Abstract: The mercaptan-laden natural gas is contacted with a mercaptan-adsorbing sieve T1. The mercaptan-rich gaseous effluent obtained upon regeneration of sieve T2 is then contacted with an olefin-containing liquid feed in the presence of an acid catalyst. Under suitable conditions, the mercaptans are absorbed in the liquid feed and they react with the olefins so as to form solvent-soluble sulfides. A solvent regeneration stage allows the capture agent to be recycled.

Abstract: The method enables the antihydrate compounds contained in a condensed-hydrocarbon liquid feedstock arriving through pipe 1 to be extracted. The liquid feedstock is brought into contact, in zone ZA, with a non-aqueous ionic liquid having the general formula Q+ A31 , where Q+ designates an ammonium, phosphonium, and/or sulfonium cation, and A31 designates an anion able to form a liquid salt. The antihydrate compounds in the liquid hydrocarbon feedstock evacuated through pipe 2 are eliminated. The ionic liquid charged with antihydrate compounds is evacuated through pipe 3, then introduced into evaporator DE to be heated in order to evaporate the antihydrate compounds. The regenerated ionic liquid is recycled through pipes 8 and 9 to zone ZA. The antihydrates are evacuated through pipe 7a.

Abstract: The natural gas arriving through pipe 1 is deacidified by being brought into contact with a solvent in column C2. The solvent charged with acid compounds is regenerated in zone R. The purified gas evacuated by pipe 9 includes some of the solvent. The method enables the solvent contained in the purified gas to be extracted. In zone ZA, the purified gas is brought into contact with a non-aqueous ionic liquid whose general formula is Q+ A?, where Q+ designates an ammonium, phosphonium, and/or sulfonium cation, and A? designates an anion able to form a liquid salt. The solvent-impoverished purified gas is evacuated through pipe 17. The ionic liquid charged with solvent is regenerated by heating in an evaporator DE. The solvents separated from the ionic liquid in evaporator DE are recycled.

Abstract: The combustion fume flowing in through line 1 is decarbonated by contacting with a solvent in column C2. The solvent laden with carbon dioxide is regenerated in zone R. The purified fume discharged through line 9 comprises part of the solvent. The method allows to extract the solvent contained in the purified fume. The purified fume is contacted in zone ZA with a non-aqueous ionic liquid of general formula Q+ A?; Q+ designates an ammonium, phosphonium and/or sulfonium cation, and A? an anion likely to form a liquid salt. The solvent-depleted purified fume is discharged through line 17. The solvent-laden ionic liquid is regenerated by heating in evaporation device DE. The solvent separated from the ionic liquid in device DE is recycled.

Abstract: The natural gas arriving through pipe 1 is deacidified by being brought into contact with a solvent in zone C. The solvent charged with acid compounds is regenerated in zone R. The acid gases, released into pipe 5 upon regeneration, include a quantity of solvent. The method enables the solvent contained in the acid gases to be extracted. In zone ZA, the acid gases are brought into contact with a non-aqueous ionic liquid whose general formula is Q+ A?, where Q+ designates an ammonium, phosphonium, and/or sulfonium cation, and A? designates an anion able to form a liquid salt. The solvent is removed from the acid gases evacuated through pipe 6. The ionic liquid charged with solvent is regenerated by heating in an evaporator DE. The ionic liquid regenerated is recycled through pipes 8 and 9 to zone ZA. The solvent is evacuated through pipe 13.

Abstract: The raw natural gas is deacidized and dehydrated in units DA and DH. The treated gas is then purified by adsorption of the mercaptans in first enclosure A1. Part of the purified gas is heated in E1, then fed into second enclosure A2 so as to discharge the water adsorbed by the adsorbent material contained in this second enclosure. A steam-rich stream is fed into third enclosure A3 containing a mercaptan-laden adsorbent material. In A3, the mercaptans are desorbed and replaced by the steam.

Abstract: The raw natural gas is deacidized and dehydrated in units DA and DH. The treated gas is then purified by adsorption of the mercaptans in first enclosure A1. Part of the purified gas is heated in E1, then fed into second enclosure A2 so as to discharge the water adsorbed by the adsorbent material contained in this second enclosure. A water-laden purge gas is fed into third enclosure A3 containing a mercaptan-laden adsorbent material. In A3, the mercaptans are desorbed and replaced by the water. The gas from the third enclosure is washed in unit L, then recycled.

Abstract: The gas to be processed, flowing in through line 10, contains impurities. This gas is contacted in column C1 with a solvent flowing in through line 18. The scrubbed gas is discharged through line 19. The impurity-laden solvent recovered through line 12 is regenerated by expansion, then by distillation in column C2. The invention proposes carrying out expansion by means of two-phase turbines T1 and T2.

Abstract: The mercaptan-laden natural gas is contacted with a mercaptan-adsorbing sieve T1. The mercaptan-rich gaseous effluent obtained upon regeneration of sieve T2 is then contacted with an olefin-containing liquid feed in the presence of an acid catalyst. Under suitable conditions, the mercaptans are absorbed in the liquid feed and they react with the olefins so as to form solvent-soluble sulfides. A solvent regeneration stage allows the capture agent to be recycled.

Abstract: The invention relates to a method of pretreating a natural gas, water-saturated or not, essentially comprising hydrocarbons, a substantial amount of hydrogen sulfide and possibly carbon dioxide. The method according to the invention comprises an H2S-rich stream recycling stage.

Abstract: Method of regenerating a glycol solution containing water, hydrocarbons and salts. The glycol solution is expanded in drum (2), then distilled in column (7). The concentrated glycol collected at the level of reboiler (8) is placed under vacuum to vaporize the water and to precipitate the salts. The salts are separated from the glycol in separation device (13). The concentrated glycol freed of the salts is stored in capacity (16).

Abstract: The raw natural gas is pretreated in treating unit 30. The treated gas is then purified by adsorption of the mercaptans in first enclosure 31. The various cuts that make up the purified gas are separated in fractionating unit 34. Part of the methane making up the purified gas is saturated with a C5+ hydrocarbon in contactor 33, then it is fed into second enclosure 32 so as to regenerate the adsorbent material contained in this second enclosure. The gas from the second enclosure is washed in unit 35, then recycled.

Abstract: The gaseous feed flowing in through line 1 is contacted in contacting zone ZA with a liquid solvent flowing in through line 2. The solvent comprises between 0.001% and 100% by weight of a liquid olefin. Contacting in zone ZA is carried out in the presence of an acid catalyst. The purified gaseous feed is discharged from zone ZA through line 3. The sulfide-laden solvent is discharged through line 4, then regenerated in unit RE. The regenerated solvent is recycled through lines 7 and 2 to zone ZA.

Abstract: The natural gas is deacidized by contacting in zone 3 with a solvent containing amine in aqueous solution. The gas is then dehydrated by contacting in zone 4 with a solvent very rich in amine. After the contacting operations, the solvent containing H2S. and water is expanded in drum 9, then regenerated in column 11. Part of the regenerated solvent is sent to zone 3. Another part of the regenerated solvent is vacuum distilled in column 18 so as to produce an amine-rich solvent that is sent to zone 4.

Abstract: The method allows pretreatment of an acid gas that can comprise more than 10% H2S, for example a natural gas or a gas associated with the production of a crude petroleum effluent. The gas is dehydrated in unit DH, then cooled by heat exchangers E9 to E12 and by expansion carried out through valve V7. Cooling allows part of the H2S contained in the gas to be condensed. The condensates are separated from the gas in drum B1. The liquid recovered at the bottom of drum B1 is pumped and injected into well P to be sequestered in an underground reservoir or a geologic structure. The gas discharged at the top of drum B1 is depleted in H2S. This gas is sent through line 43 to a treating site in order to be subjected to additional treatments prior to being used.

Abstract: The invention relates to a method for treating a natural gas, saturated or not with water, containing essentially hydrocarbons, a substantial amount of hydrogen sulfide and possibly carbon dioxide. The method of the invention comprises a condensation stage intended to condense a major part of the water, a distillation stage wherein a gaseous effluent depleted in hydrogen sulfide and substantially free of water is recovered, and a contacting stage wherein the gaseous effluent from the previous stage is contacted with a solvent so as to obtain a treated gas substantially free of hydrogen sulfide and possibly of carbon dioxide.

Abstract: The raw natural gas is deacidized and dehydrated in units DA and DH. The treated gas is then purified by adsorption of the mercaptans in first enclosure A1. Part of the purified gas is heated in E1, then fed into second enclosure A2 so as to discharge the water adsorbed by the adsorbent material contained in this second enclosure. A steam-rich stream is fed into third enclosure A3 containing a mercaptan-laden adsorbent material. In A3, the mercaptans are desorbed and replaced by the steam.

Abstract: The combustion fume flowing in through line 1 is decarbonated by contacting with a solvent in column C2. The solvent laden with carbon dioxide is regenerated in zone R. The purified fume discharged through line 9 comprises part of the solvent. The method allows to extract the solvent contained in the purified fume. The purified fume is contacted in zone ZA with a non-aqueous ionic liquid of general formula Q+ A?; Q+ designates an ammonium, phosphonium and/or sulfonium cation, and A? an anion likely to form a liquid salt. The solvent-depleted purified fume is discharged through line 17. The solvent-laden ionic liquid is regenerated by heating in evaporation device DE. The solvent separated from the ionic liquid in device DE is recycled.

Abstract: The natural gas is successively contacted in column CA with a relatively methanol-rich solvent flowing in through line 4, then with a relatively poor solvent flowing in through line 9. The acid gas-containing solvent recovered through line 3 at the bottom of column CA is expanded through valves V1 and V2 to release acid gases through line 6. A fraction of the expanded solvent is distilled in column CR. The regenerated solvent obtained at the bottom of column CR is sent to the top of column CA through line 9. A second fraction of the expanded solvent is mixed with a solvent drawn off from column CR at an intermediate point between the bottom and the top of this column. This mixture of solvents is sent through line 4 into column CA.

Abstract: The gaseous feed flowing in through line 1 is contacted in contacting zone ZA with a liquid solvent flowing in through line 2. The solvent comprises between 0.001% and 100% by weight of a liquid olefin. Contacting in zone ZA is carried out in the presence of an acid catalyst. The purified gaseous feed is discharged from zone ZA through line 3. The sulfide-laden solvent is discharged through line 4, then regenerated in unit RE. The regenerated solvent is recycled through lines 7 and 2 to zone ZA.