Abstract: A cyclic, fluidized catalytic cracking process providing reduced emissions of noxious effluents in regeneration zone flue gases is operated with homogeneous or non-homogeneous, regenerable, fluidized, solid particles which are circulated throughout the catalytic cracking process cycle and which comprise (1) a molecular sieve-type cracking catalyst, comprising a cracking catalyst matrix containing crystalline aluminosilicate distributed throughout said matrix and (2) a metallic reactant which reacts with sulfur oxides in the regeneration zone.

Abstract: A method for initiating essentially complete oxidation of carbon monoxide, resulting from the oxidative removal of coke from spent FCC catalyst, to carbon monoxide in a dense-phase bed of catalyst maintained in a regeneration zone. Coke is oxidized at first oxidizing conditions including a temperature of from about 750.degree. F. to about 1250.degree. F. to produce partially spent regeneration gas and regenerated catalyst having a first carbon content. The essentially complete oxidation of carbon monoxide is initiated by: (a) increasing the coke on regenerated catalyst from the first carbon content to a second carbon content and then (b) passing to the dense bed fresh regeneration gas at a flow rate at least stoichiometrically sufficient to produce regenerated catalyst having a third carbon content, less than the first carbon content, and sufficient to produce spent regeneration gas.

Abstract: A reactor that consists of a single shell that contains a reaction zone and a regeneration zone. The reaction zone and regeneration zone are arranged in such a manner that (a) a particulate solid may be transferred by flow of gases from the regeneration zone to the reaction zone by a first route and then back to the regeneration zone by a second route; and (b) the gases passing through the regeneration zone are not transferred to the reaction zone and the gases passing through the reaction zone are not transferred to the regeneration zone.

Abstract: By manipulating the degree of stripping of the used or spent catalyst leaving the cracker, the afterburning in a regenerator is controlled both efficiently and rapidly.

Abstract: A method for regenerating a coke-contaminated cracking catalyst with the simultaneous carefully controlled catalyzed combustion of CO to CO.sub.2 within a regeneration zone to produce regenerated catalyst and flue gas. Novel features of the method include adding to the regeneration zone, independently of the cracking catalyst, a supported CO oxidation promoter and combusting CO to CO.sub.2 in the presence of the promoter and regenerated catalyst. A supported oxidation promoter may be added to the regeneration zone in amounts to control the CO concentration in the flue gas, a regeneration zone temperature, or the residual carbon concentration on regenerated catalyst.

Abstract: Oil shale is pyrolyzed by introducing an oil shale feed to a retorting zone fluidized bed to yield, as products of retorting, retorted oil shale containing residual carbonaceous material and volatilized hydrocarbons. The retorted oil shale particles are passed to the top of a combustion zone fluidized bed into which a gaseous source of oxygen is introduced for fluidizing the combustion zone fluidized bed and oxidizing residual carbonaceous material contained in the retorted oil shale particles to yield combustion gases for fluidizing the retorting zone fluidized bed and for maintaining the retorting zone fluidized bed at a temperature sufficient to retort oil shale.

Abstract: A metal combustion promoter is introduced into the circulating inventory of catalyst in the catalytic cracking process to temporarily change the operating mode of the regenerator and decrease the CO content of the flue gas, thus permitting temporary shutdown of the CO-boiler or CO-incinerator, while continuing operation of the catalytic cracking process. The metal combustion promoters are compounds of platinum, iridium, osmium, palladium, rhodium, ruthenium, or rhenium. The described technique permits rapid shutdown and minimizes the time of operation outside of compliance with local or other ordinances.

Abstract: A cyclic fluidized catalytic cracking process is operated with a cracking catalyst which is modified with one or more metal oxides capable of reacting with sulfur oxides in the regeneration zone wherein the catalyst is regenerated under conditions which result in substantially complete conversion of carbon monoxide to carbon dioxide. Tail gases and flue gases from refinery furnaces which contain carbon monoxide and sulfur oxides are conveyed to the regeneration zone where they are scrubbed by the modified catalyst. The sulfur oxides are absorbed and the carbon monoxide is converted to carbon dioxide in the regeneration zone.

Abstract: Apparatus for the regeneration of fluidized solid catalyst including a regeneration chamber adapted to hold a fluidized solids bed, oxygen containing gas source communicating with the chamber, a tangential inlet communicating with the regeneration chamber to impart a swirling motion to spent catalyst entering the regeneration chamber and a free standing drawoff conduit disposed within the regeneration chamber, the drawoff conduit having an upper, open end in communication with the solids bed, the open end being formed by an obliquely truncated, outwardly flared portion of the conduit, the high portion of said truncated conduit lying closest the spent catalyst inlet.

Abstract: A cracking reactor is controlled in response to the proportion of heavy aromatic constituents in a feedstock to be cracked.

Abstract: A hydrocarbon conversion-catalyst regeneration system is described which particularly relies upon a fluidized catalyst regeneration operation arranged to restrict the catalyst inventory of the system by employing upflowing and downflowing fluid masses of catalyst in cooperative arrangement with one another providing a limited dispersed catalyst phase section and wherein the recycle of regenerated hot catalyst admixed with spent catalyst is controlled principally as a function of the pressure differential between the upflowing and downflowing catalyst masses.

Abstract: A hydrocarbon conversion-catalyst regeneration operation and apparatus required is described. Hot regenerated catalyst is mixed with spent catalyst in a first upflow annular fluid catalyst bed regeneration operation about a second concentric downflow fluid catalyst bed regeneration operation. Catalyst flow-through passageways pass catalyst from said downflowing catalyst bed operation to said upflow catalyst bed regeneration operation.

Abstract: A method and system is described for effecting chemical reactions of aliphatic hetero compounds to gasoline boiling components with crystalline zeolites in the presence of a relatively inert particle material arranged to exercise distribution of exothermic heat and utilized in a catalyst system under conditions to minimize undesired deactivation of catalyst particles.

Abstract: A method and system for cracking hydrocarbons with distinct fluid catalyst particles differing in activity, selectivity and physical characteristics is described wherein a common catalyst regeneration system is employed which will measurably contribute to the heat requirements of the operation as well as the activity/selectivity characteristics of the catalyst employed. Except for size, the catalysts upon make-up may have different or identical catalytic characteristics. However, upon contact with a particular hydrocarbon stream, such as vacuum resid, the selectivity and coke producing characteristics of the catalysts may be altered.

Abstract: A method for regenerating a coke-contaminated cracking catalyst with the simultaneous carefully controlled combustion of CO to CO.sub.2 within a regeneration zone to produce regenerated catalyst and flue gas. Novel features of the method include adding to the regeneration zone, independently of the cracking catalyst, a liquid comprising a soluble CO oxidation promoter selected from the group consisting of the noble metals and compounds thereof and combusting CO to CO.sub.2 in the presence of the promoter and regenerated catalyst. The liquid may be added to the regeneration zone in amounts to control the CO concentration in the flue gas, a regeneration zone temperature, or the residual carbon concentration on regenerated catalyst.

Abstract: An improved method for regenerating a catalytic cracking catalyst which comprises the steps of (1) increasing the temperature of the regeneration zone dense phase catalyst bed to a desired level above that normally employed during the regeneration so as to accelerate the rate of carbon conversion, (2) reducing the coke make in the reaction zone while maintaining the elevated temperature obtained in step (1) so as to increase the oxygen concentration in said regeneration zone so as to establish low levels of carbon monoxide in the flue gas and (3) reducing the temperature of the regeneration zone dense phase catalyst bed below the elevated temperature obtained in steps (1) and (2) while maintaining low levels of carbon monoxide in the flue gas. According to this invention, the flue gas may contain less than 0.05 volume %, preferably less than 0.02 volume %, carbon monoxide and, as such, may be discharged directly to the atmosphere with no discernable effect upon ambient air quality.

Abstract: A catalytic cracking process is provided in which entrained nitrogen is stripped from the regenerated cracking catalyst with a stripping gas comprising at least about 80 mole percent of carbon dioxide prior to contacting the hydrocarbonaceous feed with the regenerated catalyst.

Abstract: The activity maintenance of silica containing catalysts used in catalytic cracking operations is improved by the addition to the system of a silica containing compound or mixture which is in a form and in an amount that will readily vaporize in the steam added to or formed in the process. By the method of operation, the refiner is able to realize substantial savings in the amount of catalyst make-up required to maintain a given activity level in the unit.

Abstract: A hydrocarbon-feed distributor for injecting a hydrocarbon feed into contact with a fluidizable catalyst at conversion conditions in the lower end of the riser reactor conduit whereby wall temperatures within the conversion zone are reduced and overcracking of the hydrocarbon feed is minimized.

Abstract: In the fluid catalytic cracking process, improved adaptive behavior of the catalyst section with the regenerator operating in the complete CO-burning mode is achieved by including, as elements of control, variable preheat of the air feed and variable recycle of regenerated catalyst to spent catalyst. In response to excursions of the regenerated catalyst temperature, such as would be caused by change of feedstock, the air preheat temperature and recycle ratio are altered in a direction to restore the regenerated catalyst temperature to a predetermined value. The improved control system extends the useful control range, and it also diminishes counterproductive changes in severity induced by disturbances such as change of feedstock quality.

Abstract: A catalytic process for cracking of gas oil is disclosed, wherein trace amounts of metals of Periods 5 and 6 of Group VIII or rhenium is added to the total catalyst inventory so as to enhance significant conversion of the CO in the regenerator while maintaining the efficiency of the cracking reaction at high levels.

Abstract: A fluid catalytic cracking unit is controlled by sensing the reactor bed temperature and the riser temperature and by manipulating the flow of regenerated cracking catalyst into the riser responsive to these two temperature measurements. A gain function generator is utilized to compensate for the non-linear relationship between the change in valve position and change in riser temperature caused thereby.

Abstract: An improvement in the fluid cracking process is obtained by contacting the hydrocarbon feed in a riser reaction zone first with a recycled coke-containing spent catalyst and then contacting the resultant mixture with freshly regenerated catalyst to produce the desired conversion of the hydrocarbon feed and a coke-containing spent catalyst, a portion of the spent catalyst being recycled without regeneration to the inlet of the reaction zone and the remainder being regenerated and returned to an intermediate point in the reaction zone. The recycled coke-containing spent catalyst has sufficient activity so that the highly reactive nitrogen and carbon residue containing hydrocarbon contaminants in the oil feed will deposit on the spent catalyst and thus minimize the deactivation of the freshly regenerated catalyst used in the subsequent cracking of the oil feed.

Abstract: Non-hydrogenative endothermic catalytic cracking of hydrocarbon, particularly petroleum, fractions at relatively low pressures and high temperatures in a system where the endothermic heat required for cracking is supplied by catalyst as the heat transfer medium, which catalyst has been heated by burning coke deposited on the catalyst during cracking; and wherein a decomposable compound of platinum, palladium, ruthenium, iridium, osmium, rhodium or rhenium, is introduced into contact with the cracking catalyst during said process.

Abstract: In a fluidized catalytic cracking unit a riser discharge head for discharging catalyst and hydrocarbon vapor from a riser conduit substantially vertically downward into a vertical reaction vessel such that erosion of the discharge head and the reaction walls is avoided.

Abstract: Improved apparatus for carrying out catalytic chemical conversion and restoring the catalytic activity of solid particles previously used to promote chemical conversion involve improved devices to at least partially separate solid particles-vapor mixtures. These improved devices include, for example, properly positioned arresting vanes, flow reversal systems and/or plates, and provide for reduced attrition of the solid catalyst particles.Improved methods employing such apparatus are also disclosed.

Abstract: A process for producing gasoline which comprises cracking of a heavy petroleum feedstock in the presence of an alumino-silicate zeolite-containing catalyst maintained in a condition of an ascending flow at a temperature ranging from 480.degree. to 520.degree. C. and a mass velocity of said feedstock of from 6 to 40 hr.sup.-1 in the direction of said ascending flow with the formation of a reaction mixture containing gasoline, a fraction with a specific gravity of from 0.75 to 0.85 and a fraction with a specific gravity of from 0.85 to 0.95; the resulting reaction mixture is isolated from the catalyst and subjected to separation; said separated fractions are employed as recycle. The fraction with a specific gravity of from 0.75 to 0.85 is subjected to cracking in the presence of said catalyst which is in a condition of an ascending flow at a temperature of from 460.degree. to 520.degree. C. and a mass velocity of said fraction of from 6 to 40 hr.sup.-1 in the direction of said ascending flow.

Abstract: A catalytic process for cracking of gas oil is disclosed, wherein trace amounts of metals of Periods 5 and 6 of Group VIII or rhenium is added to the total catalyst inventory so as to enhance significant conversion of the CO in the regenerator while maintaining the efficiency of the cracking reaction at high levels.

Abstract: A catalyst regeneration process and apparatus for the oxidation of coke from a spent catalyst and for the conversion of CO resulting from the oxidation of coke to CO.sub.2.Novel feature of the process is the mixing of a portion of regenerated catalyst produced in a coke oxidation zone and heated to a higher temperature in a CO-conversion zone with spent catalyst and passing the mixture to a coke-oxidation zone to increase the temperature within the coke oxidation zone and to disperse spent catalyst more evenly across that zone thereby increasing the rate, extent and evenness of coke oxidation. The regeneration apparatus includes components by which this can be accomplished.

Abstract: Modifying a heat balanced operating fluid catalytic cracking (FCC) system to utilize a platinum group metal modified cracking catalyst, whereby increasing the heat generated in the exothermic regeneration of coked catalyst, and to provide a regenerated catalyst heat exchange cooler to permit adjustment of cracking conditions independent of the extra heat produced in the regeneration of catalyst.

Abstract: A fluid catalytic cracking process employing in combination a riser reaction zone and a CO-burning regeneration zone for the conversion of a feedstream comprising a residual oil to a distillate fuel.

Abstract: A metal combustion promoter is introduced into the circulating inventory of catalyst in the catalytic cracking process to temporarily change the operating mode of the regenerator and decrease the CO content of the flue gas, thus permitting temporary shutdown of the CO-boiler or CO-incinerator, while continuing operation of the catalytic cracking process. The metal combustion promoters are compounds of platinum, iridium, osmium, palladium, rhodium, ruthenium, or rhenium. The described technique permits rapid shutdown and minimizes the time of operation outside of compliance with local or other ordinances.

Abstract: The catalyst circulation rate in a fluid catalytic cracking process is regulated by using a low pressure drop valve means in the spent catalyst circuit of said process in conjunction with a control riser in said circuit. More particularly, a reduced catalyst circulation rate may be obtained in a fluid catalytic cracking process, the spent catalyst circulation rate in said process being controlled by the injection of variable amounts of a control gas into the control riser so as to cause density variations therein, by employing a low pressure drop valve means in the spent catalyst circuit of said process such that the pressure drop across said valve means reduces the pressure drop across the riser and consequently the density within said riser. The reduction in density within the riser results in a lowering of the catalyst circulation rate.

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 establishing a homogeneous dense phase fluidized bed of catalyst undergoing regeneration. Additionally, a method is provided for transferring heat from a dilute phase back to the fluidized dense phase catalyst bed.

Abstract: A hydrocarbon conversion-catalyst regeneration riser means system with interconnecting standpipes is described which relies upon catalyst separating and collecting vessels about the upper end of each riser means, means for contacting collected catalyst with gaseous material, standpipe means for passing collected catalyst in each vessel means to the lower portion of each riser means opposite from that from which obtained, a standpipe for passing collected regenerated catalyst directly to a lower bottom portion of said regeneration riser means and another standpipe for passing collected regenerated catalyst into the standpipe passing spent catalyst to the lower portion of the regeneration riser.

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: An apparatus for the oxidation of coke from a spent fluid catalytic cracking (FCC) catalyst and for the essentially complete conversion of carbon monoxide resulting from the oxidation of coke to produce regenerated catalyst and spent regeneration gas which 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; an internal regenerated-catalyst recycle means by which a portion of hot regenerated catalyst can be recycled from the transfer conduit to the spent-catalyst receiving chamber; a regenerated-catalyst receiving chamber for containing a dense-bed of regenerated catalyst and in which

Abstract: A fluid catalytic cracking process for simultaneously cracking a gas oil feed and upgrading a gasoline-range feed to produce high quality motor fuel. The gasoline-range feed is contacted with freshly regenerated catalyst in a relatively upstream portion of a short-time dilute-phase riser reaction zone maintained at first catalytic cracking conditions and the gas oil feed is contacted with used catalyst in a relatively downstream portion of the riser reaction zone which is maintained at second catalytic cracking conditions.Particularly suited to efficiently cracking a gas oil feed and upgrading a wide variety of gasoline-range feed, including the more refractory of such feeds, is a fluid catalytic cracking process comprising a short-time dilute-phase riser reaction zone and a regeneration zone in which CO, produced by the oxidation of coke, is essentially completely oxidized to CO.sub.2 and in which at least part of the heat of combustion is transferred to regenerated catalyst.

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 gas phase and a liquid phase pass countercurrently through a reaction vessel, and solid particles move from stage to stage in the reactor concurrently with either the liquid phase or the gas phase. In one embodiment of the invention the liquid phase is a hydrocarbon oil to be treated, for example, desulphurized, the gas phase is hydrogen, and the solid particles are hydrodesulphurization catalyst particles.

Abstract: Catalyst and hydrocarbon vapors are separated in a cyclone attached to the discharge of a riser cracking operation. The cyclone is modified to include a separate cyclonic stripping of catalyst separated from hydrocarbon vapors.

Abstract: An improved hydrocarbon catalytic cracking process which comprises introducing tin into the cracking zone so as to maintain a volume ratio of carbon dioxide to carbon monoxide in the gaseous effluent from the catalyst regeneration zone of at least 3.0.

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: A regenerator design and method are provided which rely upon a segmented regeneration gas distributor grid to vary regeneration gas flow upwardly through the bed of catalyst above. The design includes an expanding annular section formed by a curved vertically extending baffle positioned adjacent and downstream of the catalyst tangential inlet and a radical dilute phase baffle extending from slightly beneath the bed surface to above the cyclone inlets. The width of the dilute phase baffle is from the wall of the regenerator to the center thereof, and beyond the rim of the catalyst outlet. Further, all cyclone diplegs between the outlet and inlet should be positioned to discharge tangentially to the swirl.

Abstract: A hydrocarbon conversion-catalyst regeneration operation is described which relies upon a dense fluid catalyst bed superimposed by a dispersed catalyst phase operation to effect elevated temperature regeneration of the catalyst providing low CO levels less than 0.15 mol percent in the flue gas by mixing regenerated catalyst with spent catalyst to obtain an initial mix temperature of at least 1175.degree. F. before contact with oxygen containing regeneration gas. The ratio of regenerated to spent catalyst is restricted to within the range of 0.5 to 1.5 and the oxygen content through the dense and dispersed catalyst phase is selected to provide a discharged dispersed catalyst phase temperature of at least 1350.degree. F.

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: An apparatus for the oxidation of coke from an FCC spent catalyst is disclosed which 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; an internal regenerated catalyst recycle means by which a portion of hot regenerated catalyst can be recycled from the transfer conduit to the spent-catalyst receiving chamber; 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, an external regenerated-catalyst recycle means by which a portion of hot regenerated catalyst can be re

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: 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: An oxygen-containing gas distribution apparatus is dicslosed which can be employed in the fluidized bed regeneraton of carbon-contaminated catalysts, such as cracking catalysts.Said apparatus comprises a plurality of gas discharge nozzles affixed to at least one manifold member substantially horizontally disposed at the lower end of the regeneration chamber, said nozzles being 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 the 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 gas flow does not exceed 0.18 and b) the ratio of the diameter of the upstream portion to its length taken in direction of gas flow does not exceed 1.67.