Abstract: A catalyst regeneration apparatus for the oxidation of coke from a spent catalyst and for the conversion of carbon monoxide resulting from the oxidation of coke to carbon monoxide.

Abstract: An apparatus for catalytically cracking hydrocarbons comprising a riser reactor having a plurality of catalyst injectors positioned along the length thereof. Adjacent to and upstream of certain of the catalyst injectors, cyclone separators are connected to the reactor so that fluid which contains a partially converted or cracked hydrocarbon and catalyst pass therethrough for separating the catalyst from the fluid with the fluid being returned to the reactor. Fresh catalyst is introduced into the fluid after same exits the separator to continue the cracking process. Steam can also be introduced into the reactor adjacent the catalyst injectors.

Abstract: A fluid cat cracker process and apparatus including at least one shutoff valve having improved valve stem guide apparatus. The valve stem guide apparatus comprises a guide member adapted to be attached within the valve body through which the valve stem is disposed. A plurality of annular grooves positioned one above the other are provided in the interior of the guide member and a plurality of expansible seal rings are disposed in the grooves. The seal rings are of a size and shape such that a seal is provided between the valve stem and the surfaces of the grooves whereby pressurized materials within the valve body are prevented from flowing through the valve stem guide apparatus.

Abstract: An apparatus for the oxidation of coke from a spent catalyst at a controlled temperature and for the essentially complete conversion of carbon monoxide resulting from the oxidation of coke to produce regenerated catalyst and spent regeneration gas.

Abstract: Flue gas containing CO.sub.2 and CO from a fluidized cracking unit catalyst regenerator is fed to a combustor in which CO combustion is completed. The CO combustion can be enhanced by injection of air or oxygen-containing gas into the combustor. The combustor may include CO combustion promoters such as oxidation-promoting catalyst grids, and may also include auxiliary fuel injection or other means to initiate or facilitate the combustion. The process of this invention further comprises indirect or direct recovery of the heat resulting from the combustion of CO in the flue gas by the cracking catalyst particles, which may be returned separately to the regenerator bed or transferred to the cracking reactor with or without fresh catalyst, or may be recycled to the CO combustor inlet or combined with other catalyst particles passing to the regenerator.

Abstract: Steam coils having two different pressure levels are provided in a bed of carbon-contaminated catalyst undergoing regeneration by combustion with an oxygen-containing gas to control the temperature.

Abstract: An improved method for the regeneration of catalytic cracking catalyst wherein a regeneration flue gas having a reduced concentration of carbon monoxide, preferably less than 0.05 vol. %, and a regenerated catalyst having a reduced residual carbon content, preferably less than 0.1 wt. %, are obtained by first burning coke from the coke-contaminated catayst at an elevated temperature such that when the coke burned is substantially completely converted to carbon dioxide, the temperature of the fluidized bed in the regeneration zone may then be reduced to a desired operating level while maintaining substantially complete conversion of the carbon to carbon dioxide. This is accomplished by regulating the amount of coke deposited on the catalyst in the reaction zone and adjusting the catalyst circulation rate. Effluent gas from the regeneration zone may be discharged directly to the atmosphere with no discernible effect upon ambient air quality.

Abstract: In the catalytic cracking of oil, especially in a riser-type of transport pipe reactor, feedstock in the liquid state is added to the reactor together with sufficient regenerated catalyst to effect essentially complete vaporization of the oil but with minimum cracking. Preferably the regenerated catalyst is cooled to about 900.degree. to 1100.degree. F prior to contact with the oil. The mixture of oil and catalyst is propelled through the riser until the oil is substantially vaporized and then a major portion of hot regenerated catalyst is added to effect the cracking reaction.

Abstract: Process and apparatus for hydrocarbon conversion, such as, fluid catalytic cracking, in which finely divided catalyst is circulated from a catalyst regeneration vessel through a standpipe connected by an angle bend to a vertically inclined conduit which in turn is connected to a straight vertical transferline riser reaction zone into a gas-solids disengaging and stripping vessel without the necessity of a variable orifice flow control valve. Separated spent and stripped catalyst flows from the disengaging-stripping vessel to the regeneration vessel through an external conduit.

Abstract: In a fluid catalytic cracking unit utilizing a zeolite cracking catalyst and employing a multiplicity of elongated reaction zones or risers, significant improvements are obtained by introducing a light gas oil to at least one elongated reaction zone and a heavier gas oil to at least one other elongated reaction zone. Optionally, the vaporous effluent from either or both elongated reaction zones may be subjected to further cracking in the dense phase of catalyst in the reactor vessel. Operating conditions within the elongated reaction zones are established to permit the conversion of the heavier gas oil to be 0-30 volume percent lower than the light gas oil. Higher yields of higher octane gasoline are obtained where the unit is operated in the disclosed manner.

Abstract: In a fluidized cracking unit, the cracking catalyst regeneration vessel is specially adapted for high temperature operation to permit essentially complete combustion of coke on the spent catalyst particles and, in addition, the essentially complete combustion of carbon monoxide produced thereby, within the dense phase zone of the regenerator. A partition in the regenerator divides the lower dense phase zone operating at high temperatures from the upper dilute phase zone which may be cooled, for instance, by boiler tubes, water sprays and the like. The partition contains one or more rough separation catalyst knock-out means such as cyclone separators whereby hot catalyst particles are separated from the rising combusted gases and returned to the dense phase regeneration zone. In one embodiment, the regeneration vessel is elongated to facilitate recovery of most of the extra heat produced by complete carbon monoxide combustion by the catalyst particles returning to the dense phase zone.

Abstract: This invention relates to a process for catalytically cracking hydrocarbon feedstocks containing a contaminant deleterious to the process and catalyst and to a method for removing the contaminant from a crystalline aluminosilicate cracking catalyst used in the process, where the contaminant is vanadium, or vanadium and nickel, and optionally iron.

Abstract: A refinery process is described for converting desalted full range crude oils and syncrudes derived from coal, shale and tar sands. The process involves mixing and reacting the full range heavy oil feed with a low molecular weight carbon-hydrogen fragment contributor such as methanol or C.sub.2 -C.sub.5 olefins in the presence of a fluid zeolite cracking catalyst comprising mordenite.

Abstract: In fluidized bed regeneration of carbon-contaminated catalysts, such as cracking catalysts, wherein at least a portion of the oxygen-containing gas required for fluidization and burn-off of carbon deposits is introduced as a separate stream into the dense phase of the fluidized catalyst, contained in the regeneration chamber, by means of a plurality of gas discharge nozzles, affixed to at least one manifold member substantially horizontally disposed at the lower end of the regeneration chamber, catalyst attrition is reduced and backflow of catalyst particles into the nozzles is minimized by utilizing gas discharges which are restricted in internal cross-sectional area in their upstream portion connected to the manifold member and expanded in the internal cross-sectional area of their downstream portion such that (a) the numerical ratio of the difference between diameter of the downstream portion and the diameter of the upstream portion divided by the length of the downstream portion taken in the direction of

Abstract: A fluid catalytic cracking - catalyst regeneration system is described wherein regeneration of a crystalline zeolite hydrocarbon conversion catalyst is accomplished at an elevated temperature in the presence of regenerated catalyst mixed therewith in the upper portion of a bed of regenerated catalyst with the mix ratio controlled as a function of the amount of primary regeneration gas introduced to a lower portion of the bed of regenerated catalyst.

Abstract: An improved method is disclosed for controlling the temperature of the fluidized dense catalyst phase of the regeneration zone in a fluid catalytic cracking unit, wherein the coke laydown in the reaction zone is at a level such that the coke concentration of the partially deactivated catalyst from the reaction zone is not sufficient to provide the heat required to maintain the controlled temperature in the fluidized dense catalyst phase of the regeneration zone. In this method, torch oil is added to the partially deactivated catalyst in the spent catalyst transfer line in an amount such that the catalyst charged to the regeneration zone contains sufficient combustible material to provide the heat necessary to maintain the fluidized dense catalyst phase of the regeneration zone at the controlled temperature.

Abstract: A fluidized catalytic cracking process wherein the reaction zone comprises one or more riser reaction conduits discharging into a reaction vessel. Hydrocarbon vapors and catalyst discharging from the risers separate to form a dense phase fluidized catalyst bed and a hydrocarbon vapor phase within the reaction vessel. A selected weight inventory of catalyst is maintained in the reaction vessel dense phase catalyst bed by valve means responsive to the weight of catalyst. Conversion of hydrocarbon in the reaction vessel may be increased by reducing the dense phase catalyst bed bulk density and consequently increasing contact of catalyst with hydrocarbon vapor within the reaction vessel.

Abstract: The specific disclosure is directed to a catalytic cracking model wherein the reactant and product species are lumped according to molecular type and boiling range. The specific invariant lumping scheme includes paraffins, naphthenes, aromatic rings, and aromatic substituent groups.

Abstract: Regeneration of spent catalyst contaminated by a carbonaceous deposit is conducted by contacting the spent catalyst with a hot flue gas emanating from a first dense phase regeneration zone. The heated spent catalyst is then contacted countercurrently with an oxygen-containing gas in the first dense phase regeneration zone to produce partially regenerated catalyst which is subsequently contacted concurrently with an oxygen-containing gas in a second dense phase regeneration zone. The regenerator includes a standpipe section disposed within the regeneration vessel in concentric relation to the vertical axis thereof with a cylindrical baffle disposed around an upper portion of the standpipe section. The baffle has at least one orifice at its lower portion for direct passage of catalyst from the fluidized bed into the annular zone between the baffle and the standpipe.

Abstract: A transport type fluid catalytic cracking reactor comprising a riser conduit, a flow reversal means and a downcomer conduit, wherein the flow reversal means has a closable top such that a shorter or longer residence time of catalyst and oil vapor in the transport reactor may be selected without affecting vapor velocity within the riser conduit. Also, a process employing such transport reactor.

Abstract: A transport type fluid catalytic cracking reactor comprising a riser conduit, a flow reversal means and a downcomer conduit, wherein the flow reversal means has a closable top such that a shorter or longer residence time of catalyst and oil vapor in the transport reactor may be selected without affecting vapor velocity within the riser conduit.

Abstract: The apparatus comprises in combination and particular arrangement a spent-catalyst receiving chamber for containing a dense-bed of fluidized catalyst in which chamber spent catalyst is oxidized to produce regenerated catalyst and partially spent regeneration gas; a transfer conduit through which said gas and said catalyst pass and in which carbon monoxide is essentially completely converted to carbon dioxide to produce spent regeneration gas and regenerated catalyst at an increased temperature; a regenerated-catalyst receiving chamber for containing a dense-bed of regenerated catalyst and in which spent regeneration gas and regenerated catalyst are separated; and, a regenerated-catalyst recycle means by which hot regenerated catalyst can be recycled within the apparatus from the regenerated-catalyst receiving chamber to the spent-catalyst receiving chamber in amounts to control the temperature and hence the rate of coke oxidation in the spent-catalyst receiving chamber.