Abstract: An entrained bed or fluidised bed process for catalytic cracking of a hydrocarbon feed in two reaction zones is described, one zone (1) being in catalyst dropper mode, the other (2) being in catalyst riser mode. A feed (102) and catalyst from at least one regeneration zone (302) are introduced into the upper portion of the dropper zone, the feed and catalyst are circulated in accordance with a catalyst to feed weight ratio, C/O, of 5 to 20, the cracked gases are separated from the coked catalyst in a first separation zone (105), the cracked gases are recovered (107), the coked catalyst is introduced (110) into the lower portion of the riser zone (2), the coked catalyst and said feed are circulated in a C/O weight ratio of 4 to 8, the used catalyst is separated from the effluent produced in a second separation zone (203), the catalyst is stripped in a stripping zone (212), the effluent and stripping gases are recovered (206) and the used catalyst is recycled (7) to the regeneration zone.

Abstract: In order to recover hydrogen from a hydrogen-rich gaseous effluent, a procedure is used that comprises:

Abstract: Device that is integrated in a chamber that allows a separation of a mixture that comprises at least one gaseous fraction and one liquid fraction, whereby said mixture is obtained from a zone for bringing into contact a liquid phase, a gaseous phase and solid particles.

Abstract: A sub-assembly is described that ensures contact, material distribution and heat and/or material exchange of at least one gas phase, at least a portion of which is hydrogen, and at least one liquid phase, for a vessel containing at least one bed of granular solid, said phases being in overall downflow mode and traversing said bed of granular solid, said sub-assembly comprising at least one distributor tray (P) located above the bed of granular solid, comprising a plurality of downcomers (1) each surmounted by at least one jet disturber device and each having in its upper portion at least one cross section of flow (22) for entry of the major portion of said gas phase into said downcomer and, between said upper portion and the lower portion of said downcomer above tray (P), at least one cross section of flow (2) for entry of the major portion of said liquid phase into said downcomer, and in its lower portion at least one cross section of flow (23) of the mixture formed in the downcomer for distributing it over

Abstract: An apparatus for separating and stripping a mixture of gas and particles comprises an envelope having separation chambers and circulation chambers distributed about a reactor, the upper portion of each separation chamber comprising an inlet opening communicating with the reactor and with a zone for rotating the mixture in a vertical plane. Each separation chamber comprises two lateral walls which are also walls for the circulation chamber, at least one of the walls of each chamber comprising a lateral outlet opening for mixing gas and particles into the adjacent circulation chamber. Each separation chamber also comprises an axial opening for particles to enter a stripping chamber, the envelope further comprises a conduit for evacuating a gas-particle mixture connected to at least one secondary separator and the stripping chamber communicating with the conduit via circulation chambers. Application of this apparatus is to fluidized bed catalytic cracking of hydrocarbons in a riser and/or dropper.

Abstract: A separator and process for separating particles from a gaseous mixture wherein the separator includes: at least one chamber comprising a zone (1) which forms a rectangular or square cross section for passage of the mixture circulating in a tube reactor (R) towards a turning zone (3) which rotates the mixture in a vertical plane through an angle of at most 360 degrees; an external wall (30) which defines the turn through an angle of 70 to 225 degrees; a deflection (10) which turns co-axially with the external wall (30) through an angle of at least 30 degrees and at most the angle through which the external wall turns plus 90 degrees; a gas outlet (4) which is coaxial with the turning zone; the separator is indirectly or otherwise connected to a secondary cyclone (12). It also includes a particle outlet (9) having a wall (32) connected to forming zone (1).

Abstract: A process is described for catalytic cracking of a petroleum feed in which a catalyst from a regeneration zone 4 is caused to flow in a dense fluidized bed conditioning zone 2 upstream of an injection zone 10, the fluidization rate being 0.1 to 30 cm/s. The throughput of catalyst into injection zone 10 is regulated by a constriction means 11. The hydrocarbon feed 12 is injected below the constriction means and flows counter-current to the direction of flow of the shaped catalyst flow. The hydrocarbon feed 12 is injected at a set injection angle depending on the movement of the feed and the catalyst.

Abstract: A hydrocarbon catalytic cracking process in which, a substantial portion of the hydrocarbons is pulverized and placed in contact with a specific contact zone, which is composed of: a mixing chamber having a maximum section S.sub.2, the upper part of which is fed with a heated regenerated catalyst through an upper opening delimiting a catalyst-flow section S.sub.1, and a descending-flow reaction area, in which the solid-gas mixture emanating from the mixing chamber is poured through an intermediate opening having a section S.sub.3 located in the lower part of said chamber. The ratios S.sub.2 /S.sub.1 and S.sub.2 /S.sub.3 have values of between 1.5 and 8.

Abstract: The invention concerns a process for thermal regulation in a continuous fluidized bed treatment process for a powdered solid, wherein the solid is treated in a fluidized bed treatment zone, at least a portion of the solid is extracted from said zone and transported to an external heat exchanger (21) containing at least one array (22) of thermal exchange tubes in which vaporizable cooling fluid circulates, fluidized or mobile bed thermal regulation by indirect heat exchange with the fluid is carried out and the portion of regulated solid is extracted for recycling into the treatment zone or to another treatment zone (1). More precisely, said portion of solid is circulated in descending mode by means of an inert or non inert fluidization fluid across the array of tubes (22) which are wound such that the current of solid intersects said tubes and that the cooling fluid is circulated in one direction in the array of tubes.

Abstract: A catalyst, e.g., a cracking catalyst, and a part of the regeneration fumes are drawn off from the dense catalytic bed of a second regenerator (9) and are introduced by force of gravity into an external exchanger (21) at a junction point beneath the level of the dense bed of the second regenerator. The heat exchange takes place in the bottom part of the exchanger below the junction point. Between the bottom end of the exchanger and the region above the junction point a dense bed zone is formed at a level which is substantially at the height of the dense bed in the regenerator and a discharge zone (27), of suitable size, for the regeneration gases and fluidization gas. The gases and fumes from the exchanger are removed in the diluted fluidized phase from the second regenerator through a conduit (28), while the catalyst is recycled into the bed of the first regenerator through a conduit (34).

Abstract: Disclosed is a cocurrent cyclone separator extractor for both the separation of a gas/solid mixture into at least one light phase, and for the extraction of gases sorbed by the solid, comprising a first elongated external enclosure, which has a substantially circular cross-section, having at a first end, external inlet means for the introduction of the mixture, said means making it possible to give at least to the light phase a helical movement in the flow direction of the mixture in said enclosure; an elongated second enclosure, which has a substantially circular cross-section of smaller diameter than the first enclosure, whose end close to the inlet means; and a second external enclosure having a substantially vertical axis of symmetry, connected to said first enclosure, said second enclosure collecting the separated dense phase and having means for the injection of a light extraction phase, injection taking place in countercurrent manner with respect to the flow of the separated dense phase and, at least i

Abstract: The invention relates to a process for catalytic cracking and the associated apparatus in which the cracking reaction takes place in two substantially vertical and successive reaction zones, the loads being introduced into the first zone where it circulates from the top downwards, then at least a part of the product obtained is introduced into a second reaction zone in which it circulates in an ascending fashion. A supplementary hydrocarbonated phase is advantageously introduced into the product entering the second zone. The invention applies particularly to heavy loads, with a U-shaped apparatus.

Abstract: A catalyst, e.g., a cracking catalyst, and a part of the regeneration fumes are drawn off from the dense catalytic bed of a second regenerator (9) and are introduced by force of gravity into an external exchanger (21) at a junction point beneath the level of the dense bed of the second regenerator. The heat exchange takes place in the bottom part of the exchanger below the junction point. Between the bottom end of the exchanger and the region above the junction point a dense bed zone is formed at a level which is substantially at the height of the dense bed in the regenerator and a discharge zone (27), of suitable size, for the regeneration gases and fluidization gas. The gases and fumes from the exchanger are removed in the diluted fluidized phase from the second regenerator through a conduit (28), while the catalyst is recycled in to the bed of the first regenerator through a conduit (34).

Abstract: Process for the catalytic conversion of a charge incorporating at least one oxygen compound such as methanol, into olefinic hydrocarbons having 2 to 4 carbon atoms. Conversion takes place in a reactor (100), into which the charge is introduced by the pipe (20), the catalytic solid by the pipe (30) and the solid entrainment gas by the pipe (40), the reactor being connected by a pipe (1) to a co-current cyclone separator (S) making it possible to separate a solid phase from a gaseous phase containing the conversion products, which is recovered by the pipe (4). The solid phase is fed by the pipe (9) to a regenerator (R), in which the catalytic particles are at least partly regenerated before being returned by the pipe (80), connected to the pipe (30), to the reactor (100).

Abstract: The conversion of a charge comprising at least one oxygen compound is performed in a reactor C, into which the charge is introduced by the pipe (11), the solid catalytic particles forming the dense phase D1 by the pipe (14) and the solid entrainment gas by the pipe (12). The reactor is connected by a pipe (1) to a cocurrent cyclone separator-mixer (MS) making it possible to separate a solid phase from a gaseous phase containing the conversion products recovered by the pipe (4'), while carrying out a quenching of said gaseous phase by a product M2 introduced by the pipe (3). The phase D1 is fed by the pipe (7) to a regenerator R before being returned by the pipe (13) into the reactor C. The mixture of the gaseous phase and the product M2 is separated in a separator and the product M2, optionally after cooling, is recycled to the mixer-separator (MS).

Abstract: A co-current separator is provided which makes it possible to separate a light phase contained in a mixture from a dense phase. Disposed downstream in the direction of circulation of the dense phase is an internal output opening of an interior enclosure. Fins are provided on the interior enclosure for limiting the progression of the light phase to the outside of the interior enclosure. The mixture is introduced tangentially into an inlet, and the dense phase is recovered at one outlet with the light phase recovered at another outlet. This makes it possible to rapidly separate the dense phase from the light phase, providing an apparatus useful for separating, for example, a solid from a gas.

Abstract: A co-current cyclone mixer-separator which makes it possible to separae a light phase L1 contained in a mixture M1 which also contains a dense phase D1 from the dense phase and to mix this phase L1 with a dense phase or with a mixture containing this phase and a light phase. The mixture M1 is introduced at and the phase D1 is recovered at. The dense phase of a mixture is introduced at and enters a second inner enclosure at, at least a part of the phase likewise entering the latter enclosure. A mixture comprising the phases, if it has been introduced, is obtained at. Preferably, the apparatus comprises blades which make it possible to limit the progress of the vortex into the outlet. This apparatus permits of a rapid heat exchange, for exmple the hardening, of a phase by a phase or a mixture. It can also be used for the rapid replacement of a phase contained in a mixture also containing a phase by a phase other than.