Institut Francais Du Pe'trole

Other

Procedes Petroliers Et Petrochimiques

Gaz De France

Institute Francais Du Petrole

Institut Francais Du Petrole Procedes Petroliers Et Petrochimques Eric

Jean-Pierre Burzynski

Eric Lenglet

Roland Huin

Christine Travers

Ari Minkkinen

Christian R Busson

Paul Broutin

Jean De Bonneville

Yves Gougne

Herve Cazor

Germain J Martino

Yvon Castel

Fabienne Le Peltier

Joseph Y Larue

Jean-Paul Boitiaux

Gerard Leger

John Lynch

Christian Dubois

G&eacute;rard Courteheuse

Pierrr Marache

Pierre Renard

Sigismond Franckowiak

Quang Dang Vu

Henri Delhomme

Alain Grehier

Larry Mank

Luc Nougier

Didier Duee

Gerard Courteheuse

Jean-Claude Simandoux

Philippe Vacher

Albert Chaillard

Blaise Didillion

A steam-cracking unit comprises at least one multitube quenching exchanger, equipped with a non-obstructive impact separator for preventing the erosion of the tubular input plate. The impact separator is at least 50% opaque when viewed from transfer pipe. It is arranged inside of an input cone in such a way that there is free passage of at least 40 mm between the periphery of the impact separator and the cone.

Steam cracking installation with means for protection against erosion

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

A steam-cracking process includes the injection, at at least one point upstream from a secondary quenching indirect exchanger (,), of particles with a mean size of between 0.02 and 4 mm, at a velocity speed in the exchanger of 20 to 180 m/s, in sufficient quantity to limit the rise in the output temperature of the effluents from the exchanger to a value that is less than 100&deg; C. per month. At least 70% by weight of the quantity of injected particles is introduced downstream from primary quenching exchangers (,) and upstream from the inlet to the secondary quenching exchanger. At intervals, decoking of the pyrolysis pipes and primary quenching exchangers is carried out in the presence of air.

Method and device for steam cracking comprising the injection of particles upstream of a secondary quenching exchanger

Steam cracking installation and method with single controlled injection

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

Flexible steam cracking process and corresponding steam cracking facility

Steam cracking method and plant using controlled injection of solid

A process for the regeneration of a sulfur containing catalysts, wherein the catalyst is stripped of sulfur before the oxychlorination treatment of the regeneration process, typically before the catalyst is sent to the regeneration zone. The process is particularly useful for catalyst employed in hydrocarbon conversions such as dehydrogenation reactions, particularly those which comprise the injection of sulfur and/or at least one sulfur compound before or simultaneously to the introduction of the charge into the first reaction zone.

Process for the regeneration of catalyst containing sulphur

The present invention concerns, in the dehydroisomerization of at least one C.sub.4 -C.sub.5 n-paraffin, preferably n-butane, the use of a catalyst comprising a refractory oxide based support, preferably an alumina, at least one precious metal from group VIII, preferably platinum or palladium, optionally at least one element from group IVB such as titanium or zirconium, preferably titanium, optionally at least one element from the group formed by germanium, tin, lead, rhenium, tungsten and indium, and optionally at least one halogen such as chlorine. The present invention also concerns the regeneration of this catalyst.

Catalytic dehydroisomerization of C.sub.4 -C.sub.5 n-paraffins

Steam cracking process and facility comprising injection of powder which

A device for the catalytic dehydrogenation of a C.sub.2+ paraffinic hydrocarbon charge is applicable to the synthesis of methyl tert-butyl ether. Effluent coming from the dehydrogenation reactor and containing olefins and water is cooled in at least one heat exchanger (41), saturated with water in a column (3) and sent to a stripping column (10) where it is at least partly put in contact with a recycled aqueous liquid phase containing a solvent, preferably methanol. The compressed gaseous effluent in which the water is thereby inhibited from freezing by the methanol is cooled in a heat exchanger (13) then separated in separator (8) into olefins and into hydrogen. An aqueous liquid phase with methanol is decanted at (8) and recycled in column (10).

Device for catalytic dehydrogenation of a C.sub.2+ paraffinic charge

A device for catalytic dehydrogenation of a C.sub.2+ paraffinic cut with an improved system for cooling the effluent is applicable, for example, to the synthesis of methyl tert-butyl ether. Liquid charge 12 is evaporated in the calandria of a heat exchanger 13 in the optional presence of at least one part recycled hydrogen 15, then optionally compressed in a compressor 14 before being pre-heated in an exchanger 41 by effluent 1 and introduced into a dehydrogenation reactor 40. The effluent cooled in the tubes of exchanger 13 can be mixed with a cryogenic phase 17 resulting from the isentropic expansion of a hydrogen-rich phase separated in a separator 8, the hydrogen optionally being recycled to the calandria of the heat exchanger. The olefins recovered with the unconverted paraffins are stabilized in a column 20.

Device for catalytic dehydrogenation A C.sub.2+ paraffinic charge

Continuous process for the skeletal isomerization of n-olefins containing at the most 20 carbon atoms, in the presence of a catalyst essentially constituted by alumina and titanium, in which a charge containing the said n-olefins is made to flow through at least one fluidized bed reaction zone, the catalyst flowing into each reaction zone. The catalyst drawn off from the final reaction zone is passed into a regeneration zone, at the outlet of which it is passed into a zone where it undergoes a steam treatment prior to its reintroduction into the first reaction zone. The process is performed in the presence of steam, so that the catalyst is in contact with 3 to 85 wt. % (based on the catalyst weight) of steam. The water/olefin charge molar ratio in the reaction zone is between 0.1 and 3.

Continuous process for the isomerization of olefins with regeneration of

Olefin isomerisation process

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Sainte Foy Les Lyon, France

Jean-Pierre Burzynski