Abstract: A cogeneration method and device by turbine, particularly by gas turbine, uses a compression section, at least one expansion section, and a combustion chamber. A combustion agent including oxygen is compressed in the compression section; in the combustion chamber, one combustion step is carried out under pressure with a mixture of combustion agent compressed with a fuel; at least some of the hot gases obtained by pressurized combustion are used to effect an exchange with an external facility; and at least one postcombustion step is carried out of a mixture of hot gases coming from combustion with a fuel, prior to the exchange, and at least one other postcombustion step of a mixture of hot gases, coming from the exchange, with a fuel, in order to obtain hot gases that are sent to the expansion section.

Abstract: The invention relates to a plant for regasification of liquefied natural gas (GNL), comprising a liquefied gas storage reservoir (10) and a regasification device (12) for the GNL through which the natural gas and a heat transfer medium flow. According to the invention, the plant comprises a loop circuit (16) in which the heat transfer medium circulates in the form of a low-viscosity organic liquid with a low crystallisation point and the regasification device (12) comprises at least two exchangers (60, 62).

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 present invention relates to a cogeneration method and device by turbine, particularly by gas turbine, having a compression section (14), at least one expansion section (18, 52, 96), and a combustion chamber (20). According to the method of the invention, a combustion agent including oxygen is compressed in the compression section (14); in the combustion chamber (20), one combustion step is carried out. under pressure, of a mixture of combustion agent compressed with a fuel; at least some of the hot gases obtained by pressurized combustion are used to effect an exchange with an external facility (34, 70); and at least one postcombustion step is carried out of a mixture of hot gases, coming from the exchange, with a fuel, in order to obtain hot gases that are sent to the expansion section (18, 52, 96), under temperature and pressure conditions close to the conditions prevailing in the absence of an exchange.

Abstract: The invention relates to a process for converting a synthesis gas into liquid hydrocarbons used in at least two reactors that are arranged in series and that contain a catalytic suspension of at least one solid catalyst in suspension in a liquid phase, in which said reactors are essentially perfectly mixed, the last reactor is at least in part fed by at least a portion of at least one of the gaseous fractions that are collected at the outlet of at least one of the other reactors, at least one reactor is fed by a flow of catalytic suspension that is obtained directly from another reactor, and at least one flow of catalytic suspension that is obtained from a reactor is at least in part separated so as to obtain a liquid product that is essentially free of catalyst and a catalytic suspension that is high in catalyst, which is recycled.

Abstract: Process for synthesis of hydrocarbons by Fischer-Tropsch reaction starting from synthesis gas, operating in three-phase fluidization, the reactor having an exchanger immersed within the fluidized bed and using as coolant a fluid introduced at its boiling point at a pressure slightly greater than the pressure of the process, this boiling point being from 10 to 70° C. below the temperature of the process.

Abstract: Installation for the production of synthesis gas from a hydrocarbon feedstock comprising at least one reactor for steam reforming, at least one reactor for converting CO2 that is equipped with at least one feed means by the effluent that is obtained from the steam reforming and at least one other feed means by a gas comprising carbon dioxide, characterized in that at least one reactor for steam reforming or for converting CO2 is heated by a hot gas.

Abstract: Process for synthesis of hydrocarbons by Fischer-Tropsch reaction starting from synthesis gas, operating in three-phase fluidization, the reactor having an exchanger immersed within the fluidized bed and using as coolant a fluid introduced at its boiling point at a pressure slightly greater than the pressure of the process, this boiling point being from 10 to 70° C. below the temperature of the process.

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 invention relates to a process for converting a synthesis gas into liquid hydrocarbons used in at least two reactors that are arranged in series and that contain a catalytic suspension of at least one solid catalyst in suspension in a liquid phase, in which said reactors are essentially perfectly mixed, the last reactor is at least in part fed by at least a portion of at least one of the gaseous fractions that are collected at the outlet of at least one of the other reactors, at least one reactor is fed by a flow of catalytic suspension that is obtained directly from another reactor, and at least one flow of catalytic suspension that is obtained from a reactor is at least in part separated so as to obtain a liquid product that is essentially free of catalyst and a catalytic suspension that is high in catalyst, which is recycled.

Abstract: A process for eliminating oxygen (O2) from a gas that contains nitrogen and carbon dioxide (CO2) is described in which combustion of the gas with a hydrocarbon stream is carried out in at least one catalytic combustion zone (5); at the end of the combustion zone, combustion effluents (line 9) that essentially no longer contain O2, a major portion of CO2, and water, are recovered; said combustion effluents are cooled in at least one heat-exchange zone (10) (4) (11) (12); and the cooled effluents are condensed in at least one condensation zone (13) from where condensed water (line 14) and a gas effluent (line 15) essentially no longer containing oxygen are extracted.

Abstract: Installation for the production of synthesis gas from a hydrocarbon feedstock comprising at least one reactor for steam reforming, at least one reactor for converting CO2 that is equipped with at least one feed means by the effluent that is obtained from the steam reforming and at least one other feed means by a gas comprising carbon dioxide, characterized in that at least one reactor for steam reforming or for converting CO2 is heated by a hot gas.

Abstract: For the purification of an effluent that contains carbon dioxide and hydrocarbons resulting from a carbon dioxide-assisted recovery stage, the effluent is circulated in a gas-liquid separator (3) to recover C3+ liquid and a gas that contains carbon dioxide and, for example, less than 10% of methane and ethane. Pressurized combustion (13) of the gas with air produced a combustion gas (21) enriched with carbon dioxide and water vapor. The combustion gas (21) is cooled (11) (22) to recover heat, and the cooled combustion gas is recycled under pressure by a compressor (27) to an injection well (29). Nitrogen is at least partly separated from the combustion gas before the recycling, and in an optional intermediate step the condensed water is also separated from the carbon dioxide. The invention has a particular application for the assisted recovery of petroleum by CO2 with a reduction of the greenhouse effect.

Abstract: For the separation of acid, carbon dioxide and/or hydrogen sulfide from a gaseous mixture comprising at least one lighter gas, e.g. methane, the gaseous mixture (1) is precooled at least once during a heat exchange operation E2; the resultant precooled gas mixture, flowing upwardly is cooled and rectified simultaneously in an approximately vertical heat exchange zone (ER) forming a downwardly-flowing countercurrent liquid reflux; the resultant rectified gaseous fraction (8) depleted in acid gases and enriched in light gas is collected at the top of the vertical exchange zone; and (d) a liquid fraction (4) enriched in acid gas components is collected at the bottom of the exchange zone. The collected liquid fraction (4) can be expanded and evaporated to provide cooling. The system has particular application for the treatment of natural gas or in petroleum refining or recovery operations.

Abstract: A process for the production of paraxilene comprises an adsorption stage (18) using toluene as a desorbent in a simulated moving bed of a feedstock previously depleted in ethylbenzene by distillation (3) or by adsortion, an isomerization stage (26) without hydrogen in liquid phase diluted with toluene from the raffinate produced, a distillation stage (27) of the raffinate that is isomerized to recover the toluene (29) that is recycled. The separated isomerate is introduced into a xylene distillation column (9). The separated ethylbenzene is isomerized separately in gas phase with hydrogen at higher temperature and is distilled (5, 2, 9) in the presence of a catalyst that comprises an EUO-structural-type zeolite, then recycled to adsorption stage (18).

Abstract: For the separation of acid, carbon dioxide and/or hydrogen sulfide from a gaseous mixture comprising at least one lighter gas, e.g. methane, the gaseous mixture (1) is precooled at least once during a heat exchange operation E2; the resultant precooled gas mixture, flowing upwardly is cooled and rectified simultaneously in an approximately vertical heat exchange zone (ER) forming a downwardly-flowing countercurrent liquid reflux; the resultant rectified gaseous fraction (8) depleted in acid gases and enriched in light gas is collected at the top of the vertical exchange zone; and (d) a liquid fraction (4) enriched in acid gas components is collected at the bottom of the exchange zone. The collected liquid fraction (4) can be expanded and evaporated to provide cooling. The system has particular application for the treatment of natural gas or in petroleum refining or recovery operations.

Abstract: A process for the production of paraxylene is described that comprises an adsorption stage (18) that uses toluene as a desorbent in a simulated moving bed of a feedstock whose ethylbenzene was separated by distillation (line 3) or by adsorption, an isomerization stage (26) without hydrogen in liquid phase that is diluted with toluene from the raffinate produced, a distillation stage (27) of the raffinate that is isomerized to recover the toluene (line 29) that is recycled. The separated isomerate is introduced into a xylene distillation column (9) then recycled, in adsorption. The separated ethylbenzene is isomerized separately in gas phase with hydrogen at higher temperature and is distilled (5, 2, 9) in the presence of a catalyst that comprises an EUO-structural-type zeolite, then recycled in adsorption column (18). The pure paraxylene is collected as extract (line 22) then optionally purified by crystallization (17).

Abstract: A process for purification of an effluent that contains carbon dioxide and hydrocarbons that are produced by carbon dioxide-assisted recovery is described in which the effluent is circulated in a gas-liquid separator (3) to recover a gas that contains carbon dioxide and, for example, less than 10% of methane and ethane, and pressurized combustion (13) is produced to recover an effluent (21) that is enriched with carbon dioxide and water vapor. Effluent (21) is cooled (11) (22) to recover the heat, and the effluent that is cooled in an injection well (29) by a compressor (27) is recycled under pressure. It is possible to separate (24) the condensed water from carbon dioxide.

Abstract: A process and a device for separating ethane and ethylene from a hydrocarbon steam-cracking effluent is described. Effluent (1) is absorbed in an absorption column (7) by a cooled solvent (9). At the bottom of the column, liquid phase (12) that contains the solvent and the C2+ hydrocarbons is recovered and hydrogenated (15). The hydrogenation effluent that contains the solvent is introduced into a first distillation column (70) where the solvent is regenerated. The solvent is cooled and recycled at the top of absorption column (7). The C2+ hydrocarbons are collected at the top, and a condensed liquid phase is distilled in a second distillation column (77) to recover a C2 fraction that consists of ethane and ethylene.

Abstract: A process for separating ethane and ethylene from a hydrocarbon steam-cracking effluent is described. Effluent (1) is absorbed in an absorption column by a cooled solvent (9). At the bottom of the column, the liquid phase that contains the solvent and the C2+ hydrocarbons is recovered and hydrogenated (15). The hydrogenation effluent that contains the solvent is introduced into a first distillation column (16). Ethane-ethylene mixture (17) is drawn off laterally from the column, and a phase (19) that contains the solvent and hydrocarbons with at least 3 carbon atoms is drawn off at the bottom of the column. This phase (19) is separated in a second distillation column (22), and C3+ hydrocarbons and, at the bottom of the column, regenerated solvent (26) that is cooled and that is recycled (9, 52) in the absorption column are collected.