Abstract: A radial adsorber comprising: an adsorbent mass containing particles, a cylindrical shell ring extending along a longitudinal axis that is vertical when the adsorber is in operation, an external grid and an internal grid arranged in such a way as to be permeable to the gas and impermeable to the particles, the internal grid and external grid between them forming an annular volume housing the adsorbent mass, an internal chamber located between the vertical longitudinal axis and the internal grid, an external chamber located between the external grid and the shell ring, the internal chamber and external chamber being intended for the circulation of the gas, the external grid being formed by a plurality of wires and a plurality of supports, the supports being mounted transversely to the wires, the supports and the wires being mounted secured to one another.

Abstract: A hydrocarbon selective catalytic reduction (HC-SCR) catalyst is regenerated using a nitrogen-based reductant agent. The HC-SCR catalyst is in communication with a power system such as an internal combustion engine and receives exhaust gasses from the internal combustion engine. Sulfur in the exhaust gasses may deactivate the HC-SCR catalyst by sulfur oxides forming thereon. To remove the sulfur oxides, a nitrogen-based reductant agent is introduced to the exhaust gasses. The nitrogen-based reductant agent decomposes to nitrogen oxides and hydrogen. The hydrogen reacts with the sulfur oxides to form hydrogen sulfides thereby removing the sulfur oxides from the HC-SCR catalyst.

Abstract: Systems and methods for regenerating a spent catalyst are provided. The method can include mixing a spent catalyst with a carrier fluid to provide a mixture. The spent catalyst can include carbon deposited on at least a portion thereof. The carrier fluid can include an oxygen containing gas. The mixture can be introduced to or above an upper surface of a dense phase catalyst zone disposed within a regenerator. A gas can be introduced to a lower zone of the dense phase catalyst zone. At least a portion of the carbon deposited on the catalyst can be combusted to provide a flue gas, heat, and a regenerated catalyst.

Abstract: Systems and methods for regenerating a spent catalyst are provided. The method can include heating a hydrocarbon and a coke precursor in the presence of catalyst particles to provide a cracked hydrocarbon product and coked catalyst particles. The cracked hydrocarbon product and the coked catalyst particles can be selectively separated to provide a hydrocarbon product and coked catalyst particles. The coked catalyst particles can be mixed with a carrier fluid to provide a mixture. The mixture can be introduced to an upper surface of a dense phase catalyst zone disposed within a regenerator. A gas can be introduced to a lower zone of the dense phase catalyst zone. At least a portion of the carbon deposited on the coked catalyst particles can be combusted to provide a flue gas, heat, and a regenerated catalyst.

Abstract: Additive particles for use in a fluid catalytic cracking system are provided for reducing the opacity of flue gas that is generated from a regenerator within the system. Particles are supplied to the unit to catalyze the cracking of hydrocarbon feeds, and to react with sulfur oxides that are produced during regeneration of catalysts supplied for the cracking reactions. At least a portion of the supplied particles include active particulates and a binder, with at least a portion of the active particulates being in a size range from 0.5 to 40 microns.

Abstract: A process for catalyst regeneration is presented. The process regenerates a catalyst in a paraffin dehydrogenation process, where the reaction is endothermic. The regeneration process provides the heat for the process through heating the catalyst and removes the need for a charge heater to the dehydrogenation reactor, which in turn eliminates high temperature thermal residence time which eliminates thermal cracking of the feed and improves the overall product selectivity. In addition, plot area, equipment costs and operating complexity are reduced.

Abstract: An apparatus suitable for generating gaseous hydrocarbon fuel from a carbon based synthesis gas including a reaction chamber having a rotating shaft including a plurality of radial blades mixing and circulating carbon based synthesis gas and particulate catalyst upwardly generating gaseous hydrocarbon fuel, a stripping chamber located above the reaction chamber having a second axial rotating shaft including a plurality of radial blades driving hydrocarbon fuel radially outwardly, a source of hot stripping gas, an annular filter surrounding the stripping chamber and an annular gas collection chamber surrounding the filter. The blades in the stripping chamber are rotated independently at a greater velocity than the blades in the reaction chamber and the reaction is controlled by the temperature of the synthesis gas and the rotational velocity of the mixing blades in the reaction chamber.

Abstract: Disclosed is a catalyst distributor and process for spreading catalyst over a regenerator vessel. Nozzles disposed angular to a header of the distributor spread catalyst throughout a full cross section of the catalyst bed.

Abstract: The invention relates to a process for incorporating sulfur in the porosity of the solid particles of a catalyst for the conversion of hydrocarbons or an adsorbent. This process is carried out off-site in the presence of hydrogen sulfide that is pure or diluted in hydrogen or nitrogen, a process in which said particles are made to rise or fall in a sulfur incorporation zone that comprises at least one vibratory helical coil that is essentially tubular in shape and that comprises at least two turns, whereby said particles are subjected to a temperature profile over the majority of their path in said coil and whereby said particles are brought into contact with at least one fluid on at least one portion of their path.

Abstract: The invention concerns a process for regenerating a catalyst for the production of aromatic hydrocarbons or for reforming, comprising a step for combustion in a zone A comprising at least 2 beds A1 and A2, a step for oxychlorination in a zone B, and a step for calcining in a zone C. A portion of the effluent gas from the oxychlorination zone is recycled via at least one scrubbing section D to the inlet to beds A1 and A2. Further, a portion of the effluent gas from zone B is recycled to the combustion bed A2, passing via a blower but without passing via said scrubbing section D, and a portion is recycled to the inlet to zone B, passing via said blower but not via said scrubbing section. The invention also concerns the vessel in which said process is carried out.

Abstract: A combination of moving bed regeneration technology and CO oxidation technology is used in a novel moving bed regeneration apparatus containing an integral CO oxidation zone to solve the problem of regenerating a coke-containing catalyst that does not contain a CO oxidation promoter without generating an effluent flue gas stream containing hazardous and undesired amounts of CO. The CO oxidation zone is located in the flue gas collection zone within the moving bed regeneration apparatus and functions autogenously to eliminate the CO hazard by oxidizing CO to CO2 with a portion of the unreacted oxygen withdrawn from the coke combustion zone of the moving bed regeneration apparatus.

Abstract: Disclosed is an apparatus and process for disengaging regenerated catalyst from flue gas in a catalyst regenerator so as to avoid re-entrainment of catalyst that has settled into a bed in the catalyst regenerator using a disengaging device. A disengaging arm of the disengaging device has an outer shell that encloses the arm, an inner shell with a slot for allowing catalyst and flue gas to exit the arm and an outer baffle having a lower edge located below the opening in the outer wall. The baffle directs the catalyst and flue gas downwardly and limits radial flow. Catalyst and flue gas enter the disengaging arm through an opening in an outer wall of a riser section at a first superficial velocity and exits through a slot in a bottom of the disengaging arm at no more than 1.33 the first superficial velocity.

Abstract: The instant invention relates to a process to produce low sulfur distillate products through the hydrotreating of distillate boiling range feedstreams in the presence of a bulk metal hydrotreating catalyst.

Abstract: The instant invention relates to a process to produce liquid products through the hydroprocessing of hydrocarbonaceous feedstreams in the presence of a bulk metal hydroprocessing catalyst.

Abstract: The present invention concerns a process for ex situ oxidizing passivation of hydrocarbon hydroconversion catalysts, in particular for hydrotreatment in their sulphurized states, in which the sulphurized catalyst undergoes two treatments: contact with an oxidizing gas stream, and contact with an organic liquid (for example hydrocarbon) which partially fills its pores.

Abstract: The invention pertains to a process for combusting coke of a coke-containing FCC catalyst in a regeneration unit of a FCC unit having the introduction of oxygen-containing gas through a gas-transport unit into the regeneration unit and combusting the coke by means of an oxygen-containing gas, in which the oxygen-containing gas is cooled in a cooling unit before it is brought in contact with the coke-containing FCC catalyst. The invention further relates to an apparatus for performing said process.

Abstract: This invention relates to efficiently regenerating catalyst particles by minimizing the formation of localized “hot spots” and “cold spots” in a regeneration zone. In one embodiment, the invention includes mixing spent catalyst from a reactor and cold catalyst from a catalyst cooler in a mixing zone and directing the mixed catalyst to the regeneration zone in a fluidized manner with a fluidizing medium. In the regeneration zone, the mixed catalyst contacts an oxygen-containing regeneration medium under conditions effective to regenerate the spent catalyst contained therein.

Abstract: A process for regenerating a palladium catalyst from a catalytic reaction where the catalyst is contaminated with at least carbon. The regenerating is conducted prior to any heating step under oxidizing conditions in the regenerating section. The regenerating involves at least one heating step under a hydrogen-containing reducing atmosphere and under conditions sufficient to lower the content of carbon in the palladium catalyst.

Abstract: Process for controlling the combustion zone of a fluidized bed process comprising a regeneration zone and a reaction zone, the catalyst circulating between these two zones, and the regeneration zone comprising a combustion stage of the coke deposited on the catalyst in the reaction zone, control of the combustion zone being performed on the basis of a characteristic variable of the operation of said combustion zone, said characteristic variable being the object of automatic regulation by acting on the catalyst throughput, characterized in that the value of the catalyst throughput or of any control variable connected unequivocally to the catalyst is determined based on information on the operating values of the combustion zone, at least one of which corresponds to an independent evaluation of the level of coke deposited on the catalyst.

Abstract: Solvent extraction is used to remove wax and contaminants from an iron-based Fischer-Tropsch catalyst in a natural circulation continuous-flow system. The wax-free catalyst is then subjected to controlled oxidation to convert the iron to its initial oxidized state, Fe2O3. Reactivation of the oxide catalyst precursor is carried out by addition of synthesis gas.

Abstract: In a fluid catalytic cracking (FCC) unit, a regenerator, a stripper or a withdrawal well connecting to either of the vessels, includes a standpipe for circulating catalyst from one vessel to another, the standpipe having an inlet design which reduces gas entrainment during catalyst transport by partial de-fluidization in the standpipe inlet region. The standpipe inlet design could include multiple inlet openings through the top of the standpipe or from the side wall by slots, or both, and a horizontal disk surrounding the standpipe below the slots for blocking the upward flow of bubbles, the combination thereby forming a dense fluidization zone above the disk and surrounding the inlet, including the slots. Additionally, the disk may include a downwardly-projecting lip or edge forming an inverted void space around the standpipe and the downwardly-projecting edge may further include vent holes around its circumference which allow bubbles trapped under the disk to be vented outside the standpipe inlet region.

Abstract: A baffle-style stripping arrangement for an FCC process having substantially horizontal stripping baffles is disclosed. The stripping baffles comprise a perforated section and a downcomer section which generates transverse movement of catalyst across the baffle to ensure adequate vertical movement of stripping media. The perforated section is covered with stripping openings to provide improved stripping efficiency and catalyst flux through the stripping vessel. The perforated section may comprise a grate. Baffles may also include an imperforate section which is vertically aligned with a downcomer section of a superjacent baffle.

Abstract: The invention relates to a process for maintaining heat balance in a fluidized bed catalytic cracking unit. More specifically, the invention relates to a combustion control method capable of maintaining or restoring heat balance by conducting, under appropriate conditions, fuel and an oxygen-containing gas to a transfer line. The transfer line conducts effluent including spent catalyst and combustion products to the unit's catalyst regeneration zone.

Abstract: The invention concerns a process for regenerating a catalyst in a fixed or moving bed, for example a catalyst for reforming or for aromatic compound production, including a step for monitoring and controlling combustion completion which is carried out after the catalyst has undergone all of the combustion steps of the process. The monitoring and control step is carried out by injecting an oxygen-containing gas into the zone where monitoring and control takes place, the monitoring and control step being carried out under conditions which are more severe than those in the combustion steps. The monitoring and control step is carried out with an oxygen consumption of less than 10%. The temperature advantageously remains substantially constant. The vessel for carrying out the invention is also claimed.

Abstract: The invention concerns a process for regenerating a catalyst in a fixed or moving bed, for example a catalyst for reforming or for aromatic compound production, including a step for monitoring and controlling combustion completion which is carried out after the catalyst has undergone all of the combustion steps of the process. The monitoring and control step is carried out by injecting an oxygen-containing gas into the zone where monitoring and control takes place, the monitoring and control step being carried out under conditions which are more severe than those in the combustion steps. The monitoring and control step is carried out with an oxygen consumption of less than 10%. The temperature advantageously remains substantially constant. The vessel for carrying out the invention is also claimed.

Abstract: Process for regeneration of a catalytic moving bed in which the catalyst successively passes through at least one combustion zone A, at least one halogenation zone B, and at least one calcination zone C, whereby this process operates in a partial-regeneration-mode, the partially coked catalyst that is obtained from the last combustion zone passes into the halogenation zone in which the amount of halogen and the amount of oxygen are essentially zero--the valves of tubes (19) and (20) are then virtually closed--and the catalyst then passes through the calcination zone in which the amount of oxygen is essentially zero--the valve of tube (11) is then virtually closed.

Abstract: The invention concerns a process for regenerating a catalyst for the production of aromatic compounds, in particular for reforming, comprising combustion (A), oxychlorination (B) and calcining (C) steps, in which at least one chlorinating agent (conduit 19), at least one oxygen-containing gas (conduit 18), and water (conduit 20) are introduced into the oxychlorination step such that the H.sub.2 O/HCl molar ratio is 3 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.

Abstract: The invention concerns a process for moving bed regeneration of a reforming or aromatic hydrocarbon production catalyst. The catalyst includes a support, at least one noble metal and at least one halogen. The process includes a combustion step in which the catalyst is treated in at least two successive combustion zones. Also, the process includes each combustion zone separated from adjacent combustion zones allowing catalyst to pass and preventing passage of gas, at least one oxygen-containing gas introduced into each zone and produced gases extracted from each zone, and the severity of the operating conditions in each zone increasing in the direction of catalyst flow. Advantageously, the combustion step ends in a zone for monitoring and controlling combustion completion characterized by a low or zero oxygen consumption.

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: This invention relates to a method for sulfiding hydrocarbon conversion catalysts, e.g., hydrotreating catalysts comprising at least one metal sulfide and passivating said sulfided catalyst. The catalysts which may be treated by the method of the present invention comprise an alumina or an silica-alumina support e.g., a zeolite, and at least one Group VI metal sulfide and/or at least one Group VIII metal sulfide. In particular, the present invention provides a process for continuously activating a fresh or regenerated catalyst comprising at least one Group VI or Group VIII metal oxide supported on a particulate refractory oxide support material by converting substantially all of said Group VI or Group VIII metal oxide to the corresponding metal sulfide and passivating the resulting activated catalyst.

Abstract: An FCC arrangement uses a regenerator stripper vessel for removing CO and light hydrocarbons upstream of the regeneration zone that can operate with backmix addition of regenerated catalyst directly from the regeneration zone. The regenerator stripping vessel can also serve as a blending vessel for an the transfer of spent and regenerated catalyst back to the reaction zone for increasing the catalyst to oil ratio of the process. This invention makes the recycle of spent catalyst in large proportions possible for an FCC operation that cracks a heavy feed by eliminating light combustibles such as CO and light hydrocarbons from the regeneration zone. Elimination of light gases permits spent catalyst to be recycled to the riser despite the high delta coke produced by the heavy feed.

Abstract: The invention concerns a process for the regeneration of a used hydrocarbon treatment catalyst, preferably a reforming catalyst, containing at least one precious metal preferably platinum, optionally at least one additional metal selected from the group formed by metals from groups 7, 8, 9, 10, 13 and 14 of the periodic classification of the elements and copper, optionally and preferably at least one halogen, preferably chlorine, and at least one porous support, preferably alumina, said process comprising at least one of the following two successive steps: at least one step (1) for the combustion of the coke present on said catalyst, carried out in the presence of an oxygen-containing gas, at a temperature in the range of 300.degree. C. to 680.degree. C. for a time in the range 0.3 to 7 hours, at least one step (2) for oxyhalogenation, preferably oxychlorination, carried out in a controlled air atmosphere, at a temperature in the range 350.degree. C. to 550.degree. C., for a time in the range 0.

Abstract: A process and apparatus for the heat regulation of fluidized or fluid catalyst beds are described, the apparatus having a fluid bed heat exchanger. According to the invention, a pulverulent solid is made to flow essentially from the base of an enclosure (1) into a heat exchanger (6) having an internal separating partition (22) which defines two elongated, adjacent compartments (23, 24) communicating at their lower part. In the compartment in which the pulverulent solid flows downwards, the fluidization speed or rate is between 0.1 cm to 2 m/s, whereas in the compartment wherein the pulverulent solid rises again into the heat exchanger (6), the fluidization speed is between 0.1 and 6 m/s. The invention can be used for refining reaction (e.g., catalytic reforming), for the regeneration of a fluidized bed catalytic cracking catalyst of a petroleum or oil charge, or for the combustion of coal.

Abstract: An improved process for the alkylation of benzene in the presence of an alkylation catalyst. The catalyst bed may be caused to move in a direction countercurrent to the movement of the benzene and olefin, or a portion of the catalyst bed is periodically removed and replaced. A regeneration step, whereby the catalyst is heated in a controlled oxygen atmosphere in order to reactivate the catalyst, is also described.

Abstract: Process for sampling particulate matter in a downwardly movable bed thereof which is successively contacted by two different process gases, the second of which is moving upwardly, in such a manner that the particulate matter sampled will be fully representative of particles which have been fully contacted by the first process gas but which have not been contacted by the upwardly moving second process gas. The particulate matter is passed downwardly in the shape of an annular bed through a first annular treatment zone while the major portion of the first process gas is passed through the annular bed in a radially inward direction. The annular bed is then passed downwardly along with a small amount of the first process gas from the first treatment zone through an elongated transition zone and into the radially outermost upper portion of a generally cylindrical second treatment zone.

Abstract: Used catalyst containing carbon and sulfur deposits is continuously regenerated by staged burnoff of the carbon and sulfur using a multiple zone treatment vessel containing thin beds of catalyst. The catalyst is exposed to successively increased temperatures and oxygen concentrations to effectively remove substantially all the carbon and sulfur deposits. The used catalyst can be that removed from hydroconversion processes, such as from H-Oil, H-Coal and fluid catalystic cracking processes, and processed in a multizone treatment vessel in combination with proper auxiliary heating equipment for continuous step-wise regeneration of the catalyst. Operating conditions of catalyst temperature, oxygen concentration of gas, and catalyst residence time in each stage of the catalyst regeneration process are carefully controlled to provide staged burnoff of carbon and sulfur deposits for superior regenerated catalyst results.

Abstract: A process is described for regenerating a coke-deactivated platinum-containing zeolite catalyst material, which includes oxidizing the deactivated catalyst material in the presence of water under conditions which do not cause significant agglomeration of the platinum on the catalyst.

Abstract: An improved moving bed continuous catalytic cracking process for cracking hydrocarbon feedstocks, such as gas oil, in the absence of added hydrogen, which includes the use of a minute amount of dispersed platinum supported directly on a cracking catalyst. The trace of platinum induces a substantial increase in the heat efficiency with which coke on catalyst is converted to CO.sub.2 in the regenerator section with minimal or no detriment to the cracking reaction.

Abstract: A catalyst regeneration process and apparatus for the oxidative removal of coke from a coke contaminated fluid catalyst. The process comprises a high temperature coke combustion zone, a catalyst disengagement zone and an external heat removal zone. A mixture of coke contaminated catalyst, oxygen containing gas, hot regenerated catalyst and cool regenerated catalyst from the heat removal zone are contacted in the high temperature combustion zone, the temperature of which is controlled by adjusting the rate at which catalyst is recycled from the heat removal zone. The temperature of the catalyst-gas mixture is controlled by adjusting the rate at which hot catalyst is recycled from the disengagement zone.

Abstract: An improved moving bed continuous catalytic cracking process for cracking hydrocarbon feedstocks, such as gas oil, in the absence of added hydrogen, which includes the use of a minute amount of dispersed platinum supported directly on a cracking catalyst. The trace of platinum induces a substantial increase in the heat efficiency with which coke on catalyst is converted to CO.sub.2 in the regenerator section with minimal or no detriment to the cracking reaction.