Abstract: Apparatus for regeneration of spent, coke contaminated fluidized cracking catalyst by burning coke therefrom with a molecular oxygen containing regeneration gas in a fluidized dense phase bed, and for burning substantially all carbon monoxide to carbon dioxide. Means are provided for transferring heat from the top of said regeneration apparatus to the bottom, employing catalyst as the transfer medium. Additionally, means are provided for maintaining a homogeneous fluidized dense phase bed of catalyst undergoing regeneration.

Abstract: A process is described herein for regeneration of spent, coke contaminated fluidized cracking catalyst by burning coke therefrom with a molecular oxygen containing regeneration gas in a fluidized dense phase bed, and for burning substantially all carbon monoxide formed to carbon dioxide. A method is provided for supplying additional oxygen to a dilute phase above the dense phase bed for combustion of carbon monoxide. Additionally, a method is provided for transferring heat from the dilute phase back to the bottom of the fluidized dense phase bed.

Abstract: A process is described herein for regeneration of spent, coke contaminated fluidized cracking catalyst by burning coke therefrom with a molecular oxygen containing regeneration gas in a fluidized dense phase bed, and for burning substantially all carbon monoxide formed to carbon dioxide. A method is provided for balancing oxygen concentration across the cross-sectional area of the dense phase bed, as is a method for supplying additional oxygen above the dense phase bed for combustion of carbon monoxide. Additionally, a method is provided for transferring heat from a dilute phase back to the fluidized dense phase bed.

Abstract: A liquid phase alkylation process for production of alkylate useful as motor fuel, wherein low molecular weight isoparaffin hydrocarbons are alkylated with olefin hydrocarbons in the presence of a catalyst, comprising a mixture of a major portion of sulfuric acid (H.sub.2 SO.sub.4) with a minor portion of trifluoromethane sulfonic acid (CF.sub.3 SO.sub.3 H) which may contain about 0-3 weight percent water and about 0-10 weight percent acid oils.

Abstract: Apparatus for regeneration of spent, coke contaminated fluidized cracking catalyst by burning coke therefrom with a molecular oxygen containing regeneration gas in a fluidized dense phase bed, and for burning substantially all carbon monoxide to carbon dioxide. Means are provided for transferring heat from the top to the bottom of the regeneration apparatus, employing catalyst as the transfer medium. Also, conical standpipe means is provided for deaerating regenerated catalyst.

Abstract: Apparatus for regeneration of spent, coke contaminated fluidized cracking catalyst by burning coke therefrom with a molecular oxygen containing regeneration gas in a fluidized dense phase bed, and for burning substantially all carbon monoxide to carbon dioxide. Means are provided for transferring heat from the top of said regeneration apparatus to the bottom, employing catalyst as the transfer medium. Additionally, means are provided for maintaining a homogeneous fluidized dense phase bed of catalyst undergoing regeneration. Also, conical standpipe means is provided for deaerating regenerated catalyst.

Abstract: A process for removal of fluoride compounds from spent alkylation catalyst containing fluorosulfonic acid and sulfuric acid wherein said spent catalyst is hydrolyzed in the presence of water, at subatmospheric pressure in a vacuum digestion zone for conversion of a major portion of fluorosulfonic acid to hydrogen fluoride, wherein said hydrogen fluoride is removed from the vacuum digestion zone as a vapor, and wherein the remaining sulfuric acid rich liquid fraction of the spent catalyst is treated with silica-alumina cracking catalyst for removal of most of the remaining residual fluoride compounds for providing a sulfuric acid effluent substantially free of fluoride compounds. The hydrogen fluoride recovered is reacted with sulfur trioxide to form fresh fluorosulfonic acid which is combined with sulfuric acid to provide fresh alkylation catalyst.

Abstract: The present application discloses a fluidized catalytic cracking process wherein light cycle gas oil is stripped of heavy naphtha components employing reboiled light cycle gas oil as stripping vapor. Heavy naphtha vapors stripped from the light cycle gas oil are returned to the reaction vapor as primary stripping vapor. This process results in increased naphtha octanes, and reduced sour water production from a fluidized catalytic cracking unit.

Abstract: The present application discloses a fluidized catalytic cracking process wherein intermediate cycle gas oil is stripped of light cycle gas oil components employing reboiled intermediate cycle gas oil as stripping vapor for improving light cycle gas oil yield, reducing feed preheat requirements, and reducing sour water production from a fluidized catalytic cracking unit.

Abstract: Improved alkylation reactor and reaction emulsion phase separation apparatus is described. Such apparatus is particularly useful in sulfuric acid catalyzed alkylation of isoparaffin with olefins for production of high octane value alkylate.

Abstract: Pyrolysis naphtha is contacted with a residuum hydrocarbon charge stock under process conditions suitable for delayed coking of said residuum hydrocarbon charge. Unstable olefinic and diolefinic components of said pyrolysis naphtha are reduced in the product naphtha. Such conversion of unstable olefin and diolefin components is accomplished without substantial conversion of aromatic components of said pyrolysis naphtha.

Abstract: A liquid phase alkylation process for production of alkylate useful as motor fuel, wherein low molecular weight isoparaffin hydrocarbons are alkylated with olefin hydrocarbons in the presence of a catalyst comprising HFSO.sub.3 and H.sub.2 SO.sub.4 in weight ratio of from about 0.11 to 1 to about 0.32 to 1, respectively, having a titratable acidity in the range of 16.5 to 21 milliequivalents per gram, and which may contain about 0-3 weight percent water and about 0-10 weight percent acid oils.

Abstract: Foul water streams from refining processes such as fluidized catalytic cracking, containing about 1-100 ppm metal cyanide complex compounds, are contacted with flue gas from combustion of hydrocarbonaceous fuels at temperatures of 750.degree. F and higher for essentially complete decomposition of cyanide radicals.

Abstract: A strong acid catalyzed alkylation process wherein an isoparaffin is alkylated with an alkylating agent such as olefin hydrocarbon and alkyl sulfates, in the liquid phase, at a superatmospheric pressure and a temperature in the range of from below zero to about 100.degree.F, employing a liquid catalyst consisting essentially of about 98.5 to about 88 weight percent of an acid selected from H.sub. 2 SO.sub.4, HFSO.sub.3, and mixtures thereof, about 0.5 to about 8 weight percent acid oils, about 0 to about 6 weight percent water, and having at least about 0.1 weight percent carbon dioxide dissolved therein.

Abstract: A process for removal of fluoride compounds from spent alkylation catalyst containing fluorosulfonic acid and sulfuric acid wherein hydrogen fluoride and fluorosulfonic acid, in the presence of water, are removed by vacuum distillation following which the remaining sulfuric acid rich fraction of the spent catalyst is reacted with a silica containing material to convert most of the remaining residual hydrogen fluoride to silicon fluoride which is volatilized from the mixture to thereby provide a sulfuric acid effluent free of substantial amounts of fluoride compounds. The hydrogen fluoride recovered is reacted with sulfur trioxide to form fresh fluorosulfonic acid which is combined with sulfuric acid to provide fresh alkylation catalyst.

Abstract: A liquid phase alkylation process for production of alkylate useful as motor fuel, wherein low molecular weight isoparaffin hydrocarbons are alkylated with olefin hydrocarbons in the presence of a catalyst, comprising a mixture of a major portion of sulfuric acid (H.sub.2 SO.sub.4) with a minor portion of trifluoromethane sulfonic acid (CF.sub.3 SO.sub.3 H) which may contain about 0-3 weight percent water and about 0-10 weight percent acid oils.

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: 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.