment producing a stream of acid gas, which contains the CO 2 present in the demethanized rich solvent, also producing a mixture of hydrocarbons called hydrocarbon cut and finally producing a regenerated solvent, which is recycled to the washing zone.

Le procédé selon l'invention se distingue du procédé de la citation US-A-3770622, et se caractérise donc, en ce que le traitement du solvant riche déméthanisé est réalisé en soumettant ledit solvant riche déméthaniséThe 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

à une régénération (33) par stripage produisant le solvant régénéré (34) et un mélange gazeux (42) contenant le C02 ainsi que les hydrocarbures en C2 et plus présents dans le solvant riche déméthanisé (27), puis en effectuant un lavage dudit mélange gazeux (42) au moyen d'un solvant hydrocarboné en C5 et plus, dans un espace de lavage (47) opérant à basse température, avec production, d'une part, d'un courant de gaz acide riche en C02, constituant le courant de gaz acide (44) et consistant en la quasi totalité du C02 présent dans le solvant riche déméthanisé renfermant, exprimé en équivalent méthane, moins de 10 % molaire d'hydrocarbures par rapport au C02, et, d'autre part, d'un solvant hydrocarboné riche (45) contenant la presque totalité des hydrocarbures en C2 et plus présents dans le mélange gazeux (42) et en fractionnant par distillation ledit solvant hydrocarboné riche en une fraction d'hydrocarbures, qui constitue la coupe d'hydrocarbures (48) et renferme au moins 80 % molaire des hydrocarbures en C3 et plus présents dans le gaz à traiter, et en un solvant hydrocarboné régénéré (50) en C5 et plus, que l'on recycle à l'espace de lavage (47) après l'avoir réfrigéré (52).to a regeneration (33) by stripping producing the regenerated solvent (34) and a gaseous mixture (42) containing the C0 2 as well as the C 2 and higher hydrocarbons present in the rich demethanized solvent (27), then by washing of said gaseous mixture (42) by means of a C 5 and higher hydrocarbon solvent, in a washing space (47) operating at low temperature, with the production, on the one hand, of a stream of acid gas rich in C0 2 , constituting the acid gas stream (44) and consisting of almost all of the C0 2 present in the demethanized rich solvent containing, expressed in methane equivalent, less than 10 mol% of hydrocarbons relative to C0 2 , and, d on the other hand, a rich hydrocarbon solvent (45) containing almost all of the C 2 and more hydrocarbons present in the gas mixture (42) and by fractionating by distillation said hydrocarbon solvent rich in a hydrocarbon fraction, which constitutes cutting hydrocarbons (48) and contains at least 80 mol% of C 3 and higher hydrocarbons present in the gas to be treated, and in a regenerated hydrocarbon solvent (50) of C 5 and above, which is recycled to the washing space (47) after having refrigerated it (52).

Par "équivalent méthane", on désigne suivant l'invention autant de pseudo-molécules à un seul atome de carbone qu'il y a d'atomes de carbone dans la molécule considérée d'hydrocarbure.By "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.

Le solvant, qui est défini généralement ci-dessus pour la mise en contact avec le mélange gazeux à traiter aux fins d'absorption du C02 et des hydrocarbures en C2 et plus, possède de préférence une viscosité inférieure à 0,05 Pa.s.The solvent, which is generally defined above for bringing into contact with the gaseous mixture to be treated for the purpose of absorbing C0 2 and C 2 and higher hydrocarbons, preferably has a viscosity of less than 0.05 Pa. s.

Le solvant suivant l'invention peut consister en particulier en un ou plusieurs absorbants liquides sélectifs du C02 et utilisés sous forme anhydre ou en mélange avec de l'eau, le ou lesdits solvants étant choisis parmi les amides de formules

Figure imgb0001

les aldéhydes de formule
Figure imgb0002
les esters de formules
Figure imgb0003
les alcanols en Ci à C4, les diéthers de formule
Figure imgb0004
les diéthers alcools de formule R9O- C2 H4- O - C2 H4 - OH les lactones de formule
Figure imgb0005
et le carbonate de propylène, avec dans ces formules R1 et R2, identiques ou différents, désignant un atome d'hydrogène ou un radical alcoyle en Ci ou C2, R3 étant un radical alcoyle en C3 ou C4, R6 étant un radical alcoyle en C2 à C4 ou un radical
Figure imgb0006
avec R8 désignant un radical alcoyle en Ci ou C2 et n étant égal à 1 ou 2, R7 étant un radical alcoyle en C1 ou C2 ou un radical
Figure imgb0007
Rg désignant un radical alcoyle en Ci à C4 et p étant un nombre entier allant de 2 à 4.The solvent according to the invention may consist in particular of one or more liquid absorbents selective for CO 2 and used in anhydrous form or in mixture with water, the said solvent (s) being chosen from the amides of formulas
Figure imgb0001
aldehydes of formula
Figure imgb0002
formula esters
Figure imgb0003
alkanols Ci -C 4 diethers of formula
Figure imgb0004
diether alcohols of formula R 9 O- C 2 H 4 - O - C 2 H 4 - OH lactones of formula
Figure imgb0005
and propylene carbonate, with in these formulas R 1 and R 2 , identical or different, denoting a hydrogen atom or an alkyl radical in Ci or C 2 , R 3 being an alkyl radical in C 3 or C 4 , R 6 being a C 2 -C 4 alkyl radical or a radical
Figure imgb0006
with R 8 denoting an alkyl radical Ci or C 2 and n is 1 or 2, R 7 being an alkyl radical in C 1 -C 2 or a radical
Figure imgb0007
Rg denotes an alkyl to C 4 and p is an integer from 2 to 4.

Des exemples non limitatifs d'absorbants organiques liquides répondant aux formules ci-dessus sont tels que N,N-diméthylformamide, N,N-diméthylacétamide, diméthoxyméthane, diéthoxyméthane, diméthoxy-1,1 éthane, méthanol, éthanol, diméthyléther de l'éthylène glycol, diméthyléther du diéthylèneglycol, monométhyléther de l'éthylèneglycol, butyrolactone, propiolactone et carbonate de propylène.Non-limiting 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.

La température de mise en contact du mélange gazeux à traiter avec le solvant, dans la zone de lavage, est de préférence comprise entre 0 °C et -45 °C.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.

La zone de lavage consiste avantageusement en une ou plusieurs colonnes de lavage renfermant le nombre approprié d'étages théoriques de lavage, lesdites colonnes étant, par exemple, du type des colonnes à plateaux ou encore des colonnes à garnissage. Avantageusement on maintient substantiellement constante la température dans chacune des colonnes de lavage par échange indirect de chaleur, effectué en un ou plusieurs points de la colonne considérée, entre le milieu fluide contenu dans cette colonne et un fluide réfrigérant.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 even packed columns. Advantageously, 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 in question, between the fluid medium contained in this column and a refrigerating fluid.

Le traitement de déméthanisation appliqué au solvant riche est réalisé, en particulier, en deux étapes, à savoir une première étape dans laquelle ledit solvant riche est soumis à une première détente à une pression intermédiaire propre à libérer une fraction importante du méthane dissous dans ledit solvant à déméthaniser et à produire un premier gaz riche en méthane et un fluide prédéméthanisé et une seconde étape dans laquelle le fluide prédéméthanisé est soumis à une seconde détente puis à une distillation de manière à produire un second gaz riche en méthane et le solvant riche déméthanisé, le second gaz riche en méthane étant comprimé jusqu'à la pression du premier gaz riche en méthane puis mélangé à ce dernier pour constituer la phase gazeuse riche en méthane.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 at an intermediate pressure capable of releasing a large fraction of the methane dissolved in said solvent to demethanize and produce a first gas rich in methane and a premethanized fluid and a second step in which the premethanized fluid is subjected to a second expansion then to a distillation of so as to produce 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.

La phase gazeuse riche en méthane, résultant du traitement de déméthanisation appliqué au solvant riche, est avantageusement comprimée jusqu'à la pression du mélange gazeux à traiter, puis elle est refroidie et mélangée au mélange gazeux à traiter avant la mise en contact de ce dernier avec le solvant dans la zone de lavage.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.

Avantageusement la régénération du solvant riche déméthanisé est mise en oeuvre en réchauffant ledit solvant jusqu'à une température proche de l'ambiante, en partageant le solvant réchauffé en un premier et un second courants, en dirigeant le premier courant directement vers une zone de régénération, en dirigeant le second courant vers ladite zone de régénération après l'avoir réchauffé par échange indirect de chaleur avec le solvant régénéré, et en soumettant le solvant à une distillation dans la zone de régénération. La dite distillation peut être effectuée en présence d'un courant de gaz inerte, par exemple azote, injecté dans la zone de régénération.Advantageously, the regeneration of the demethanized rich solvent is carried out by reheating said solvent to a temperature close to ambient, by dividing the reheated solvent into first and second streams, directing the first stream directly to a regeneration zone by directing the second stream to said regeneration zone after having heated it by indirect heat exchange with the regenerated solvent, and by subjecting the solvent to distillation in the regeneration zone. Said distillation can be carried out in the presence of a stream of inert gas, for example nitrogen, injected into the regeneration zone.

Lorsque le mélange gazeux à traiter renferme de l'eau et/ou des hydrocarbures en C5 et plus, il est avantageusement soumis à un prétraitement destiné à éliminer tout ou partie de ces composés avant d'être mis en contact avec le solvant dans la zone de lavage.When the gaseous mixture to be treated contains water and / or C 5 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 washing area.

Ce prétraitement peut consister en une distillation réalisée éventuellement en présence de solvant, prélevé sur le solvant injecté dans la zone de lavage, pour produire le mélange gazeux prétraité présentant une teneur en hydrocarbures en C6 et plus inférieure à 0,1 % en poids, une fraction d'hydrocarbures dits lourds renfermant la quasitotalité des hydrocarbures en C6 et plus et tout ou partie des hydrocarbures en C5 et, éventuellement, un liquide consistant en un mélange de solvant et d'eau. Ladite distillation du mélange gazeux est effectuée à une température au moins égale à la température régnant dans la zone de lavage.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 C 6 hydrocarbon content and more than 0.1% by weight, a fraction of so-called heavy hydrocarbons containing almost all of the C 6 and higher hydrocarbons and all or part of the C 5 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.

L'invention sera mieux comprise à la lecture de la description donnée ci-après de l'une de ses formes de mise en oeuvre faisant appel à l'installation schématisée sur la figure du dessin annexé.The invention will be better understood on reading the description given below of one of its forms of implementation using the installation shown schematically in the figure of the accompanying drawing.

En se référant à la figure, le mélange gazeux a traiter arrivant par le conduit 1 est introduit dans la partie inférieure d'une colonne 2 de distillation, dans laquelle ledit mélange gazeux est distillé éventuellement en présence de solvant prélevé, par un conduit 41 débouchant dans la partie supérieure de la colonne 2, sur le solvant régénéré 38 amené à la colonne 5 de lavage, avant passage dudit solvant dans une zone 39 de réfrigération montée sur le conduit 6 d'injection du solvant régénéré dans ladite colonne 5 de lavage, de manière à produire d'une part un mélange gazeux séché, évacué de la colonne 2 par un conduit 3 et dont la teneur en hydrocarbures en C6 et plus est inférieure à 0,1 % en poids, et d'autre part une coupe hydrocarbonée renfermant la quasi-totalité des hydrocarbures en C6 et plus et éventuellement tout ou partie des hydrocarbures en Cs, soutirée de la colonne 2 par un conduit 4 et éventuellement un liquide soutiré de la colonne 2 par un conduit 54 et consistant en un mélange de solvant et l'eau.Referring to the figure, 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 gaseous mixture, evacuated from column 2 by a line 3 and whose hydrocarbon content in C 6 and more is less than 0.1% by weight, and on the other hand a cut hydrocarbon containing almost all of the C 6 and more hydrocarbons and possibly all or part of the C s hydrocarbons, withdrawn from column 2 by a conduit 4 and optionally a liquid withdrawn from the column 2 via a conduit 54 and consisting of a mixture of solvent and water.

Le mélange gazeux séché sortant de la colonne 2 par le conduit 3 est introduit dans la partie inférieure d'une colonne 5 de lavage, par exemple du type colonne à plateaux, dans laquelle il est mis en contact, à contrecourant, avec du solvant froid régénéré injecté dans la partie supérieure de la colonne 5 par le conduit 6, après passage dans le réfrigérant 39, cette mise en contact étant effectuée à une température comprise, par exemple, entre O ° C et -45 ° C, ladite température étant contrôlée par passage du milieu liquide contenu dans la colonne 5 dans des réfrigérants 7. En tête de la colonne 5 on évacue, par un conduit 8, un gaz traité consistant principalement en méthane et appauvri en C02, ledit gaz traité étant réchauffé dans un système 9 de réchauffage puis dirigé, par un conduit 10, vers une zone d'utilisation, tandis qu'en fond de ladite colonne 5 on soutire, par un conduit 11, une phase liquide constituée du solvant enrichi en C02 et autres composés absorbés et appelée solvant riche.The dried gaseous mixture leaving column 2 via 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. At the head of column 5, a treated gas consisting mainly of methane and depleted in C0 2 is discharged, via a conduit 8, said treated gas being heated in a system 9 for 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 C0 2 e t other compounds absorbed and called rich solvent.

On réalise la mise en contact du mélange gazeux séché avec le solvant dans la colonne 5 de lavage à une température appropriée dans l'intervalle O ° C à -45 ° C et avec un rapport des débits de mélange gazeux à traiter et de solvant tel que d'une part le gaz traité recueilli, par le conduit 8, en tête de la colonne 5 ait une teneur molaire en C02 au plus égale à 2 % et que d'autre part le solvant riche, s'écoulant par le conduit 11, renferme au moins 80 % molaire des hydrocarbures en C3 et plus présents dans le mélange gazeux séché introduit dans la colonne 5.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 content of C0 2 at most equal to 2% and that on the other hand the rich solvent, flowing through the line 11, contains at least 80 mol% of the C 3 and higher hydrocarbons present in the dried gas mixture introduced into column 5.

Le solvant riche circulant dans le conduit 11 est introduit, après passage à travers la vanne 12 de détente, dans la partie supérieure d'un ballon de détente 13 dans lequel se sépare un premier gaz riche en méthane, que l'on évacue en tête du ballon 13 par un conduit 14, et un solvant riche prédéméthanisé, que l'on soutire en fond du ballon 13 par un conduit 15. Ledit solvant riche prédéméthanisé est soumis à une seconde détente à travers une vanne de détente 16 suivie d'une distillation dans une colonne 17 de distillation pourvue d'un rebouilleur 18, de manière à produire un second gaz riche en méthane, que l'on évacue en tête de la colonne 17 par un conduit 19, et une phase liquide appauvrie en méthane, appelée solvant riche déméthanisé, qui est soutirée en fond de la colonne 17 par un conduit 27. Le second gaz riche en méthane circulant dans le conduit 19 est amené à passer dans un compresseur 20 d'où il sort, par un conduit 21, à une pression sensiblement égale à celle du premier gaz riche en méthane passant dans le conduit 14, puis ces deux gaz riches en méthane sont mélangés dans le conduit 22 et la phase gazeuse résultant de ce mélange est recyclée, par l'intermédiaire d'un compresseur 23 dont la sortie est prolongée par un conduit 24, un réfrigérant 25 et un conduit 26, dans le conduit 3 d'amenée du mélange gazeux séché à la colonne 5 de lavage.The rich solvent circulating in the conduit 11 is introduced, after passage through the expansion valve 12, into the upper part of an expansion tank 13 in which a first methane-rich gas separates, which is removed at the head of the flask 13 by a conduit 14, and a predemethanized rich solvent, which is withdrawn from 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 discharged at the head of column 17 through a pipe 19, and a methane-depleted liquid phase, called demethanized rich solvent, which is drawn off at the bottom of the column 17 through a pipe 27. The second methane-rich gas circulating in the pipe 19 is caused to pass into a compressor 20 from which it exits, via a conduit 21, at a pressure substantially equal to that of the first gas rich in methane passing through the conduit 14, then these two gases rich in methane are mixed in the conduit 22 and the gas phase resulting from this mixture is recycled, by means of a compressor 23, the outlet of which is extended by a conduit 24, a coolant 25 and a conduit 26, in the conduit 3 for supplying the dried gaseous mixture to washing column 5.

Le solvant riche déméthanisé, soutiré de la colonne 17 par le conduit 27, traverse une vanne de détente 29 puis un système 28 de réchauffage, dans lequel il est amené à une température proche de l'ambiante, puis il est amené à une colonne 33 de régénération pourvue d'un rebouilleur 40 après avoir été partagé en un premier courant 30, qui est introduit directement dans la colonne 33 de régénération, et un second courant 31, qui est introduit dans ladite colonne de régénération après avoir été réchauffé dans un échangeur indirect de chaleur 35. La régénération peut être réalisée en présence d'un courant de gaz inerte, notamment un courant d'azote, injecté dans la partie inférieure de la colonne 33 par un conduit 43. Ladite régénération produit, d'une part, un solvant régénéré soutiré en fond de la colonne 33, par un conduit 34, et utilisé dans l'échangeur de chaleur 35, pour réchauffer le second courant 31 de solvant riche déméthanisé à régénérer, avant d'être recyclé, par la pompe 37 et le conduit 38, vers la colonne 5 de lavage, et d'autre part un mélange gazeux évacué en tête de la colonne 33, par un conduit 42, et contenant le C02 ainsi que les hydrocarbures en C2 et plus présents dans le solvant riche déméthanisé.The demethanized rich solvent, withdrawn from the column 17 by the conduit 27, passes through an expansion valve 29 then a heating system 28, in which it is brought to a temperature close to ambient, then it is brought to a column 33 regeneration provided with a reboiler 40 after being divided into a first stream 30, which is introduced directly into the regeneration column 33, and a second stream 31, which is introduced into said regeneration column after having been reheated in an exchanger indirect heat 35. The regeneration can be carried out in the presence of a stream of inert gas, in particular a stream of nitrogen, injected into the lower part of the column 33 through a conduit 43. Said regeneration produces, on the one hand, a regenerated solvent withdrawn from the bottom of the column 33, through a pipe 34, and used in the heat exchanger 35, to heat the second stream 31 of demethanized rich solvent to be regenerated, before being recycled, by the pump 37 and the conduit 38, towards the washing column 5, and on the other hand a gas mixture discharged at the head of the column 33, by a conduit 42, and containing the C0 2 as well as the C 2 and higher hydrocarbons present in the rich demethanized solvent.

Le mélange gazeux passant dans le conduit 42 est lavé à contre-courant, dans une tour de lavage 47 munie d'un réfrigérant 46 en tête et d'un rebouilleur 70 en fond et opérant à basse température, au moyen d'un solvant hydrocarboné en C5 et plus amené à la tour de lavage 47 par un conduit 53, ledit lavage produisant, d'une part, un courant 44 de gaz acide riche en C02, qui renferme la quasi-totalité du C02 présent dans le solvant riche déméthanisé et possède, exprimée en équivalent méthane, une teneur en hydrocarbures inférieure à 10 % molaire par rapport au C02, et, d'autre part, un solvant hydrocarboné riche 45 pratiquement exempt de C02 et contenant la presque totalité des hydrocarbures en C2 et plus présents dans le mélange gazeux arrivant par le conduit 42.The gaseous mixture passing through the conduit 42 is washed against the current, in a washing tower 47 provided with a condenser 46 at the head and a reboiler 70 at the bottom and operating at low temperature, using a hydrocarbon solvent in C 5 and over brought to the washing tower 47 by a conduit 53, said washing producing, on the one hand, a stream 44 of acid gas rich in C0 2 , which contains almost all of the C0 2 present in the solvent rich demethanized and has, expressed in methane equivalent, a hydrocarbon content of less than 10 mol% relative to C0 2 , and, on the other hand, a rich hydrocarbon solvent 45 practically free of C0 2 and containing almost all of the hydrocarbons in C 2 and more present in the gas mixture arriving via line 42.

Le solvant hydrocarboné riche 45 est amené à une colonne 49 de régénération dans laquelle ledit solvant 45 est soumis à une distillation pour produire, d'une part, une fraction d'hydrocarbures 48 constituant la coupe d'hydrocarbures en C2 et plus renfermant au moins 80 % molaire des hydrocarbures en C3 et plus contenus dans le gaz à traiter amené à la colonne 5 de lavage par le conduit 3, et, d'autre part, un solvant hydrocarboné 50 régénéré, qui est recyclé, par la pompe 51, à la colonne tour de lavage 47 après réfrigération dans le système 52 et passage dans le conduit 53.The rich hydrocarbon solvent 45 is brought to a regeneration column 49 in which said solvent 45 is subjected to distillation to produce, on the one hand, a fraction of hydrocarbons 48 constituting the cut of C 2 hydrocarbons and more containing the minus 80 mol% of the C 3 hydrocarbons and more contained in the gas to be treated brought to the washing column 5 by the line 3, and, on the other hand, a regenerated hydrocarbon solvent 50, which is recycled, by the pump 51 , to the washing tower column 47 after refrigeration in the system 52 and passage in the conduit 53.

Pour compléter la description qui précède, on donne ci-après, à titre non limitatif, un exemple de mise en oeuvre du procédé selon l'invention.To complete the above description, an example of implementation of the method according to the invention is given below, without implied limitation.

EXEMPLE:EXAMPLE:

En faisant appel à une installation analogue à celle schématisée sur la figure du dessin annexé et fonctionnant comme décrit précédemment, on traitait un mélange gazeux ayant la composition molaire suivante :

Figure imgb0008
Using an installation similar to that shown schematically in the figure of the appended drawing and operating as described above, a gas mixture having the following molar composition was treated:
Figure imgb0008

Le mélange gazeux à traiter, arrivant par le conduit 1 avec un débit de 10 000 kmoles/h, une température de 30 ° C et une pression de 5 000 kPa était introduit dans la colonne 2 d'élimination des hydrocarbures en C6 et plus. Dans cet exemple, le mélange gazeux à traiter étant sec, aucune addition de solvant n'était réalisée par le conduit 41.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 elimination of C 6 and higher hydrocarbons. . In this example, the gas mixture to be treated being dry, no addition of solvent was carried out via line 41.

Par le conduit 4 de la colonne 2, on évacuait 352 kmoles/h d'une coupe hydrocarbonée lourde ayant une pression de 5 000 kPa et une température égale à 30 ° C, ladite coupe ayant la composition suivante :

Figure imgb0009
Via line 4 of column 2, 352 kmol / h of a heavy hydrocarbon fraction having a pressure of 5,000 kPa and a temperature equal to 30 ° C. was discharged, said fraction having the following composition:
Figure imgb0009

Par le conduit 3 en tête de la colonne 2 on évacuait 9648 kmoles/h d'un mélange gazeux prétraité ayant une températeur de -20 °C et une pression de 4950 kPa, ledit mélange gazeux prétraité ayant la composition molaire suivante :

Figure imgb0010
Via line 3 at the head of column 2, 9648 kmol / h of a pretreated gas mixture having a temperature of -20 ° C. and a pressure of 4950 kPa were discharged, said pretreated gas mixture having the following molar composition:
Figure imgb0010

Le mélange gazeux prétraité était mis en contact avec 6000 kmoles/h de solvant consistant en un mélange de méthanol et d'eau dans un rapport molaire égal à 95:5 et présentant une pression de 5000 kPa et une température égale à -30 °C, ladite mise en contact étant réalisée dans une colonne 5 de lavage comportant 14 plateaux et opérant à - 30 ° C sous une pression de 4900 kPa. Les réfrigérants 7 équipant la colonne 5 de lavage permettaient de maintenir la température dans ladite colonne à la valeur désirée.The pretreated gas mixture was brought into contact with 6000 kmol / h of solvent consisting of a mixture of methanol and water in a molar ratio equal to 95: 5 and having a pressure of 5000 kPa and a temperature equal to -30 ° C. , said contacting being carried out in a washing column 5 comprising 14 plates and operating at - 30 ° 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.

En tête de la colonne 5, on évacuait, par le conduit 8, 7405 kmoles/h d'un gaz traité ayant une pression de 4900 kPa et une température de -30 ° C, ledit gaz traité ayant la composition molaire suivante :

Figure imgb0011
At the head of column 5, 7,405 kmol / h were evacuated through line 8 of a treated gas having a pressure of 4,900 kPa and a temperature of -30 ° C, said treated gas having the following molar composition:
Figure imgb0011

En fond de la colonne 5 de lavage, on soutirait, par le conduit 11, 9182 kmoles/h de solvant riche ayant une température de -30 ° C et une pression de 4900 kPa, ledit solvant riche ayant la composition molaire ci-après:

Figure imgb0012
At the bottom of the washing column 5, 9,182 kmol / h of rich solvent having a temperature of -30 ° C. and a pressure of 4,900 kPa were withdrawn through line 11, said rich solvent having the following molar composition:
Figure imgb0012

Le gaz traité, évacué par le conduit 8, était réchauffé jusqu'à température ambiante dans le système échangeur de chaleur 9, ce qui permet d'assurer la réfrigération du solvant dans le réfrigérant 39. Le gaz traité réchauffé est dirigé par le conduit 10 vers un gazoduc d'expédition.The treated gas, discharged through line 8, was warmed up to ambient temperature in the heat exchanger system 9, which makes it possible to ensure the refrigeration of the solvent in the refrigerant 39. The heated treated gas is directed through line 10 to an expedition pipeline.

La déméthanisation du solvant riche comportait tout d'abord une première détente dudit solvant à une pression de 3000 kPa, le solvant riche détendu alimentant le ballon 13 de détente dans lequel on produisait 362kmoles/h d'un premier gaz renfermant 68 % molaire de méthane, que l'on évacuait en tête du ballon 13 par le conduit 14, et un solvant riche prédéméthanisé soutiré dudit ballon par le conduit 15 et dont la teneur molaire en méthane a été réduite de 6,11 % à 3,57 %. Le solvant riche prédéméthanisé, dont la température était égale à -33,6 °C, était détendu dans la vanne 16 et alimentait ensuite la colonne 17 de distillation comportant 10 plateaux et opérant à 1800 kPa. La colonne 17 produisait 577 kmoles/h d'un second gaz riche en méthane, évacué par le conduit 19 sous une pression de 1800 kPa et une température de -37 ° C, et un solvant riche déméthanisé soutiré de la colonne 17 par le conduit 27 avec un débit de 8243 kmoles/h, une pression de 1800 kPa et une température de -8,2 °C.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 362 kmol / h of a first gas containing 68 mol% of methane were produced. , 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 was reduced from 6.11% to 3.57%. The premethanized rich solvent, the temperature of which was equal to -33.6 ° C., was expanded in valve 16 and then fed to the distillation column 17 comprising 10 plates and operating at 1800 kPa. Column 17 produced 577 kmol / h of a second gas rich in methane, evacuated through line 19 under a pressure of 1800 kPa and a temperature of -37 ° C, and a demethanized rich solvent withdrawn from column 17 through line 27 with a flow rate of 8243 kmol / h, a pressure of 1800 kPa and a temperature of -8.2 ° C.

Le solvant riche déméthanisé avait la composition molaire suivante :

Figure imgb0013
The demethanized rich solvent had the following molar composition:
Figure imgb0013

Le second gaz riche en méthane était comprimé, dans le compresseur 20, jusqu'à la pression du premier gaz riche en méthane, à savoir 3000 kPa. Le gaz comprimé sortant du compresseur 20, par le conduit 21, était mélangé au premier gaz riche en méthane pour constituer la phase gazeuse riche en méthane 22, qui était ensuite comprimée, dans le compresseur 23, jusqu'à la pression du mélange gazeux a traiter, à savoir 5000 kPa, ladite phase gazeuse comprimée étant ajoutée à travers le conduit 24, le réfrigérant 25 et le conduit 26, au mélange gazeux prétraité circulant dans le conduit 3.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.

La phase gazeuse comprimée riche en méthane passant dans le conduit 26 avait une température de -20 °C, une pression de 5 000 kPa et un débit de 938 kmoles/h.The compressed methane-rich gaseous phase passing through line 26 had a temperature of -20 ° C, a pressure of 5,000 kPa and a flow rate of 938 kmol / h.

La composition molaire de ladite phase gazeuse riche en méthane circulant dans le conduit 26 était la suivante :

Figure imgb0014
The molar composition of said methane-rich gas phase flowing in line 26 was as follows:
Figure imgb0014

Le solvant riche déméthanisé, après détente dans la vanne 29 et réchauffage dans le système 28 de réchauffage, avait une température de 10°C et une pression de 800 kpa. Ledit solvant réchauffé était alors partagé en un premier courant 30 ayant un débit de 4533 kmoles/h, qui était dirigé directement vers la colonne 33 de régénération, et en un second courant 31, qui était réchauffé à 70 °C dans l'échangeur de chaleur 35 avant d'être acheminé vers la colonne de régénération 33. Cette colonne opérait sous une pression de 700 kPa et comportait 18 plateaux, les courants 30 et 31 étant injectés respectivement au niveau des plateaux 8 et 12, comptés à partir du sommet de la colonne.The demethanized rich solvent, after expansion in the valve 29 and heating in the heating system 28, had a temperature of 10 ° C and a pressure of 800 kpa. Said heated solvent was then divided into a first stream 30 having a flow rate of 4533 kmol / h, which was directed directly to the regeneration column 33, and into a second stream 31, which was heated to 70 ° C. in the heat exchanger. heat 35 before being conveyed to the regeneration column 33. This column operated under a pressure of 700 kPa and included 18 plates, the currents 30 and 31 being injected respectively at the plates 8 and 12, counted from the top of the column.

La colonne de régénération 33 produisait en tête un mélange gazeux renfermant C02 et les hydrocarbures en C2 et plus, qui était évacué par le conduit 42 avec une température de -14 °C, une pression de 700 kPa et un débit de 2244 kmoles/h et en fond un solvant régénéré soutiré de la colonne de régénération 33 par le conduit 34.The regeneration column 33 produced at the head a gaseous mixture containing C0 2 and the hydrocarbons in C 2 and more, which was evacuated via line 42 with a temperature of -14 ° C, a pressure of 700 kPa and a flow rate of 2244 kmol / h and at the bottom a regenerated solvent withdrawn from the regeneration column 33 through the pipe 34.

Le mélange gazeux passant dans le conduit 42 avait la composition molaire suivante :

Figure imgb0015
The gas mixture passing through line 42 had the following molar composition:
Figure imgb0015

Le solvant régénéré est refroidi par passage dans l'échangeur de chaleur 35, puis recomprimé à une pression de 5000 kPa par la pompe 37, et il est ensuite dirigé par le conduit 38 d'une part en quantité majeure vers la colonne 5 de lavage, à travers le réfrigérant 39 et le conduit 6.The regenerated solvent is cooled by passage through the heat exchanger 35, then recompressed to a pressure of 5000 kPa by the pump 37, and it is then directed through the conduit 38 on the one hand in a major quantity to the washing column 5 , through the refrigerant 39 and the conduit 6.

Le mélange gazeux passant dans le conduit 42 était lavé à contre courant dans la tour de lavage 47 à l'aide d'un solvant hydrocarboné consistant en majorité en hexane. La tour 47 comportait 35 plateaux et opérait sous une pression de 700 kPa avec une température de -30 ° C en tête au niveau du réfrigérant 46.The gas mixture passing through line 42 was washed against the current in washing tower 47 using a hydrocarbon solvent consisting mainly of hexane. Tower 47 had 35 platforms and operated under a pressure of 700 kPa with a temperature of -30 ° C at the head at the level of the refrigerant 46.

L'alimentation de la tour 47 en solvant, par le conduit 53, et en mélange gazeux, par le conduit 42, était effectuée respectivement sur le premier plateau et sur le plateau 21 de ladite tour. La tour de lavage 47 produisait en tête un courant de gaz acide 44 riche en C02 et ayant une teneur en hydrocarbures, exprimée en équivalent méthane, inférieure à 10 % molaire par rapport au C02, ledit courant de gaz acide ayant une température de -30 °C, une pression de 650 kPa et un débit de 1685 kmoles/h, et en fond un solvant hydrocarboné 45 à teneur réduite en C02 ayant une température de 95,8 °C, une pression de 730 kPa et un débit de 5059 kmoles/h.The supply of tower 47 with solvent, via line 53, and in gaseous mixture, through line 42, was carried out respectively on the first plate and on plate 21 of said tower. The washing tower 47 produced at the head an acid gas stream 44 rich in C0 2 and having a hydrocarbon content, expressed in methane equivalent, of less than 10 mol% with respect to C0 2 , said acid gas stream having a temperature of -30 ° C, a pressure of 650 kPa and a flow rate of 1685 kmol / h, and in the background a hydrocarbon solvent 45 with reduced C0 2 content having a temperature of 95.8 ° C, a pressure of 730 kPa and a flow rate 5059 kmol / h.

La composition molaire du courant de gaz acide 44 était la suivante :

Figure imgb0016
The molar composition of the acid gas stream 44 was as follows:
Figure imgb0016

Le solvant riche hydrocarboné 45 avait la composition molaire suivante :

Figure imgb0017
The rich hydrocarbon solvent 45 had the following molar composition:
Figure imgb0017

Le fractionnement du solvant riche hydrocarboné 45 dans la colonne 49 pourvue de 28 plateaux et opérant sous une pression de 600 kPa produisait en tête 561 kmoles/h d'une coupe d'hydrocarbures 48 en C2 et plus ayant une température de 18°C et une pression de 600 kPa et en fond 4500 kmoles/h de solvant hydrocarboné régénéré ayant une température de 142,7°C et une pression de 670 kPa, ledit solvant renfermant, en mole, 98,89 % d'hexane et 1,11 % de butane.The fractionation of the rich hydrocarbon solvent 45 in the column 49 provided with 28 trays and operating under a pressure of 600 kPa produced at the head 561 kmol / h of a cut of hydrocarbons 48 in C 2 and more having a temperature of 18 ° C and a pressure of 600 kPa and at the bottom 4500 kmol / h of regenerated hydrocarbon solvent having a temperature of 142.7 ° C and a pressure of 670 kPa, said solvent containing, in mole, 98.89% of hexane and 1, 11% butane.

La composition molaire de la coupe d'hydrocarbures 48 en C2 et plus était la suivante :

Figure imgb0018
The molar composition of the cut of hydrocarbons 48 at C 2 and above was as follows:
Figure imgb0018

Claims (9)

1. Procédé de décarbonatation et de dégazolinage simultanés d'un mélange gazeux, qui possède une pression absolue supérieure à 0,5 MPa et renferme principalement des hydrocarbures consistant en méthane et hydrocarbures en C2 et plus et comporte également C02 et éventuellement un ou plusieurs composés non sulfurés à bas point d'ébullition tels que H2, CO, N2 et Ar, dans lequel on met le mélange gazeux en contact, dans une zone de lavage (5), avec un solvant (6) consistant en un liquide, qui dissout préférentiellement C02 et les hydrocarbures en C2 et plus et qui possède d'une part, à la pression atmosphérique, une température d'ébullition supérieure à 40 ° C et d'autre part, à -30 ° C, une viscosité inférieure à 0,1 Pa.s, en opérant à une température suffisamment basse et avec un rapport des débits de mélange gazeux à traiter et de solvant tel que l'on produise, d'une part, un gaz traité (8) consistant principalement en méthane et présentant une teneur molaire en C02 au plus égale à 2 % et, d'autre part, une phase liquide appelée solvant riche (11) et formée du solvant enrichi en C02 et en une fraction d'hydrocarbures en C2 et plus renfermant au moins 80 % molaire des hydrocarbures en C3 et plus présents dans le mélange gazeux à traiter, on soumet le solvant riche à un traitement de déméthanisation au moins partielle (12, 17) par détente séparant ledit solvant riche en une phase liquide appauvrie en méthane et appelée solvant riche déméthanisé (27) et en une phase gazeuse riche en méthane (22) et on soumet le solvant riche déméthanisé à un traitement produisant un courant de gaz acide (44), qui renferme le C02 présent dans le solvant riche déméthanisé, produisant également un mélange d'hydrocarbures appelé coupe d'hydrocarbures (48) et produisant enfin un solvant régénéré (34), qui est recyclé vers la zone (5) de lavage, ledit procédé se caractérisant en ce que le traitement du solvant riche déméthanisé est réalisé en soumettant ledit solvant à une régénération (33) par stripage produisant le solvant régénéré (34) et un mélange gazeux (42) contenant le C02 ainsi que les hydrocarbures en C2 et plus présents dans le solvant riche déméthanisé (27), puis en effectuant un lavage dudit mélange gazeux (42) au moyen d'un solvant hydrocarboné en C5 et plus, dans un espace de lavage (47) opérant à basse température, avec production, d'une part, d'un courant de gaz acide riche en C02, constituant le courant de gaz acide (44) et consistant en la quasi totalité du C02 présent dans le solvant riche déméthanisé renfermant, exprimé en équivalent méthane, moins de 10 % molaire d'hydrocarbures par rapport au C02, et, d'autre part, d'un solvant hydrocarboné riche (45) contenant la presque totalité des hydrocarbures en C2 et plus présents dans le mélange gazeux (42) et en fractionnant par distillation ledit solvant hydrocarboné riche en une fraction d'hydrocarbures, qui constitue la coupe d'hydrocarbures (48) et renferme au moins 80 % molaire des hydrocarbures en C3 et plus présents dans le gaz à traiter, et en un solvant hydrocarboné régénéré (50) en C5 et plus, que l'on recycle à l'espace de lavage (47) après l'avoir réfrigéré (52).1. Process for the simultaneous decarbonation and degassing of a gaseous mixture, which has an absolute pressure greater than 0.5 MPa and mainly contains hydrocarbons consisting of methane and C 2 and more hydrocarbons and also comprises C0 2 and optionally one or several low-boiling unsulfurized compounds such as H 2 , CO, N 2 and Ar, in which the gas mixture is brought into contact, in a washing zone (5), with a solvent (6) consisting of a liquid, which preferentially dissolves C0 2 and hydrocarbons in C 2 and above and which has, on the one hand, at atmospheric pressure, a boiling temperature above 40 ° C and, on the other hand, at -30 ° C, a viscosity of 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, on the one hand, a treated gas is produced (8) consisting mainly of methane and presented nt a molar content of C0 2 at most equal to 2% and, on the other hand, a liquid phase called rich solvent (11) and formed of the solvent enriched in C0 2 and in a fraction of hydrocarbons in C 2 and more containing at least 80 mol% of the C 3 and higher hydrocarbons present in the gas mixture to be treated, the rich solvent is subjected to an at least partial demethanization treatment (12, 17) by expansion separating said rich solvent into a liquid phase depleted in methane and called demethanized rich solvent (27) and in a methane-rich gas phase (22) and the demethanized rich solvent is subjected to a treatment producing a stream of acid gas (44), which contains the C0 2 present in the demethanized rich solvent, also producing a mixture of hydrocarbons called hydrocarbon cut (48) and finally producing a regenerated solvent (34), which is recycled to the zone ( 5) washing, said method being characterized in that the treatment of the demethanized rich solvent is carried out by subjecting said solvent to a regeneration (33) by stripping producing the regenerated solvent (34) and a gaseous mixture (42) containing C0 2 as well as the C 2 and higher hydrocarbons present in the demethanized rich solvent (27), then by washing said gaseous mixture (42) using a C 5 and higher hydrocarbon solvent, in a washing space (47 ) operating at low temperature, with the production, on the one hand, of an acid gas stream rich in C0 2 , constituting the acid gas stream (44) and consisting of almost all of the C0 2 present in the demethanized rich solvent containing , expressed in methane equivalent, less than 10 mol% of hydrocarbons relative to C0 2 , and, on the other hand, of a rich hydrocarbon solvent (45) containing almost all of the hydrocarbons C 2 and more present in the gas mixture (42) and by fractionating said hydrocarbon solvent rich in a hydrocarbon fraction by distillation, which constitutes the hydrocarbon fraction (48) and contains at least 80 mol% of the C 3 and higher hydrocarbons present in the gas to treat, and in a regenerated hydrocarbon solvent (50) of C 5 and more, which is recycled to the washing space (47) after having cooled it (52). 2. Procédé selon la revendication 1, caractérisé en ce que le solvant mis en contact avec le mélange gazeux a traiter a une viscosité, à -30 °C, inférieure à 0,05 Pa.s.2. Method according to claim 1, characterized in that the solvent brought into contact with the gaseous mixture to be treated has a viscosity, at -30 ° C, less than 0.05 Pa.s. 3. Procédé selon la revendication 1 ou 2 caractérisé en ce que le solvant mis en contact avec le mélange gazeux à traiter dans la zone (5) de lavage consiste en un ou plusieurs absorbants organiques liquides, utilisés sous forme anhydre ou en mélange avec l'eau, le ou lesdits absorbants étant choisis parmi les amides de formules
Figure imgb0019
 les aldéhydes de formule
Figure imgb0020
 les esters de formules
Figure imgb0021
 les alcanols en Ci à C4, les diéthers de formule
Figure imgb0022
 les diéthers alcools de formule RgO - C2H4 - O - C2 H4-OH, les lactones de formule
Figure imgb0023
et le carbonate de propylène, avec dans ces formules R1 et R2, identiques ou différents, désignant un atome d'hydrogène ou un radical alcoyle en Ci ou C2, R3 étant un radical alcoyle en C3 ou C4, R6 étant un radical alcoyle en C2 à C4 ou un radical
Figure imgb0024
 avec R8 désignant un radical alcoyle en Ci ou C2 et n représentant 1 ou 2, R7 étant un radical alcoyle en C1 ou C2 ou un radical
Figure imgb0025
 Rg désignant un radical alcoyle en Ci à C4 et p étant un nombre entier allant de 2 à 4. 3. Method according to claim 1 or 2 characterized in that the solvent brought into contact with the gaseous mixture to be treated in the washing zone (5) consists of one or more liquid organic absorbents, used in anhydrous form or in mixture with l water, said absorbent (s) being chosen from amides of formulas
Figure imgb0019
 aldehydes of formula
Figure imgb0020
 formula esters
Figure imgb0021
 alkanols Ci -C 4 diethers of formula
Figure imgb0022
 diether alcohols of formula RgO - C 2 H 4 - O - C 2 H 4 -OH, lactones of formula
Figure imgb0023
and propylene carbonate, with in these formulas R 1 and R 2 , identical or different, denoting a hydrogen atom or an alkyl radical in Ci or C 2 , R 3 being an alkyl radical in C 3 or C 4 , R 6 being a C 2 -C 4 alkyl radical or a radical
Figure imgb0024
 with R 8 denoting an alkyl radical Ci or C 2 and n is 1 or 2, R 7 being an alkyl radical in C 1 -C 2 or a radical
Figure imgb0025
 Rg denotes an alkyl to C 4 and p is an integer from 2 to 4. 4. Procédé selon l'une des revendications 1 à 3, caractérisé en ce que la température de mise en contact du mélange gazeux à traiter avec le solvant, dans la zone (5) de lavage, est comprise entre 0 ° C et -45 ° C.4. Method according to one of claims 1 to 3, characterized in that the contacting temperature of the gas mixture to be treated with the solvent, in the washing zone (5), is between 0 ° C and -45 ° C. 5. Procédé selon l'une des revendications 1 à 4, caractérisé en ce que le traitement de déméthanisation appliqué au solvant riche (11) est réalisé en deux étapes, à savoir une première étape dans laquelle ledit solvant riche est soumis à une première détente (12, 13) propre à libérer une fraction importante du méthane dissous dans ledit solvant et à produire un premier gaz riche en méthane (14) et un fluide prédéméthanisé (15) et une seconde étape dans laquelle le fluide prédéméthanisé est soumis à une seconde détente (16) puis à une distillation (17) de manière à produire un second gaz riche en méthane (19) et le solvant riche déméthanisé (27), le second gaz riche en méthane étant comprimé jusqu'à la pression du premier gaz riche en méthane puis mélangé à ce dernier pour constituer la phase gazeuse (22) riche en méthane.5. Method according to one of claims 1 to 4, characterized in that the demethanization treatment applied to the rich solvent (11) is carried out in two stages, namely a first step in which said rich solvent is subjected to a first expansion (12, 13) capable of releasing a large fraction of the methane dissolved in said solvent and of producing a first gas rich in methane (14) and a premethanized fluid (15) and a second step in which the premethanized fluid is subjected to a second expansion (16) then distillation (17) so as to produce a second methane-rich gas (19) and the demethanized rich solvent (27), the second methane-rich gas being compressed to the pressure of the first rich gas in methane and then mixed with the latter to constitute the gas phase (22) rich in methane. 6. Procédé selon l'une des revendications 1 à 5, caractérisé en ce que la phase gazeuse (22) riche en méthane est comprimée jusqu'à la pression du mélange gazeux a traiter, puis elle est refroidie (25) et mélangée au mélange gazeux à traiter avant la mise en contact de ce dernier avec le solvant dans la zone de lavage (5).6. Method according to one of claims 1 to 5, characterized in that the gas phase (22) rich in methane is compressed to the pressure of the gas mixture to be treated, then it is cooled (25) and mixed with the mixture gaseous to be treated before the latter is brought into contact with the solvent in the washing zone (5). 7. Procédé selon l'une des revendications 1 à 6, caractérisé en ce que l'on effectue la régénération du solvant riche déméthanisé en réchauffant (28) ledit solvant jusqu'à une température proche de l'ambiante, puis en partageant le solvant réchauffé en un premier (30) et un second (31) courants, en dirigeant le premier courant (30) directement vers une zone de régénération (33), en dirigeant le second courant (31) vers ladite zone de régénération après l'avoir réchauffé par échange indirect de chaleur (35) avec le solvant régénéré (34) et en soumettant le solvant à une distillation dans la zone (33) de régénération.7. Method according to one of claims 1 to 6, characterized in that the regeneration of the demethanized rich solvent is carried out by heating (28) said solvent to a temperature close to ambient, then sharing the solvent reheated in first (30) and second (31) streams, directing the first stream (30) directly to a regeneration zone (33), directing the second stream (31) to said regeneration zone after having reheated by indirect heat exchange (35) with the regenerated solvent (34) and subjecting the solvent to distillation in the regeneration zone (33). 8. Procédé selon la revendication 7, caractérisé en ce que la distillation du solvant dans la zone (33) de régénération s'effectue en présence d'un courant de gaz inerte (43), par exemple azote, injecté dans ladite zone.8. Method according to claim 7, characterized in that the distillation of the solvent in the regeneration zone (33) is carried out in the presence of a stream of inert gas (43), for example nitrogen, injected into said zone. 9. Procédé selon l'une des revendications 1 à 8, caractérisé en ce que, le mélange gazeux à traiter renfermant de l'eau et/ou des hydrocarbures en C5 et plus, ledit mélange gazeux est soumis à un prétraitement consistant en une distillation (2) effectuée à une température au moins égale à celle régnant dans la zone (5) de lavage et, éventuellement, en présence de solvant, prélevé sur le solvant amené à la zone (5) de lavage, pour produire une fraction (4) d'hydrocarbures dits lourds et renfermant la quasi-totalité des hydrocarbures en C6 et plus et éventuellement tout ou partie des hydrocarbures en Cs, un mélange gazeux prétraité (3) présentant une teneur en hydrocarbures en C6 et plus inférieure à 0,1 % en poids et, éventuellement, un liquide (54) consistant en un mélange de solvant et d'eau.9. Method according to one of claims 1 to 8, characterized in that, the gaseous mixture to be treated containing water and / or C 5 and higher hydrocarbons, said gaseous mixture is subjected to a pretreatment consisting of distillation (2) carried out at a temperature at least equal to that prevailing in the washing zone (5) and, optionally, in the presence of solvent, taken from the solvent brought to the washing zone (5), to produce a fraction ( 4) so-called heavy hydrocarbons containing almost all of the C 6 and higher hydrocarbons and optionally all or part of the C 6 hydrocarbons, a pretreated gas mixture (3) having a C 6 hydrocarbon content and greater than 0.1% by weight and, optionally, a liquid (54) consisting of a mixture of solvent and water.
EP93107550A 1988-11-15 1989-11-14 Process for the simultaneous elimination of CO2 and gasoline from a gaseous hydrocarbon mixture comprising methane, C2 and higher hydrocarbons and also CO2 Expired - Lifetime EP0556875B1 (en)

Applications Claiming Priority (3)

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FR8814784 1988-11-15
FR888814784A FR2641542B1 (en) 1988-11-15 1988-11-15 PROCESS FOR SIMULTANEOUS DECARBONATION AND DEGAZOLINATION OF A GASEOUS MIXTURE MAINLY CONSISTING OF METHANE AND HYDROCARBONS OF C2 AND MORE AND INCLUDING CO2
EP89403123A EP0373983B1 (en) 1988-11-15 1989-11-14 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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JP5383338B2 (en) 2009-06-17 2014-01-08 三菱重工業株式会社 CO2 recovery device and CO2 recovery method
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BR8907193A (en) 1991-03-05
EP0556875A3 (en) 1993-11-10
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WO1990005766A1 (en) 1990-05-31
EP0556875B1 (en) 1995-07-12
FR2641542A1 (en) 1990-07-13
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US5298156A (en) 1994-03-29
NO180687B (en) 1997-02-17
ATE124987T1 (en) 1995-07-15
AU627250B2 (en) 1992-08-20
JP2742328B2 (en) 1998-04-22
NO180687C (en) 1997-05-28
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UA26318A (en) 1999-08-30

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