Institut Francais Du Pe'trole

Institute Francais Du Petrole

Agip Petroli

Institut Fracnais Du Petrole

Ari Minkkinen

Alexandre Rojey

Joseph Y Larue

Jean-Pierre Burzynski

Paul Mikitenko

Reynald Bonneau

Etienne Lebas

Larry Mank

Pierre Marache

Jean-Herv&eacute; Le Gal

Pierre Renard

Fabio Alario

Fabrice Lecomte

Andre Deschamps

Julia Magne-Drisch

Gerard Martin

Elisabeth Merlen

Gerard Leger

Jean-Fran&ccedil;ois Joly

Lionel Asselineau

Jean-Marc Schweitzer

Sophie Jullian

Didier Duee

B&eacute;atrice Fischer

Eric Marty

Pierre Capron

Daniel Benayoun

Yves Barthel

Philippe Vacher

Jean-Paul Cariou

Jean-Piere Burzynski

Jean Claude Collin

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.

Cogeneration method and device using a gas turbine comprising a post-combustion chamber

The natural gas is deacidized by contacting in zonewith a solvent containing amine in aqueous solution. The gas is then dehydrated by contacting in zonewith a solvent very rich in amine. After the contacting operations, the solvent containing HS. and water is expanded in drum, then regenerated in column. Part of the regenerated solvent is sent to zone. Another part of the regenerated solvent is vacuum distilled in columnso as to produce an amine-rich solvent that is sent to zone

Natural gas deacidizing and dehydration method

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.

Process for converting synthesis gas in reactors that are arranged in series

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&#xb0; C. below the temperature of the process.

High-pressure fischer-tropsch synthesis process using an optimized coolant

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 COthat 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 COis heated by a hot gas.

Installation and process for the production of synthesis gas comprising a reactor for steam reforming and a reactor for converting CO2 heated by a hot gas

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 ( ) to recover C liquid and a gas that contains carbon dioxide and, for example, less than 10% of methane and ethane. Pressurized combustion ( ) of the gas with air produced a combustion gas ( ) enriched with carbon dioxide and water vapor. The combustion gas ( ) is cooled ( ) ( ) to recover heat, and the cooled combustion gas is recycled under pressure by a compressor ( ) to an injection well ( ). 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 CO with a reduction of the greenhouse effect.

Process for purification by combination of an effluent that contains carbon dioxide and hydrocarbons

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

Process for the production of paraxylene that comprises an adsorption stage, a liquid phase isomerization stage and a gas phase isomerization stage with an euo-type zeolite

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 ( ) is precooled at least once during a heat exchange operation E 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 ( ) depleted in acid gases and enriched in light gas is collected at the top of the vertical exchange zone; and (d) a liquid fraction ( ) enriched in acid gas components is collected at the bottom of the exchange zone. The collected liquid fraction ( ) 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.

Process and device for separation of at least one acid gas that is contained in a gas mixture

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

Process for separating ethane and ethylene by solvent absorption and hydrogenation of the solvent phase

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

Process and device for separating ethane and ethylene from a steam-cracking effluent by solvent absorption and hydrogenation of the solvent phase

A device for crystallization of a component from a liquid mixture comprising a chamber, a first conduit connected to said chamber for supplying said mixture, a second conduit connected to and in connection with said chamber for introducing cold gas, a third conduit for withdrawing warmed gas from said crystallizer, a turbo-expander for cooling gas withdrawn from said chamber, and a fourth conduit Icading from the turbo-expander to said chamber. The device has particular application for the crystallization of paraxylene.

Device for crystallization by isentropic expansion and its use

The specification describes a method and a fixed bed apparatus for producing olefinic hydrocarbons from a charge of saturated aliphatic hydrocarbons with 2 to 20 carbon atoms and hydrogen in a chamber,comprising a plurality of parallel tubes,filled with a catalyst and arranged in rows. A so-called reaction phase and a catalyst-regenerating phase are carried out in the tubes of the chamber. The tubes are heated by appropriate radiant heating means,, arranged in layers substantially perpendicular to the tubes. These layers heat a first part of the tubes (at the feed side) with a heat flux greater than the mean heat flux of the chamber and a second, subsequent part with a mean flux no more than equal to the mean heat flux, so that the isothermicity of the catalyst is substantially maintained, using appropriate control means.

Method and apparatus for dehydrogenating aliphatic hydrocarbons to olefinic hydrocarbons

Device and process for crystallizing a component, e.g. paraxylene, from a mixture that comprises a chamber (1) that has in its upper part means (46) for supplying the mixture, collecting means (20), and in its lower part, crystals of the component in suspension in a mother liquor, connected to means (C) for separation and purification of the crystals that are obtained, means (9) for supplying a cold gaseous fluid and means (22) for drawing off the so-called hot gaseous fluid that results from the direct heat exchange, whereby said device also comprises means for shaping a descending flow of the mixture onto tubes such that the cold gaseous fluid that circulates upward exchanges cold directly with the mixture, whereby means (22) for drawing off the hot gaseous fluid are connected to at least one fluid recompression means (24b), whose output is connected to at least one heat exchanger (27), whereby the heat exchanger is connected to a turbo-expander (30), which is connected to means (31) for supplying cold gaseous fluid.

A process for the dehydration, deacidification and stripping of a gas, characterized in that:

Process for the dehydration, deacidification and stripping of a natural

The process comprises a cold absorption step 2 for removing acid gas from natural gas using a solvent phase at a pressure P.sub.2 which delivers a purified gas 5; a step for depressurizing and separating resultant acidic solvent phase containing hydrocarbons (lines 4, 11), at a pressure P.sub.12 which is lower than pressure P.sub.2 in a column-heat exchanger 12 which delivers a purified gaseous effluent 13 overhead and a further solvent phase at the bottom (line 17) which is enriched in hydrogen sulphide; and a solvent phase regeneration step carried out in a distillation column 18 at a pressure P.sub.18 and no higher than pressure P.sub.12. A gas 29 containing essentially hydrogen sulphide which is depleted in hydrocarbons is recovered from column 18 and is a suitable feed for a Claus plant for eliminating H.sub.2 S. The regenerated hot solvent phase 20 indirectly exchanges heat with the cold acidic solvent phase from absorber 2 or separator 6. It is then recycled to the absorbent after cooling.

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Saint Nom la Breteche, France

Ari Minkkinen