Abstract: A fluidized bed reactor for producing para-xylene and co-producing light olefins from benzene and methanol and/or dimethyl ether, including a first distributor and a second distributor. The first distributor is located at the bottom of the fluidized bed, and the second distributor is located at the downstream of the first distributor along a gas flow direction. Also, a method for producing para-xylene and co-producing light olefins, including the following steps: a material stream A enters a reaction zone of the fluidized bed reactor from the first gas distributor; a material stream B enters the reaction zone of the fluidized bed reactor from the second gas distributor; a reactant contacts a catalyst in the reaction zone to generate a gas phase stream comprising para-xylene and light olefins.

Abstract: A particle disengagements device comprising a baffle plate, wherein the baffle plate comprises one or more guide baffles and one or more separation baffles, wherein the one or more guide baffles and the one or more separation baffles define one or more air flow paths and one or more solid flow paths and associated systems and methods.

Abstract: Systems for separating a contaminant trapping additive from a cracking catalyst may include a contaminant removal vessel having one or more fluid connections for receiving contaminated cracking catalyst, contaminated contaminant trapping additive, fresh contaminant trapping additive, and a fluidizing gas. In the contaminant removal vessel, the spent catalyst may be contacted with contaminant trapping additive, which may have an average particle size and/or density greater than the cracking catalyst. A separator may be provided for separating an overhead stream from the contaminant removal vessel into a first stream comprising cracking catalyst and lifting gas and a second stream comprising contaminant trapping additive. A recycle line may be used for transferring contaminant trapping additive recovered in the second separator to the contaminant removal vessel, allowing contaminant trapping additive to accumulate in the contaminant removal vessel.

Abstract: A particle disengagements device comprising a baffle plate, wherein the baffle plate comprises one or more guide baffles and one or more separation baffles, wherein the one or more guide baffles and the one or more separation baffles define one or more air flow paths and one or more solid flow paths and associated systems and methods.

Abstract: The present invention discloses a process for the catalytic cracking of a weakly coking feedstock having a Conradson carbon residue of 0.1% by weight and a hydrogen content of greater than 12.7% by weight, comprising at least a feedstock cracking zone, a zone for separating/stripping the effluents from the coked catalyst particles and a zone for regenerating said particles, characterized in that at least a solid carbon material in the fluidized state, having a carbon content equal to or greater than 80% by weight, is injected upstream of and/or during the catalyst regeneration step into a dense bed of coked catalyst.

Abstract: The invention relates to a method for removing solids in dust and sulphur oxides from process gases generated in a metallurgical process by a wet process. At least part of basic liquid is fed into the gas flow containing solids in at least one cascade scrubber in order to mix basic liquid with the gases and solids to be cleaned at the latest during the wetting of the gases and solids in the water space of the cascade scrubber, and the mixture containing basic liquid, wetted gases and solids are directed to have a cascade shower in each cascade scrubber in order to remove sulphur and solids from the gases.

Abstract: Device for use in a fluidized bed reactor includes a gas-solid separator communicated with an outlet of the fluidized bed reactor; a vertically arranged damper, a solid outlet of the gas-solid separator communicated with a lower region of the damper, a gas outlet of the gas-solid separator communicated with an upper region of the damper; a fine gas-solid separator, an inlet of the fine gas-solid separator communicated with the upper region of the damper, and a solid outlet of the fine gas-solid separator communicated with the lower region of the damper. Product from the fluidized bed reactor is fed into the preliminary gas-solid separator, most solid catalysts separated and fed into the lower region; the product entraining the rest catalysts is fed into the upper region, and into the fine gas-solid separator, the rest catalysts fed into the lower region; and final product is obtained from the fine gas-solid separator.

Abstract: One exemplary embodiment can be a process for fluid catalytic cracking. The process can include sending a first catalyst from a first riser reactor and a second catalyst from a second riser reactor to a regeneration vessel having a first stage and a second stage. The first catalyst may be sent to the first stage and the second catalyst may be sent to the second stage of the regeneration vessel. Generally, the first stage is positioned above the second stage.

Abstract: A fluidized bed reactor system with one or more fluidized bed reactors for carrying out chemical or physical reactions, at least one reactor thereof being a rapidly fluidized reactor to be operated as a circulating fluidized bed and having, at the upper end, a fluid outlet, a particle separator, and a particle line connected thereto for the purpose of feeding back separated fluidized bed particles into the same or a further reactor, wherein, at least one rapidly fluidized reactor has one or more flow control devices producing reaction zones that are separate from one another, and in order to control the flow conditions into the reaction zones, one or more of these flow control devices are specifically adjustable from outside of the system.

Abstract: Method for calibrating a device for measuring back pressure in open-ended chemical reactor tubes, comprising the steps of: providing a device for measuring back pressure in open-ended chemical reactor tubes, including a frame member and a plurality of injector tubes mounted on the frame member with a spacing between the injector tubes; providing a test stand, comprising a frame member; a base supporting said frame member; and a plurality of calibration tubes mounted on the frame member, each of said calibration tubes having an open top and a dosed bottom, with a precision orifice in the dosed bottom to simulate the chemical reactor tubes to be tested; inserting the plurality of injector tubes into the respective calibration tubes; sealing between the injector tubes and the calibration tubes; sending gas through the injector tubes and taking a back pressure reading for each of the injector tubes; and generating correction factors for each injector tube to correct for variations in the back pressure readings.

Abstract: A novel process for cracking olefins including contacting a hydrocarbon oil with a catalyst in a riser reactor having multiple reaction zones under cracking reaction conditions; separating reaction products and the catalyst; regenerating at least a part of spent catalyst obtained, contacting a part of the regenerated catalyst with the hydrocarbon in the first reaction zone; contacting the other part of the spent catalyst and/or regenerated catalyst in at least one reaction zone after the first reaction zone with the products obtained in previous reaction zones.

Abstract: A method for producing liquid ferroalloy by direct processing of manganese and chromium bearing iron compounds, by the steps: of mixing carbonaceous reductant, fluxing agent, and a binder with materials such as iron sands, metallic oxides, manganese-iron ore concentrates and/or chromium-iron ore concentrates and silica sands, to form a mixture; forming agglomerates from the mixture; feeding the agglomerates to a melting furnace with other materials; melting the feed materials at a temperature of from 1500 to 1760° C. and forming a slag and hot metal; removing the slag; tapping the hot metal as liquid ferroalloy, and utilizing the off-gases from the melting furnace as combustion fuel to drive a turbine and to generate electricity.

Abstract: A staged fluidized catalytic cracker and method for cracking a hydrocarbonaceous material includes a plurality of staged reactors that have catalyst particles flowing in series from one reactor to the next and hydrocarbon feed that is delivered in parallel to the reactors. Between each reactor the partially spent catalyst is actively stripped to partially reactivate the catalyst. Once the catalyst is fully spent in the final reactor the catalyst can be oxidatively regenerated.

Abstract: A reactor design and process for the dehydrogenation of hydrocarbons is presented. The reactor design includes a multibed catalytic reactor, where each of the reactor beds are fluidized. The catalyst in the reactor cascades through the reactor beds, with fresh catalyst input into the first reactor bed, and the spent catalyst withdrawn from the last reactor bed. The hydrocarbon feedstream is input to the reactor beds in a parallel formation, thereby decreasing the thermal residence time of the hydrocarbons when compared with a single bed fluidized reactor, or a series reactor scheme.

Abstract: A method for separating and recovering ultrafine particulate solid material from a suspension or slurry of the solid material and a hydrocarbon liquid by precipitation or flocculation of a heavy fraction of the hydrocarbon liquid with an effective amount of a precipitation or flocculation agent such that the precipitated heavy fraction encapsulates the particulate solid material. The method further comprises coking the precipitated heavy fraction and grinding the coked product to an ultrafine size.

Abstract: This invention is directed to a method and apparatus for regenerating a catalyst used in an FCC unit, including providing a spent catalyst into an upper portion of a regenerator, maintaining a calcination phase, a gasification phase, and a combustion phase of fluidized catalyst in the regenerator, combusting carbon in the combustion phase and producing a combustion flue gas, reacting carbon in the gasification phase with the combustion flue gas to form a carbon monoxide rich flue gas, and calcining the spent catalyst with the carbon monoxide rich flue gas.

Abstract: A method for separating and recovering ultrafine particulate solid material from a suspension or slurry of the solid material and a hydrocarbon liquid by precipitation or flocculation of a heavy fraction of the hydrocarbon liquid with an effective amount of a precipitation or flocculation agent such that the precipitated heavy fraction encapsulates the particulate solid material. The method further comprises coking the precipitated heavy fraction and grinding the coked product to an ultrafine size.

Abstract: A process and device to optimize the yield of fluid catalytic cracking products through a reactive stripping process are disclosed. One or more hydrocarbon streams (3) are introduced in an intermediary region of the stripper (1) of a fluid catalytic cracking unit (FCC), from a device that allows a homogeneous distribution with adequate dispersion. This/these stream(s) react(s) with the catalyst of FCC, although its activity is reduced due to the adsorption of hydrocarbons in the reaction zone, generating products that improve and/or change the global distribution of products, providing a refinery profile adequate to meet quality demands and requirements.

Abstract: The present invention relates to a thermo catalytic process to produce diesel oil from vegetable oils, in refineries which have two or more Catalytic Cracking (FCC) reactors. At least one reactor processes heavy petroleum or residue in conventional operation conditions while at least one reactor processes vegetable oils in proper operation conditions to produce diesel oil. This process employs the same catalyst employed in the FCC process, which processes conventional feedstocks simultaneously. This process transforms high heat content raw materials into fuel hydrocarbons. It may improve efficiency for the obtainment of highly pure products and may not yield glycerin, one by-product of the transesterification process. The diesel oil produced by said process may have superior qualities and/or a cetane number higher than 40. Once cracking conditions occur at lower temperatures, it may form a less oxidized product, which is consequently purer than those obtained by existent technology.

Abstract: A dual riser FCC process is disclosed wherein first and second hydrocarbon feeds (5, 6) are supplied to the respective first and second risers (2, 4) to make an effluent rich in ethylene, propylene and/or aromatics. Where the hydrocarbon feeds are different, the respective risers can have different conditions to favor conversion to ethylene and/or propylene. A minor amount of a coke precursor (80, 82) can be added to one or both of the hydrocarbon feeds (5, 6) to reduce or eliminate the amount of supplemental fuel needed to heat balance the system. The different feeds, including the coke precursor and any recycle streams (36, 44) can be segregated by type to improve olefin yields, including an embodiment where the paraffinic feeds are supplied to one riser and the olefinic feeds to the other.

Abstract: The present invention describes novel methods for reducing sulfur in gasoline with hydrotalcite like compound additives, calcined hydrotalcite like compounds, and/or mixed metal oxide solution solutions. The additives can optionally further comprise one or more metallic oxidants and/or supports. The invention is also directed to methods for reducing gasoline sulfur comprising contacting a catalytic cracking feedstock with a mixed metal oxide compound comprising magnesium and aluminum and having an X-ray diffraction pattern displaying a reflection at least at a two theta peak position at about 43 degrees and about 62 degrees, wherein the ratio of magnesium to aluminum in the compound is from about 1:1 to about 10:1.

Abstract: A fluidized-bed reactor is disclosed. The fluidized-bed reactor steadies the gas flow through the fluidized bed chamber of the reactor. The swirl chamber of the reactor consists of a conical housing in which a conical insert is also situated. This creates an annular gap between the housing and the insert, which acts as the swirl chamber and which, according to the geometry of the two components, causes a velocity of the gas flow which remains the same along the height, which increases or which decreases. Such a reactor can also be called a constant annular-gap reactor.

Abstract: The present invention is directed to a hydrocarbon conversion apparatus and process. The apparatus comprises the following: a plurality of riser reactors, each having a first end into which a catalyst is fed, a second end through which the catalyst can exit, and optionally a center axis extending therebetween. The apparatus also includes a separation zone having a plurality of inlets, each inlet not being oriented along the center axes of the riser reactors, the separation zone being provided to separate the catalyst from products of a reaction conducted in the hydrocarbon conversion apparatus. A plurality of deviating members are also provided, each deviating member being in fluid communication between the second end of a respective riser reactor and a respective inlet of the separation zone. The apparatus also includes a catalyst retention zone provided to contain catalyst, which is fed to the riser reactors.

Abstract: A reactor apparatus and process for contacting hydrocarbons with catalyst. The reactor apparatus comprises a plurality of tubular reactors each having a first end into which a catalyst is fed and a second end through which the catalyst and product exit the tubular reactor. A catalyst retention zone is provided to contain catalyst and feed catalyst to the tubular reactors. A separation zone is provided to separate the catalyst from products of a reaction conducted in the apparatus. A transport conduit having a first end in fluid communication with the second ends of at least two of the tubular reactors and a second end extending into the separation zone transports product and catalyst to the separation zone. A catalyst return in fluid communication with the separation zone and the catalyst retention zone returns catalyst to the catalyst retention zone.

Abstract: An apparatus and method for contacting fluids in a fluid-solids contacting chamber is disclosed. The fluid-solid contacting chamber has a plurality of beds, and the chamber comprises a plurality of conduits and outlet ports that are capable of providing improved fluid distribution of fluids that are introduced above or between the beds. One or more conduits are arranged within a single conduit, which provides a compact and inexpensive assembly for conveying the fluids to each conduit's outlet port. In operation, the fluid flow to the outlet port of each conduit is regulated within that outlet port's most efficient operating range, and since the flows can regulated simply by hand, the method of this invention can be practiced readily. Catalytic condensation and other hydrocarbon process units that employ this invention will have increased on-stream efficiencies and realize significant economic benefits.

Abstract: The present invention provides a catalytic cracking reactor system and process in which a riser reactor is configured to have two sections of different radii in order to produced improved selectivity to propene and butenes as products.

Abstract: A fluidized catalytic cracking process for catalytically cracking a feed to lighter products includes introducing a heated catalyst and the feed into a bottom riser of a fluidized catalytic cracking apparatus and allowing the heated catalyst and the feed to preaccelerate upwardly within the bottom riser as a mixture; flowing the mixture upwardly from the bottom riser through a plurality of microriser tubes disposed within a regenerator under conditions effective to cause a cracking reaction of the hydrocarbons and result in a mixture including coked catalyst and hydrocarbon vapors; passing the mixture from the microriser tubes through a catalyst separator for separating the coked catalyst from the hydrocarbon vapors; collecting coked catalyst in a stripper for stripping out hydrocarbon vapors carried along with the coked catalyst and introducing the coked catalyst collected into a regenerator; simultaneous with flowing the mixture, combusting the coked catalyst within the regenerator under conditions effectiv

Abstract: A method for replacing particles in a process that transfers particles is disclosed. This invention employs a seal zone which is in communication with two zones of the process and in which particles that are being added to the process are purged. This invention allows particles to be replaced without reducing the normal rate of particle transfer through the process, which results in a savings in downtime costs. This invention is adaptable to a multitude of processes for the catalytic conversion of hydrocarbons in which deactivated catalyst particles are regenerated.

Abstract: A process for contemporaneously catalytically cracking a paraffin rich feedstock and a heavy feedstock wherein the feedstocks are segregated prior to catalytic cracking in separate reactors with regenerated particulate catalyst solids. The process provides for the separate optimal cracking of paraffinic constituents and heavy naphthenic constituents while maintaining an overall heat balance.

Abstract: An improved riser reactor containing a plurality of substantially vertically oriented venturis connected in series whereby the venturis have a maximum diameter, D.sub.1, and a minimum diameter, D.sub.2 ; and, apparatus for connecting the venturis end to end in which the cross-sectional area of the venturis at D.sub.1 is A.sub.1 and the cross sectional area at D.sub.2 is A.sub.2 and the ratio of A.sub.1 /A.sub.2 is between about 1.1 and about 113, preferably between about 2 and about 100, most preferably between about 5 and about 50. The present invention also includes a process for catalytic cracking of a liquid hydrocarbon feed by use of the riser reactor of this invention.

Abstract: This FCC process suspends a layer of catalyst in a riser proximate or above the riser outlets. The density at the riser outlets is higher than the flowing density in the riser. The suspended catalyst provides a disengagement zone that enhances the separation of catalyst from product vapors. The riser operates in a manner that prevents any discharge of catalyst from its end. The arrangement also provides a convenient method for vetoing stripping vapors into a closed reactor cyclone system.

Abstract: A method and apparatus for replacing particles in a process that transfers particles is disclosed. This invention employs a seal zone which is in communication with two zones of the process and in which particles that are being added to the process are purged. This invention allows particles to be replaced without reducing the normal rate of particle transfer through the process, which results in a savings in downtime costs. This invention is adaptable to a multitude of processes for the catalytic conversion of hydrocarbons in which deactivated catalyst particles are regenerated.

Abstract: Disclosed is a method for improving fluid cracking catalyst performance by increasing metal contamination incrementally while cracking two different feedstocks that have different concentrations of metal contaminants. The relative amount of metal contamination is controlled by magnetic separation. The incrementally increased cracking catalyst is used in cracking a second feedstock.

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 process for contemporaneously catalytically cracking a paraffin rich feedstock and a heavy feedstock wherein the feedstocks are segregated prior to catalytic cracking in separate reactors with regenerated particulate catalyst solids. The process provides for the separate optimal cracking of paraffinic constituents and heavy naphthenic constituents while maintaining an overall heat balance.

Abstract: A process and apparatus for increasing the coke burning capacity of FCC catalyst regenerators is disclosed. An auxiliary regenerator receives spent catalyst from an FCC stripper and burns some of the coke at turbulent or fast fluidized bed conditions. Partially regenerated catalyst and flue gas enter a low pressure drop cyclone discharging more than 90% of the partially regenerated catalyst down into a bubbling or fast fluidized bed in the primary regenerator. Flue gas from the auxiliary regenerator is discharged into the dilute phase above the bed in the primary regenerator. Catalyst entrainment from the fluidized bed in the primary regenerator may be reduced because less combustion air is needed as a result of partial regeneration in the auxiliary regenerator. Reduced NOx and dust emissions, and/or increased coke burning capacity, may be achieved, especially when a bubbling dense bed primary catalyst regenerator is used.

Abstract: A method and apparatus for an FCC process uses means for dissipating turbulent flow at the outlet of a disengaging vessel to provide a quick separation of catalyst from product vapors and to prevent reentrainment of catalyst into the disengaging vessel. The process and apparatus use a riser for the conversion of an FCC feedstock and direct the effluent from the riser directly into a disengaging vessel to separate catalyst from the product vapors. Catalyst is directed downwardly out of the outlet of the disengaging vessel and through a series of dissipator plates that dissipate turbulent flow by eliminating the tangential velocity that would be other-wise introduced by the vortex and would lead to reentrainment of catalyst. A stripping vessel is located immediately below the disengaging vessel outlet to receive catalyst as it leaves the dissipator plates.

Abstract: A staged catalytic cracking process and apparatus is disclosed where each stage has a catalyst to oil ratio of at least 15 and there are individual hydrocarbon feeds to each stage and product removal from each stage. There is a residence time profile with the first stage having a short residence time and the successive stages having progressively longer residence times. Further, there is a feed profile with the lighter components of the total feed going to the first stage and the heavier components being fed to the later stages. The apparatus has a generally vertical orientation which permits it to be incorporated into existing cracking units for upgrading and also easily provides for both short and long residence times.

Abstract: A method and apparatus for an FCC process uses dissipator plates at the outlet of a disengaging vessel to provide a quick separation of catalyst from product vapors and to prevent reentrainment of catalyst into the disengaging vessel. The process and apparatus use a riser for the conversion of an FCC feedstock and direct the effluent from the riser directly into a disengaging vessel to separate catalyst from the product vapors. Catalyst is directed downwardly out of the outlet of the disengaging vessel and through a series of dissipator plates that eliminate the tangential velocity that would be otherwise introduced by the vortex and would lead to reentrainment of catalyst. A stripping vessel is located immediately below the disengaging vessel outlet to receive catalyst as it leaves the dissipator plates. The apparatus and process are specifically suited for operation without a reactor vessel for containment of the disengaging vessel and cyclones.

Abstract: FCC process uses an open reactor vessel to house cyclones or other separation devices that reduce the carry through of product gases with the catalyst into the reactor vessel to less than 10 wt. % so that the catalyst in the reactor vessel provides a secondary dealkylation zone. By using a highly efficient separation device to remove product from the catalyst, the environment in the reactor vessel receives a low volume of cracked hydrocarbons from the riser conversion zone and provides a convenient secondary reaction zone that receives a recycled heavy gasoline fraction separated from the riser product stream. Dealkylation in the secondary reaction zone provides additional light gasoline to satisfy T90 requirements.

Abstract: This FCC process suspends a catalyst and a riser proximate or above the riser cyclone inlets at a density that is higher than the flowing density in the riser. The suspended catalyst provides a disengagement zone that enhances the separation of catalyst from product vapors. The riser operates in a manner that prevents any discharge of catalyst from its end. The arrangement also provides a convenient method for venting stripping vapors into a closed reactor cyclone system.

Abstract: The present invention features the use of a particulate sorbent and a particulate FCC catalyst, which are physically separable, sequentially in the same FCC riser, followed by separation of commingled spent catalyst and sorbent particles from vapors, and the subsequent primary partial regeneration and heat up of spent sorbent particles and catalysts particles in an oxygen deficient burning zone, followed by physical separation of partially regenerated catalyst and sorbent particles, preferably using a cyclonic classifier to effect the separation. This is followed by secondary regeneration of the resulting segregated partially regenerated sorbent and catalyst streams in oxygen rich combustion zones to fully regenerate sorbent and catalyst particles.

Abstract: The conventional wye (where the clean regenerated catalyst returns from the regenerator to contact the feed as it enters the riser) is replaced with two or more wyes, all connected between the regenerator outlet and the inlet to a common short cracking riser. Each wye has a separate injector which can inject; e.g., diesel oil, so that neat (unmixed) diesel contacts clean catalyst and the mixture rises up a smaller riser before entering a short main riser where the largely cracked mixture is admixed with similar cat-vacuum bottoms, etc. mixtures from the other wyes. Most cracking occurs before entering the common riser so the effect is similar to a riser cracker operating on a single unmixed feed.

Abstract: An FCC process uses an open reactor vessel to house cyclones or other separation devices that reduce the carry though of product gases with the catalyst into the reactor vessel to less than 5 wt. % so that the catalyst in the reactor vessel can contact a secondary feedstock. By using a highly efficient separation device to remove product from the catalyst the environment in the reactor vessel receives a low volume of feed hydrocarbons and riser by-products. These by products comprise mainly C.sub.2 and lighter gases which are inert to a variety of other feedstreams. Possible secondary feedstreams include hydrotreated heavy naphtha, hydrotreated light cycle oil, light reformate and olefins. It is highly useful to use the secondary feedstream to heat the catalyst in the reactor vessel to facilitate hot stripping of the catalyst. Heat may be introduced in this manner by heating the secondary feedstream or using a feedstream that produces an exothermic reaction in the reactor vessel.

Abstract: A method and apparatus for an FCC process uses dissipator plates at the outlet of a disengaging vessel to provide a quick separation of catalyst from produce vapors and to prevent reentrainment of catalyst into the disengaging vessel. The process and apparatus use a riser for the conversion of an FCC feedstock and direct the effluent from the riser directly into a disengaging vessel to separate catalyst from the product vapors. Catalyst is directed downwardly out of the outlet of the disengaging vessel and through a series of dissipator plates that eliminate the tangential velocity that would be otherwise introduced by the vortex and would lead to reentrainment of catalyst. A stripping vessel is located immediately below the disengaging vessel outlet to receive catalyst as it leaves the dissipator plates.

Abstract: A process and apparatus for regeneration of coked catalyst used in the fluidized cracking of heavy oils is disclosed. A high efficiency catalyst regenerator, with a fast fluidized bed coke combustor, dilute phase transport riser, and second fluidized bed is used but modified so that at least some coked catalyst is added directly to the second fluidized bed. The coked catalyst can be heated by direct contact heat exchange in the second fluidized bed and then charged to the coke combustor, or the coked catalyst can be regenerated in the second fluidized bed, or some combination of both. Adding catalyst to the second fluidized bed increases the coke burning capacity of these regenerators, and/or permits a drier regeneration.

Abstract: A process for treating catalytic particles in a vertical chamber is disclosed. The catalytic particles comprise spent catalysts from such hydroprocesses as hydrocracking and hydroreforming. The process comprises suspending the catalytic particles in a gaseous atmosphere of a vertical chamber for a time sufficient to remove the waste products from the catalytic particles. The process can be used to remove carbonaceous and sulfur deposits from the surface of the particles as well as volatile hydrocarbons and hydrates.

Abstract: In a two stage catalytic cracking process a heavy cycle gas oil fraction (HCGO) nominal boiling range 600.degree. F. to 1050.degree. F., API gravity of -10.degree. to +10.degree. and 65 to 95 vol % aromatics is recycled to extinction between an ebullated bed hydrocracking zone and fluidized catalytic cracking zone to yield a liquid fuel and lighter boiling range fraction as the light fraction from each zone.The catalyst in the fluidized catalytic cracking zone is maintained at a micro activity 68 to 72 while cracking a virgin gas oil to HCGO. HCGO is then mixed with vacuum residuum and hydrocracked in an ebullated bed reactor. The mid range fraction is recycled to the fluidized catalytic cracking zone. The 1000.degree. F..sup.+ fraction is blended with a fuel oil.

Abstract: An improved process for controlling desired product distribution in fluidized catalytic cracking of olefins is provided wherein riser reactor temperature profiles are controlled by means of atomized quench streams provided downstream of the hydrocarbon feedstock charge level.

Abstract: The present invention features the use of a particulate sorbent and a particulate FCC catalyst, which are physically separable, sequentially in the same FCC riser, followed by separation of commingled spent catalyst and sorbent particles from vapors, and the subsequent primary partial regeneration and heat up of spent sorbent particles and catalysts particles in an oxygen deficient burning zone, followed by physical separation of partially regenerated catalyst and sorbent particles, preferably using a cyclonic classifier to effect the separation. This is followed by secondary regeneration of the resulting segregated partially regenerated sorbent and catalyst streams in oxygen rich combustion zones to fully regenerate sorbent and catalyst particles.