Abstract: A chemical conversion reactor contains a substantially vertical catalytic bed between an upper end and a lower end and comprises, in combination: close to its upper end, at least one means for introducing a solid catalyst, means for introducing and evacuating said feed allowing its flow in a substantially horizontal direction through the catalytic bed, means for heating said feed integrated into said reactor, said reactor comprising, close to its lower end, at least one means for extraction of the catalyst, which extraction is differentiated between an upstream portion and a downstream portion of said catalytic bed, with respect to the direction of flow of said feed.

Abstract: The invention relates to a process for the production of aromatic compounds from a hydrocarbon fraction with a catalyst that preferably circulates in a moving bed, a process that comprises at least the following successive stages that take place in at least one zone: treatment of the fraction in the presence of hydrogen and implementing at least one reaction for dehydrogenation of naphthenes; separation of the gas effluent that contains hydrogen, the liquid product and the catalyst; regeneration of the catalyst; reduction of the catalyst; and reintroduction of the catalyst for the treatment stage; recycling in the treatment stage of at least a portion of the gas effluent that contains the hydrogen that is called recycling gas; process in which the reduction stage is carried out in the presence of recycling gas that is introduced in an amount such that the amount of pure hydrogen that is provided is between 1-10 kg/kg of catalyst, whereby the effluent that is obtained from the reduction is then separated from

Abstract: Method for processing hydrocarbons comprising at least two processing chambers and means for separating the liquid and gaseous fractions contained in the polyphasic mixture produced in the first processing chamber, said mixture coming from a zone (700) where a batch of liquid hydrocarbons, a gaseous batch and solid particles come into contact, said method comprising separation of liquid and gaseous phases located in the chamber. Equipment comprising: a) At least a first chamber comprising means inside said chamber for separating gaseous and liquid fractions coming from said zone, b) means for conveying said liquid fraction toward a second chamber, c) a second chamber comprising a second contact zone and means of introducing, into said zone, a gaseous batch and a liquid batch comprising at least a portion of the liquid fraction coming from the first chamber.

Abstract: A moving bed process for producing aromatic compounds comprises at least a first step in which principally naphthene dehydrogenation is carried out in the presence of hydrogen in a mole ratio (H2)1/(HC), said step being followed by at least one subsequent step carried out at a mole ratio (H2)2/(HC)2, the process also comprising reducing the catalyst with hydrogen in a ratio (H2)red/(HC). In accordance with the invention, (H2)1/(HC)+(H2)red/(HC)≦(H2)2/(HC)2, (HC) representing the molar quantity of feed in the first step and (HC)2 that of the subsequent step, or (H2)1/(HC)+(H2)red/(HC)>(H2)2/(HC)2, but where (H2)1/(HC) is less than (H2)2/(HC)2. Particular application to reforming.

Abstract: A reactor for chemical conversion in the presence of a gaseous diluent contains a substantially vertical catalytic bed between an upper end and a lower end and comprises, in combination: close to its upper end, at least one means for introducing a solid catalyst, means for introducing and evacuating said feed allowing its flow in a substantially horizontal manner through the catalytic bed; in the proximity of its lower end, at least one means for extracting catalyst, at least one means for heating said feed plus added diluent, said means being internal to the reactor and traversed by said feed plus added diluent in the absence of catalyst, and separating the catalytic bed into a portion upstream of and a portion downstream of said heating means relative to the direction of flow of said feed, comprising at least one means for introducing a stream of said gaseous diluent substantially in the proximity of at least one of the upper and/or lower ends of said upstream portion of the catalytic bed, to at least reduc

Abstract: A chemical conversion reactor contains a substantially vertical catalytic bed between an upper end and a lower end and comprises, in combination: close to its upper end, at least one means for introducing a solid catalyst, means for introducing and evacuating said feed allowing its flow in a substantially horizontal direction through the catalytic bed, means for heating said feed integrated into said reactor, said reactor comprising, close to its lower end, at least one means for extraction of the catalyst, which extraction is differentiated between an upstream portion and a downstream portion of said catalytic bed, with respect to the direction of flow of said feed.

Abstract: The invention relates to a process for the production of aromatic compounds from a hydrocarbon fraction with a catalyst the preferably circulates in a moving bed. In the process, a hydrocarbon feedstock that is treated by a hydrogen-rich gas is transformed. In a particular embodiment, regenerative reforming is conducted, such as for production of BTX (butene, toluene, xylenes) with continuous regeneration of the catalyst. The invention also pertains to the related device for carrying out the process.

Abstract: A moving bed process for producing aromatic compounds comprises at least a first step in which principally naphthene dehydrogenation is carried out in the presence of hydrogen in a mole ratio (H2)1/(HC), said step being followed by at least one subsequent step carried out at a mole ratio (H2)2/(HC)2, the process also comprising reducing the catalyst with hydrogen in a ratio (H2)red/(HC). In accordance with the invention, (H2)1/(HC)+(H2)red/(HC)≦(H2)2/(HC)2, (HC) representing the molar quantity of feed in the first step and (HC)2 that of the subsequent step, or (H2)1/(HC)+(H2)red/(HC)>(H2)2/HC2, but where (H2)1/(HC) is less than (H2)2/(HC)2. Particular application to reforming.

Abstract: Process for catalytic conversion in the presence of hydrogen with regeneration of the catalyst that comprises a stage for reduction of said catalyst by the hydrogen that is obtained from the catalytic conversion stage, whereby this hydrogen is purified in advance of impurities that it contains by running it over adsorbent masses, whereby said adsorbent masses are regenerated by an increase in temperature that is provided by the effluent from the reduction stage of the catalyst. Application to the processes for regenerative reforming or dehydrogenation of paraffins and naphthenes and most generally to any moving-bed process that operates in the presence of hydrogen.

Abstract: An elongate reaction vessel includes at least two stages in the vertical direction in which an endothermic or exothermic catalytic reaction is carried out and comprises:

Abstract: The invention concerns a process for converting hydrocarbons using at least one globally endothermic chemical reaction, in which a hydrocarbon feed successively traverses at least two reaction zones each containing at least one solid catalyst and comprising between said reaction zones an intermediate step, in a non catalytic zone, for reheating the stream (ST) from the first of the two reaction zones prior to its introduction into said second reaction zone, and in which said reheating is carried out in a heat exchanger, with heat transfer essentially by convection using a thermal fluid TF with a coking sensitivity index CS that is less than that of the stream ST, the difference in temperature &Dgr;T between the temperature of the fluid TF at the inlet to the exchanger and the temperature of the stream ST at the heat exchanger outlet being less than 250° C. The invention also concerns the use of said process for converting hydrocarbons and a unit for carrying out the process.

Abstract: The invention relates to a process for the production of aromatic compounds from a hydrocarbon fraction with a catalyst the preferably circulates in a moving bed. In the process, a hydrocarbon feedstock that is treated by a hydrogen-rich gas is transformed. In a particular embodiment, regenerative reforming is conducted, such as for production of BTX (butene, toluene, xylenes) with continuous regeneration of the catalyst. The invention also pertains to the related device for carrying out the process.

Abstract: Device (DME) or panel for collecting, distributing, mixing or drawing off several fluids, at least one main fluid and at least two secondary fluids, that comprises at least:

Abstract: The invention concerns a process and unit for regenerating a catalyst for the production of aromatic compounds, in particular for reforming, the catalyst being in a moving bed, comprising combustion, oxychlorination and calcining steps, in which at least one chlorinating agent, at least one oxygen-containing gas, and water are introduced into the oxychlorination step such that the H.sub.2 O/HCl molar ratio is 1 to 50, the oxychlorination step being carried out in the presence of an oxychlorination gas containing less than 21% of oxygen and at least 50 ppm by weight of chlorine (based on HCl), and at a temperature of 350-600.degree. C., and in which the combustion step is carried out in at least two combustion zones, each zone being separated from the adjacent zones, and at least one gas charged with oxygen is introduced into each zone, the gases produced being extracted from each zone, and in which the severity of the operating conditions increases in the direction of flow of the catalyst.

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: The invention relates to a downflow fluid cracking process and apparatus, particularly suitable for use in the catalytic cracking of heavy hydrocarbon charges. More specifically, removal of at least partly regenerated catalyst, which must be recycled to the reactor 1 from a dense phase 17a contained in a regenerator 17, and the introduction of the catalyst into the upper part 3 of the reactor 1 takes place under conditions such that the density of the thus formed gas-solid suspension is between 80 and 500 kg/m.sup.3 prior to its contacting with the charge, which is introduced by the injectors 5.

Abstract: The invention relates to a downflow fluid cracking process and apparatus. More specifically, sampling takes place of the at least partly regenerated catalyst, which must be recycled to the reactor 1 from a dense phase 17a, contained in a regenerator 17 and the stage of introducing the catalyst into the upper part 3 of the reactor 1 takes place under conditions such that the density of the thus formed gas-solid suspension is between 80 and 500 kg/m.sup.3 prior to its contacting with the charge, which is introduced by the injectors 5.

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: The invention relates to a method of and an apparatus for fluidised bed regeneration of a catalyst containing coke.The catalyst and some of the regeneration fumes are drawn off from the dense bed of a regenerator (1) and are introduced by gravity into an external exchanger at a junction point below the level of the dense bed of the regenerator. Heat exchange is carried out in the lower part of the exchanger (7) below the junction point. From the bottom end of the exchanger up to above the junction point a dense bed zone is created the level of which is established substantially at the height of the dense bed in the regenerator and a zone (15) of suitable size for the escape of regeneration gases and fluidisation gas. The gases and fumes are drawn off into the dilute fluidised phase (18) of the regenerator through a duct (17) while the catalyst is recycled to the dense bed of the regenerator through a different duct (25) from that in which the fluidisation air is circulating.