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: A resid refining reactor has an ebullated catalyst bed. Hydrogen gas is released into the catalyst bed at a point which is far enough above a distributor plate at the bottom of the catalyst bed to form a gas updraft in a committed zone through the bed. This committed updraft causes a reduction in gas holdup which increases the residence time of a liquid phase in the catalyst bed.

Abstract: An FCC process and apparatus is arranged to provide a low volume dilute disengagement zone in a reactor vessel and a quench zone immediately downstream of the reactor vessel. A vented riser that provides an open discharge of catalyst and gaseous products is directly discharged into a reactor vessel. The interior of the reactor vessel is arranged such that the outlet of the reactor riser is located close to and directed at the top of the reactor vessel. The reactor vessel operates with a dense bed of catalyst having an upper bed level that is only a short distance below the outlet of the reactor riser. The cyclone separators are located to the outside of the reactor riser and circulate catalyst back to the dense bed of the reactor section. The quenching takes place downstream of the cyclone separators.

Abstract: A process for short contact time cracking of heavy feed. A falling, annular curtain of hot regenerated FCC catalyst, or hot inert solids, is formed over a cone shaped plug valve. Hydrocarbons pass from under the cone, or via a hollow stem, in radial in to out flow to contact the falling curtain of solids. After 0.01 to 1.0 seconds of contact time, solids and cracked vapor are separated, preferably in a bell separator beneath the reaction zone. Downflow of reactants into a contiguous upflowing stripper minimizes attrition.

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: A multi-stage cyclone for fluidized catalytic cracking of heavy oils is disclosed. A low efficiency inertial separator concentrates solids, FCC catalyst and fines, by forcing gas and entrained solids to make from 1/2 to 3/4 turn. Gas, with most of the solids content removed, is charged directly into the inlet horn of a conventional high efficiency cyclone. The solids concentrator/cyclone device may be used in FCC regenerators or reactors to reduce particulate losses, reduce catalyst attrition, and reduce erosion of cyclones caused by high catalyst loadings.

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.

Abstract: A process for demetallizing metals contaminated FCC catalyst in an FCC regenerator. A metals getter additive, with higher settling velocity, is added to the regenerator, to remove metals from FCC catalyst by solid-solid interaction. The FCC catalyst forms a light, discrete, dense phase fluidized bed on top of a fluidized bed of additive. FCC catalyst is recycled to the cracking reactor from the top fluidized bed, while additive can be withdrawn from the lower fluidized bed for disposal or for metals recovery and recycle. Additive can be optimized for metals removal and will not dilute the cracking catalyst in the FCC reactor.

Abstract: A fluidized catalytic cracking process operates with a turbulent or fast fluidized bed (FFB) spent catalyst stripper. Higher vapor velocities in the stripper improve stripping. Preferably spent catalyst is added to the stripper via cyclone diplegs. Preferably most of the spent catalyst is added into the bed near the top of the FFB stripper is removed via the top of the stripper, to a contiguous, annular bubbling dense bed stripper surrounding the FFB stripper. Some catalyst may be removed from the base of the FFB stripper.

Abstract: This invention provides a method of reducing the sulfur oxide emissions from the regenerator of an FCC process that cracks a sulfur containing feedstream. The sulfur oxide emissions are reduced by using an essentially sulfur free lift gas stream to shift the sulfur concentration equilibrium between the product stream from the reaction zone and the flue gas stream from the regeneration zone. Sulfur compounds present in the FCC feed leave the reaction zone as volatile sulfurous gases in the product vapor stream or as adsorbed sulfur compounds on the catalyst. Sulfurous gas in the product vapors is mainly H.sub.2 S. By lowering the concentration of H.sub.2 S that enters the riser with the lift gas the equilibrium reaction of sulfur with hydrogen in the riser is favorably shifted to increase the production of H.sub.2 S and decrease the lay down of sulfur compounds in the coke that forms on the catalyst.

Abstract: Oxides of nitrogen (NO.sub.x) emissions from an FCC regenerator are reduced by forcing the regenerator to operate between full and partial CO burn mode. Operating with less than 1 mole % O2 and up to 1 or 2% CO in the flue gas creates conditions which oxidize nitrogen compounds in coke on spent catalyst to NOx, and simultaneously convert NOx in the regenerator to nitrogen. A downstream CO boiler can burn this low CO flue gas without producing large amounts of NOx. Most NOx emissions can be eliminated. An apparatus, with the regenerator air:coke ratio controlled by both CO and O2 analyzers monitoring regenerator flue gas, is also disclosed.

Abstract: Process and apparatus for the removal of carbonaceous materials from particles containing such materials, comprising introducing said particles into the lower part of a first, riser-type reactor, into which lower part an oxygen-containing gas is introduced, the reactor being operated under entrainment conditions with a relatively high density phase in the lower part and with a relatively low density phase in the upper part at a temperature suitable to burn off carbonaceous materials at such a rate that the flue gas at the top of the reactor does not contain any substantial amount of oxygen, separating solids and gas at the top of the reactor, introducing the separated particles into the upper part of a second, fluidized bed-type reactor while introducing an oxygen-containing gas into the lower part of the second reactor, the reactor being operated under fluidized bed conditions at a temperature suitable to burn off carbonaceous materials, the amount of oxygen-containing gas being established in such a way tha

Abstract: The provision and operation of backmix coolers is facilitated by a cooler arrangement that has the backmix portion of the cooler in an inverted position. In this position the heat exchange portion of the cooler is located above the source of hot catalyst. Hot catalyst for heat exchange in the cooler enters and leaves the heat exchange zone from below the location of the heat exchange tubes. The inverted position prevents any collection of debris in the bottom of the cooler, eliminates high velocity impingement of fluidizing medium on the tube, and facilitates the incorporation of the cooler in FCC units by avoiding interference with other equipment.

Abstract: A process and apparatus for the regeneration of spent FCC catalyst in a single vessel are disclosed. In one embodiment, catalyst is at least partially regenerated in a primary stage comprising a fast or turbulent fluidized bed. The flue gas is discharged up, with some and preferably most of the catalyst discharged laterally, through windows, into a second fluidized bed, preferably disposed as an annulus about the first. In another embodiment a cyclone separator is closely coupled to, but spaced from, the primary regeneration stage, to rapidly separate catalyst from first stage flue gas, and minimize thermal stress.

Abstract: A process and apparatus for simultaneously heating and cooling of spent FCC catalyst during regeneration in a high efficiency FCC regenerator, one using a fast fluidized bed coke combustor. The coke combustor burns coke from spent catalyst in a turbulent or fast fluidized bed, and discharges catalyst and flue gas up into a dilute phase transport riser. Catalyst is separated into flue gas and a bubbling dense bed of catalyst. The coke combustor is heated by recycling hot catalyst from the bubbling dense bed and simultaneously cooled by a backmixed heat exchanger. Catalyst flows from the combustor to the cooler and is displaced back into the combustor by adding air to the catalyst in the cooler. Heating promotes rapid coke combustion, while cooling reduces thermal and hydrothermal deactivation of the spent catalyst.

Abstract: A process and apparatus for multi-stage fluidized bed regeneration of spent FCC catalyst in a single vessel. At least two isolated relatively dense phase fluidized beds are disposed beneath a common dilute phase region. Spent catalyst discharged into a primary regeneration stage is regenerated to produce flue gas and partially regenerated catalyst, which preferably overflows into the second stage. Flue gas and entrained catalyst from each fluidized bed are processed in two trains of separation means, preferably cyclones. The inlets of each train are disposed above the isolated fluidized beds, and are effectively separated although sharing an open dilute phase region.

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: An improvement in iso-olefin production without substantial decrease in overall yield is obtained in an integrated process combining a fluidized catalytic cracking reaction and a fluidized catalyst olefin interconversion reaction when crystalline medium pore shape selective zeolite catalyst particles are withdrawn in partially deactivated form from the interconversion reaction stage and added as part of the active catalyst in the FCC reaction.

Abstract: A process and apparatus for achieving hot catalyst stripping of spent FCC catalyst in a stripper mounted over a bubbling bed regenerator. Hot catalyst stripping is achieved by indirect transfer of heat from the regenerator to the stripper. Heat pipes, surface modifications such as fins on the stripper vessel, or use of a stripper in, or connective with, a heat exchange tube bundle may be used to heat spent catalyst with heat from the regenerator dilute phase, without transferring catalyst from the regenerator. The benefits of hotter catalyst stripping are achieved, without increasing catalyst traffic in the regenerator.

Abstract: A process and apparatus for fluidized bed catalyst regeneration. A mixture of spent catalyst, recycled hot regenerated catalyst and regeneration gas are charged to a riser having an outlet connective with a coke combustor immersed in a fluidized bed of catalyst. The coke combustor outlet is covered by the dense phase fluidized bed. Additional combustion air may be added to the fluidized bed of catalyst covering the coke combustor outlet for additional catalyst regeneration. Indirect heat exchange may heat spent catalyst in the riser and/or the coke combustor.

Abstract: A process and apparatus for high efficiency regeneration of spent FCC catalyst in an existing, single dense bed FCC regenerator is disclosed. Spent catalyst is added to a coke combustor immersed within the existing regenerator vessel catalyst bed. A dilute phase transport riser, above and connective with the coke combustor discharges a mixture of regenerated catalyst and flue gas. Regenerated catalyst collects around and under the coke combustor. The spent catalyst inlet, and combustion air inlet, are preferably immersed in, and in a heat exchange relationship with, the bed of hot regenerated catalyst. Heat pipes, or fins may be used to increase heat transfer into the coke combustor from the dense bed. Heating the coke combustor by indirect heat exchange, rather than recycle of hot regenerated catalyst, reduces particulates emissions and saves the energy needed to recycle catalyst in the regenerator.

Abstract: The use of lift gas for FCC risers is improved by the direct use of stripping vapors from a second stage of catalyst stripping as a lift gas. Reactor vapors recovered primarily from the stripping section of an FCC reactor/regenerator section provide an excellent source for lift gas material. These reactor vapors contain high concentrations of light paraffinic materials often with an equal weight percent amount of steam. The recovery of the stripping vapors independent from the product stream allows such gaseous mixtures to be readily used as lift gas. The lift gas material is obtained from a stripping section located subadjacent to a regenerator section so that it will have adequate pressure for use as a lift gas stream. The relatively high pressure of the lift gas stream eliminates processing requirements that would otherwise be necessary for the removal of particulate material and the compression of the gas to the pressure conditions at the bottom of the riser.

Abstract: A process and apparatus for achieving turbulent or fast fluidized bed regeneration of spent FCC catalyst in a bubbling bed regenerator having a stripper mounted over the regenerator and a stripped catalyst standpipe within the regenerator. A coke combustor vessel, which may be partially or totally open to the dilute phase above the bubbling bed, is added to the existing regenerator vessel. Spent catalyst is discharged into the coke combustor, regenerated in a turbulent or fast fluidized bed, then discharged into the dilute phase region above the bubbling bed, either via a deflector or by simply overflowing the combustor. Regeneration of catalyst is completed in the bubbling dense bed, and/or an annular fast fluidized bed surrounding the coke combustor. Catalyst may be recycled from the dense bed to the coke combustor either by a flow line, or by adjusting relative heights of bubbling to fast fluidized bed.

Abstract: A fluidized catalytic cracking process using a high efficiency regenerator comprising a coke combustor, a dilute phase transport riser, and a second fluidized bed with catalyst recirculation to the coke combustor, is operated to reduce NO.sub.x emissions in the regenerator flue gas. The amount of catalyst recirculation from the second fluidized bed to the coke combustor or combustion air addition or preferably both are adjusted based on continuous or periodic measurement of a process parameter of the FCC regenerator which directly or indirectly measures the NO.sub.x content of regenerator flue gas. Operation with restricted air or catalyst recirculation degrades coke combustor operation, shifts some regeneration to downstream portions of the regenerator, and reduces NO.sub.x emissions.

Abstract: The duty of a side-mounted, backmix type catalyst cooling zone is increasd by having one conduit that delivers catalyst to the top of the cooling zone and another conduit that uses fluidizing gas to vent catalyst from the top of the cooling zone back to a regenerator. The catalyst cooling zone is used to cool catalyst in a fluidized catalytic cracking process. The cooling zone comprises a heat exchanger located remote from an FCC regenerator that supplies hot catalyst particles to the cooling zone from a dense phase catalyst bed. Hot catalyst particles enter the top end of the cooling zone through a first conduit. Fluidizing gas, added to the cooling zone for backmixing and heat transfer purposes, exits the top of the cooling zone through a second conduit that communicates the top of the cooler with a dilute phase catalyst zone in the regenerator. Gas flow into and through the second conduit transports catalyst from the cooling zone to the regenerator.

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: A two-stage process and apparatus for the regeneration of fluidized catalytic cracking (FCC) catalyst is disclosed. A primary regenerator, a single dense bed with a spent catalyst inlet, a source of oxygen-containing gas, a flue gas outlet and a regenerated catalyst outlet, is supplemented with a secondary regenerator. The secondary regenerator has its own source of air for combustion and takes particles from a lower portion of the dense bed in the primary regenerator. Combustion gases, and some solids, are discharged from the secondary regenerator into the primary regenerator. Hot, decoked material is withdrawn from the base of the secondary regenerator for use in the catalytic cracking reaction. Preferably, a dense, fast settling additive is used with a conventionally sized FCC catalyst. These two materials can be added together to the primary regenerator and separated by elutriation therein into two catalyst phases.

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: A process and apparatus for fluidized bed combustion using a dense phase combustion zone over a dilute phase combustion zone. When used to regenerate FCC catalyst containing coke with relatively large amounts of NO.sub.x precursors, the catalyst is added to and partially regenerated in the dense phase zone and then falls down into the dilute phase zone. Most of the combustion air is added to the dilute phase and rises into and fluidizes the dense phase zone. NO.sub.x formed in the dilute phase is reduced to N.sub.2 in the dense phase.

Abstract: Disclosed is a method of and apparatus for reducing the level of extremely small catalyst particles ("fines") in an FCC system by temporarily retaining particles separated from the secondary cyclone separator in either a reactor vessel or catalyst regenerator. These particles can be withdrawn from the temporary retaining area, which takes them out of the active catalyst inventory within the reactor/regenerator system. The withdrawing of catalyst "fines" reduces the particulate contamination both in flue gas exhausted to the atmosphere from the catalyst regenerator and in the main column bottom (MCB) products from the fractionation stage. Preferred embodiments includes withdrawal of "fines" from either the regenerator or the reactor vessels and the secondary cyclones contained in each of these vessels.

Abstract: An improved process for regeneration of catalyst used in fluidized catalytic cracking of hydrocarbons using a cross-flow or swirl type catalyst regenerator is disclosed. Instead of a single catalyst withdrawal outlet for regenerated catalyst, multiple catalyst withdrawal points are provided. Use of multiple catalyst outlets, or a continuous radial catalyst outlet, greatly reduces stagnant regions in the bed. The process is useful in FCC units having inventories of from 10 to 100 tons of catalyst.

Abstract: A process and apparatus for controlled, multi-stage regeneration of FCC catalyst is disclosed. A modified high efficiency catalyst regenerator, with a fast fluidized bed coke combustor, dilute phase transport riser, and second fluidized bed regenerates the catalyst in at least two stages. The primary stage of regeneration is in the coke combustor. Second stage catalyst regeneration occurs in the second fluidized bed. The amount of combustion air added to both regeneration stages is set to maintain partial CO combustion in both stages. Controlled multi-stage regeneration reduces the steaming or deactivation of catalyst during regeneration, maximizes coke burning capacity of the regenerator, and minimizes or eliminates NOx emissions.

Abstract: A process for controlled, multi-stage regeneration of FCC catalyst is disclosed. A modified high efficiency catalyst regenerator, with a fast fluidized bed coke combustor, dilute phase transport riser, and second fluidized bed regenerates the catalyst in at least two stages. The primary stage of regeneration is in the coke combustor. Second stage catalyst regeneration occurs in the second fluidized bed. The amount of combustion air added to, and conditions in, the coke combustor are controlled to limit CO combustion, while the second stage of regeneration, in the second fluidized bed, achieves complete CO combustion. Controlled multi-stage regeneration reduces steaming or deactivation of catalyst during regeneration, increase coke burning capacity, and reduces NOx emissions.

Abstract: This invention makes possible substantially continuous flow of uniformly distributed hydrogen and hydrocarbon liquid across a densely packed catalyst bed to fill substantially the entire volume of a reactor vessel by introducing the fluids as alternate annular rings of gas and liquid at a rate insufficient to levitate the bed and with catalyst selected by a density, shape and size at a design feed rate of liquids and gas to prevent ebulation of the packed bed at the design feed rates. Catalysts are selected by measuring bed expansion in a large pilot plant run with hydrocarbon, hydrogen, and catalyst at the design pressures and flow velocities. The liquid and gas components of the feed flow into the bed in alternate annular rings across the full area of the bed.

Abstract: This invention relates to a process for the separation of fine catalyst particles from a hydrocarbon feedstock coming from a catalytic cracking unit by filtration through mineral barriers and a filtration loop.The process consists of filtering the feedstock through mineral barriers that are resistant to heat and have a porosity adapted to the minimum diameter of the particles to be retained. The porosity is generally between 0.1 and 100 microns.

Abstract: A process for simultaneously heating and cooling of spent FCC catalyst during regeneration in a high efficiency FCC regenerator, one using a fast fluidized bed coke combustor. The coke combustor burns coke from spent catalyst in a turbulent or fast fluidized bed, and discharges catalyst and flue gas up into a dilute phase transport riser. Catalyst is separated into flue gas and a bubbling dense bed of catalyst. The coke combustor is heated by recycling hot catalyst from the bubbling dense bed and simultaneously cooled by a backmixed heat exchanger. Catalyst flows from the combustor to the cooler and is displaced back into the combustor by adding air to the catalyst in the cooler. Heating promotes rapid coke combustion, while cooling reduces thermal and hydrothermal deactivation of the spent catalyst.

Abstract: A method and apparatus are disclosed to reduce the amount of unstripped hydrocarbon flowing to the regenerator in an FCC unit. The catalyst stripper section is heated by indirect heat exchange with a mixture of hot regenerator flue gas and regenerated catalyst.

Abstract: Operational flexibility of a fluid catalytic cracking process is improved by directly cooling regenerated catalyst in an external catalyst cooler/stripper (ECCS). Regenerated catalyst withdrawn from the catalytic cracking unit regenerator is mixed with spent catalyst from the reactor stripper to effect desorption of cracked products from the spent catalyst at elevated temperature. The catalyst mixture is then contacted with an alkane-containing feedstream in a fluid bed maintained within a central section of the external catalyst cooler/stripper (ECCS). The mixture of spent and regenerated catalyst, cooled by the endothermic dehydrogenation of the alkanes, then flows downward through the ECCS to a lower section of the ECCS where the catalyst is countercurrently stripped with steam to remove remaining entrained hydrocarbons. Steam is withdrawn from an upper section of the steam stripping zone and bypassed around the dehydrogenation/stripping and mixing stages to avoid steam deactivation of the catalyst.

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: Disclosed is a method and apparatus for fluid catalytic cracking (FCC). The output of a reactor riser zone is fed to a riser cyclone separator, a primary cyclone separator, and secondary cyclone separators, connected in series within a single reactor vessel. The riser cyclone separator is connected to the primary cyclone separator by a conduit, which prevents random post-riser thermal cracking of the hydrocarbons after they exit the riser cyclone separator. The conduit contains an annular port to allow strippping gas to enter the conduit to improve the separator of hydrocarbons from catalyst. Catalyst separated in the riser cyclone separator drops through a riser cyclone dipleg and passes through a dipleg seal which comprises a seal pot or catalyst held around the dipleg. The conduit is formed by two overlapping parts, one having a larger diameter than the other to form the annular port and packing or spacers may be used to align and space the overlapping parts.

Abstract: The invention relates to an installation for the fluidized-bed cracking of a hydrocarbon feedstock.In accordance with the invention recycling of the regenerated catalyst particles to the intake of the reactor comprise, from upstream to downstream, a preferably substantially vertical pipe (1) for the discharge of the regenerated particles from the regenerator, and a substantially straight pipe (2) connected to the vertical pipe (1) and sloping downward therefrom to the base (3) of the reactor to which it is connected, the downward-sloping pipe (2) being connected to the vertical pipe (1) and to the base (3) of the reactor through inward-curved portions or elbows which impose neither a sharp change in direction on the course of the particles nor sudden changes in the diameter of the pipes.

Abstract: A process and apparatus are disclosed for achieving turbulent or fast fluidized bed regeneration of spent FCC catalyst in a bubbling bed regenerator having a stripper mounted over the regenerator and a stripped catalyst standpipe within the regenerator. A closed coke combustor vessel is added alongside an existing regenerator vessel, and spent catalyst is discharged into a transfer pot beneath the existing dense bed, then into the coke combustor. Catalyst is regenerated in a turbulent or fast fluidized bed, and discharged into the dilute phase region above the existing bubbling dense bed. The discharge line preferably encompasses, and is in a heat exchange relationship with, the spent catalyst standpipe. Discharge catalyst is collected in the bubbling dense bed surrounding the coke combustor, and may be given an additional stage of regeneration. Catalyst may be recycled from the dense bed to the transfer pot.

Abstract: A process and apparatus for achieving multistage, hot catalyst stripping of spent FCC catalyst in a bubbling bed regenerator having a stripper mounted over the regenerator and a stripped catalyst standpipe within the regenerator. Hot catalyst stripping is achieved by lifting regenerated catalyst into the conventional stripper or to a secondary catalyst stripper under the primary stripper. Spent catalyst is heated by direct contact heat exchange with hot regenerated catalyst. Three different types of lift gas may be used to transport catalyst from the regenerator to the hot stripper, a light reactive hydrocarbon, an inert, or steam.

Abstract: Disclosed is a method and apparatus for fluid catalytic cracking (FCC). The output of a reactor riser zone is fed to a riser cyclone separator, a primary cyclone separator, and secondary cyclone separators, connected in series within a single reactor vessel. The riser cyclone separator is connected to the primary cyclone separator by a conduit, which prevents random post-riser thermal cracking of the hydrocarbons after they exit the riser cyclone separator. The conduit contains an annular port to allow stripping gas to enter the conduit to improve the separation of hydrocarbons from catalyst. Catalyst separated in the riser cyclone separator drops through a riser cyclone dipleg and passes through a dipleg seal which comprises a seal pot or catalyst held around the dipleg. The conduit is formed by two overlapping parts, one having a larger diameter than the other to form the annular port and packing or spacers may be used to align and space the overlapping parts.

Abstract: Oxides of nitrogen (NO.sub.x) emissions from an FCC regenerator are reduced by adding a DeNO.sub.x catalyst to the FCC regenerator in a form whereby the DeNO.sub.x catalyst remains segregated within the FCC regenerator. This permits use of a DeNO.sub.x catalyst without regard to the effect of the DeNO.sub.x catalyst on the catalytic cracking reaction. Floating hollow spheres, or catalyst fines, containing the DeNO.sub.x catalyst are preferred.

Abstract: A process and apparatus are disclosed for achieving turbulent or fast fluidized bed regeneration of spent FCC catalyst in a bubbling bed regenerator having a stripper mounted over the regenerator and a stripped catalyst standpipe within the regenerator. A coke combustor vessel is immersed in, and in open fluid communication with, the bubbling dense bed of the existing regenerator vessel. Spent catalyst is discharged into the coke combustor, mixes with hot regenerated catalyst which flows into the coke combustor, and regenerated with combustion air in a turbulent or fast fluidized bed. Catalyst and flue gas are discharged up into a dilute phase transport riser, preferably into cyclone which separate hot regenerated catalyst from flue gas. Regenerated catalyst is collected in the bubbling dense bed surrounding the coke combustor, and some is recycled by flowing into the coke combustor for direct contact heat exchange.

Abstract: A process and apparatus for achieving multistage, hot catalyst stripping of spent FCC catalyst in a bubbling bed regenerator having a stripper mounted over the regenerator and a stripped catalyst standpipe within the regenerator. A secondary or hot catalyst stripper is placed under the primary stripper and within the existing regenerator vessel. Spent catalyst from the primary stripper is heated in the secondary stripper by at least one of immersion in the bubbling dense bed of hot regenerated catalyst, addition of hot regenerated catalyst recovered from the discharged into the coke combustor and regenerated in a turbulent or fast fluidized bed, and discharged up into a dilute phase transport riser which preferably encompasses, and is in a countercurrent heat exchange relationship with, the spent catalyst standpipe. Regenerated catalyst is discharged from the dilute phase transport riser, and collected in the bubbling dense bed surrounding the coke combustor.

Abstract: A process for converting residual oil comprising vacuum bottoms in the presence of a cracking catalyst of high surface area and comprising an ultrastable zeolite is described. More particularly, a conversion process particularly contributing to producing cycle oil and gasoline boiling range products with reduced carbon deposition in combination with a relatively high regeneration temperature operation of at least 1350.degree. F. and above, and a short contact time riser hydrocarbon conversion operation contributing to reducing slurry oil product in favor of lower boiling products is described. A fluid cracking catalyst comprising a special ultrastable crystalline zeolite of high silica to alumina ratio provides hydrothermal stability of acceptable tolerance in the environment employed.