Institut Francais Du Pe'trole

Gaz De France

Institute Francais Du Petrole

Christian R Busson

Jacques Alagy

Paul Broutin

Jerome Weill

Maurice Cessou

Jean-Pierre Burzynski

Pierre Galtier

Henri Delhomme

Luc Nougier

Eric Lenglet

Jean-Paul Euzen

Pierrr Marache

Christian Dubois

Jean-Charles Viltard

Fabrice Lecomte

Claude Dezael

Bernard A Juguin

Joseph Y Larue

Yves Jacquin

Christian Streicher

Lionel Asselineau

Jean-Claude P Collin

Pierre Giuliani

Yves Gougne

Jean-Claude Mileo

Michel Cohen

Jean Luc Le Peutrec

Jean-Francois Josserand

Pierre Chaverot

Michel Fouquet

Antoine Montoya

Laure Gollion

Jean Pierre Cassagne

Christophe Berat

Thomas Nietsch

Device for connecting a pipe that is intended for heating/or cooling a pressurized reactor and said reactor

Process and furnace for steam-cracking a feedstock that contains ethane and/or propane

A process for producing methylacetylene and propadiene in a reaction zone which is elongate in one direction (one axis) comprises a heating zone and a cooling zone following said heating zone, in which a gas mixture comprising at least one hydrocarbon containing at least three carbon atoms e.g. propane and/or propylene from stream cracking, and at least one diluent is circulated in the heating zone, under super-atmospheric pressure, in a flow direction substantially parallel to the direction (to the axis) of the heating zone, wherein the heating zone comprises at least one preheating zone in which the temperature of said gas mixture increases by about 50&deg; C. to 120&deg; C. per {fraction (1/10)} of the length of the heating zone, at least one pyrolysis zone for the feed in which the temperature rises by about 20&deg; C. to 50&deg; C. per {fraction (1/10)} of the length of the heating zone and at least one methylacetylene-propadiene formation zone in which the temperature climbs by about 70&deg; C. to 150&deg; C. per {fraction (1/10)} of the length of the heating zone, the products formed at the end of the heating zone being cooled in the cooling zone then recovered at the of the reaction zone.

Process for the production of methylacetylene and propadiene

A continuous pyrolysis and decoking process and apparatus is described for the production of acetylenic compounds, in which hydrocarbons and steam are circulated in at least one tube (,) of a steam cracking reactor (,) and steam is circulated in at least one tube (,) of that reactor. The hydrocarbon effluent and steam then circulate in at least one row (,) of a pyrolysis reactor (,) and the decoking effluent comprising steam circulate in at least one other row (,) of that reactor (,) to effect decoking. A set of valves V,V,V,V,is used to alternate the pyrolysis step path and the decoking step path. The temperature in the steam cracking furnaces is lower than that in the pyrolysis reactor.

Process and apparatus for thermal conversion of hydrocarbons to aliphatic hydrocarbons which are more unsaturated than the starting products, combining a steam cracking step and a pyrolysis step

A process for thermal pyrolysis of a feedstock containing at least 80% ethane to convert to ethylene at a conversion rate of at least equal 80% by feeding the feedstock into a reaction zone in which heating means are arranged approximately perpendicular to the direction of flow of the feedstock. The temperature of the outlet of the heating zone in the reaction zone is between 880 and 960&deg; C. and the dwell time of the feedstock in the heating zone is between 1005 and 3000 milliseconds.

Process for thermal pyrolysis of a feedstock that contains ethane

Described in a process for hydrotreating (HDT) a petroleum feedstock (1) that contains sulfur and nitrogen are the catalytic cracking of the ammonia, produced by the hydrotreating process, in a catalytic cracking furnace (F), the cooling (E2) and separating of the cracking effluent to produce an H.sub.2 S containing gas phase, the extraction of the hydrogen sulfide from said gas phase and from the hydrotreating purge gas in an amine washing unit (20), and the separation (SM) of the hydrogen from the resultant effluent. The recovered hydrogen is recycled to hydrotreating unit (HDT) via a pipe (17).

Process and unit for hydrotreating a petroleum feedstock that comprises

A process for the pyrolysis of hydrocarbons in a reactor with at least two rows which are parallel to each other in which at least one row is supplied with a non hydrocarbon fluid containing steam to decoke the reaction zone at least in part. At least one other row is supplied with a gaseous mixture containing at least one hydrocarbon and water, to pyrolyze said mixture.

Continuous pyrolysis and decoking process for use in the production of

A continuous pyrolysis and decoking process and apparatus is described for the production of acetylenic compounds, in which hydrocarbons and steam are circulated in at least one tube (31) of a steam cracking reactor (30) and steam is circulated in at least one tube (32) of that reactor. The hydrocarbon effluent and steam then circulate in at least one row (1) of a pyrolysis reactor (40) and the decoking effluent comprising steam circulate in at least one other row (2) of that reactor (4) to effect decoking. A set of valves V1, V2, V11, V12 is used to alternate the pyrolysis step path and the decoking step path. The temperature in the steam cracking furnaces is lower than that in the pyrolysis reactor.

Process for thermal conversion of hydrocarbons to aliphatic hydrocarbons

A process is described for the catalytic cracking of ammonia present in a fluid containing hydrogen sulphide, in which the fluid is introduced into a reactor comprising a suitable catalyst and a catalytic cracking effluent is recovered. The temperature in the reaction zone is 1000.degree. C. to 1400.degree. C. and a reactor for carrying out the process comprises at least one heating chamber (3, 4) and at least one catalysis chamber (11) in which the ammonia is cracked without cracking the hydrogen sulphide. In a further variation, the reactor comprises at least one catalyst in the spaces defined between the heating elements.

Process for cracking ammonia present in a gas containing hydrogen

A process for the extraction of hydrogen sulphide from a gas mixture comprises: a step (a) in which the gas mixture is passed into an aqueous acidic solution of copper sulphate under conditions which lead to the formation of copper sulphide; a gas which is highly depleted in hydrogen sulphide and an aqueous phase containing copper sulphide in suspension are recovered; a step (b) in which the copper sulphide contained in suspension in the aqueous phase from step (a) is oxidised using an oxygen-containing gas under conditions which lead to the formation of solid elemental sulphur and soluble copper sulphate from this liquid phase; and a step (c) in which the solid sulphur and the solid copper sulphide which is not transformed during step (b) are separated and at least a portion of the aqueous acidic phase containing the copper sulphate formed during step (b) is optionally recycled to step (a). The process is used to absorb hydrogen sulphide contained in a variety of industrial gases.

Process for the extraction of hydrogen sulphide from a gas mixture

The invention relates to an apparatus comprising a reactor, elongated along one axis, preferably of square or rectangular cross section. The reactor has, at one extremity, at least one supply line for at least one reactant and at least one evacuation outlet at the other extremity for removal of produced effluents. In a first zone (near the first extremity of the reactor), a plurality of heat exchangers, substantially parallel to each other, are disposed in substantially parallel layers perpendicular to the reactor axis, thereby defining spaces or passages for circulation of reactant(s) and/or effluents between the heat exchangers and/or layers formed by the heat exchanger. The heat exchangers are adapted to exchange heat in the passages through successive transverse sections, which are independent and substantially perpendicular to the reactor axis. At least some of the heat exchangers comprise a tubular element formed by at least one shell, supplied with a heat exchange gas or gas mixture, and at least one evacuation element for evacuating the circulating gas or gas mixture which has undergone heat exchange with the reactant(s) and/or effluents.

Apparatus for carrying out chemical reactions requiring addition of heat

A process for the thermal pyrolysis of hydrocarbons in a reactor (1) of elongate shape comprising at a first end supply means (5) for a gaseous mixture containing at least one hydrocarbon, at the opposite end discharge means (10) for the effluents produced and between these two ends supply means (9) for effluent cooling fluid, the reactor comprising in a first part (first end side) a plurality of electric heating means (3) enclosed by casings (4) disposed in substantially mutually parallel layers perpendicular to the axis of the reactor, in such a way as to define between the casings and/or the casings and the walls (22), spaces or passages for circulation of the gaseous mixtures and/or effluents. The heating means heat the passages in successive, individual, transverse sections which are substantially perpendicular to the axis of the reactor. The reactor comprises means for introducing into the casings (4) a gas G known as a casing gas which preferably contains water vapour and/or hydrogen. The permeability of the casings is sufficient to permit diffusion, at least at certain points, of at least a part of the gas G from inside the casings to the outside of the casings, the gas G then being diluted in the gaseous mixture.

Process for the thermal pyrolysis of hydrocarbons using an electric

Apparatus suitable for the thermal conversion of methane to hydrocarbons of higher molecular weight, comprising an elongated reactor 1 provided with an inlet 5 for supplying a gas mixture containing methane (process gas) and an outlet at the opposite end, the reactor over a first part towards the inlet end having a plurality of electric heaters 3 surrounded by sheaths 4. The heaters, e.g., electric resistors, which are spaced apart and are substantially parallel with respect to one another, are arranged in substantially parallel rows perpendicular to the axis of the reactor so as to permit circulation of the process gas and/or effluent between the sheaths and/or between the sheaths and walls 22 separating two consecutive rows. The heaters heat the passages by successive independent cross sections substantially perpendicular to the axis of the reaction. Towards the outlet end, the reactor further comprises an injector for supplying cooling fluid, which cools the effluent. The reactor also has a hydrogen inlet for introducing a gas containing hydrogen into the space surrounding the heaters inside the sheaths 4 at an appropriate pressure. The reactor and the sheaths 4 are designed so that hydrogen is diffused from inside the sheaths to outside them and can then be diluted in the process gas.

Apparatus for the thermal conversion of methane

Use of nickel-based alloys in a process for the thermal cracking of a

For preparing at least one boric oxide in an anhydrous or hydrated form and of general formula B.sub.2 O.sub.3, xH.sub.2 O, in which x is a number from 0 to 3, a methyl borate hydrolyzate comprising boric oxide and methanol is introduced into a distillation column is introduced the product from, at least one compound (preferably a hydrocarbon such as, e.g., 2,3-dimethyl butane or 2-methyl pentane) forming a heteroazeotrope with methanol, said heteroazaeotrope having a boiling point below that of the azeotrope formed by methyl borate with methanol and at least one compound having a boiling point higher than that of methyl borate, said compound not forming an azeotrope with a boiling point below that of said heteroazeotrope and then at the head of the column said heteroazeotrope is recovered and at the bottom of the column a suspension containing at least one boric oxide. A description is also given of a process for the oxidation of at least one saturated hydrocarbon into a product incorporating the corresponding alcohol wherein oxidation is carried out with oxygen in the presence of a boric oxide with. The oxidation product is hydrolyzed into orthoboric acid and alcohol, which is recovered by separation from the organic phase. The aqueous phase containing the boric acid is fed into a methyl borate formation zone and the methyl borate is recovered in the form of its azeotrope with methanol. The recovery of the boric oxide from said azeotrope is performed in accordance with the aforementioned process, the recovered boric oxide being recycled to the oxidation stage.

Process for the preparation of boric oxide by hydrolysis of methyl

Growing community of inventors

Dardilly, France

Christian R Busson