Abstract: An arrangement for removing entrained catalyst particulates from a gas may include a pressure vessel, a filter assembly, and a dip leg. The pressure vessel may contain a fluidized bed of catalyst particulates suspended in the gas. Some of the gas and entrained catalyst particulates may be directed to the filter assembly where the entrained catalyst particulates are filtered from the gas by a filter medium. The catalyst particulates pass generally tangentially along a feed side of the filter medium, where they scour the feed side of the filter medium, and then pass into the dip tube which guides the catalyst particulates away from the filter medium.

Abstract: One exemplary embodiment can be a process for regenerating catalyst in a fluid catalytic cracking unit. Generally, the process includes providing a feed to a riser of a reaction vessel, and providing a stream to a distributor positioned within a void proximate to an inlet receiving unregenerated catalyst in a regenerator. The feed can include at least one of a gas oil, a vacuum gas oil, an atmospheric gas oil, a coker gas oil, a hydrotreated gas oil, a hydrocracker unconverted oil, and an atmospheric residue.

Abstract: This disclosure relates to a process for regenerating a catalyst composition, wherein the catalyst composition comprising a molecular sieve and at least 10 wt. % coke having a C/H molar ratio in the range of 0.26 to 5, the process comprising (a) contacting the catalyst composition with a first oxidative medium having oxygen and water at first conditions sufficient to form a first regenerated catalyst composition having at least 50 wt.

Abstract: One exemplary embodiment can be a process for regenerating catalyst in a fluid catalytic cracking unit. Generally, the process includes providing a feed to a riser of a reaction vessel, and providing a stream to a distributor positioned within a void proximate to an inlet receiving unregenerated catalyst in a regenerator. The feed can include at least one of a gas oil, a vacuum gas oil, an atmospheric gas oil, a coker gas oil, a hydrotreated gas oil, a hydrocracker unconverted oil, and an atmospheric residue.

Abstract: An improved spent catalyst regenerator which contains sub-troughs branching off from the main trough, distribution troughs which extend outward from the sides of the main trough and the sub-troughs, and downflow tubes extending downward from the bottom of the main trough and sub-troughs.

Abstract: In a hybrid vehicle, control is executed to operate an engine with fuel injection being performed, when an unexecuted percentage of catalyst degradation suppression control is equal to or greater than a threshold value of the unexecuted percentage, when a power storage percentage of a battery is equal to or greater than a threshold value of the power storage percentage and the battery is charging, and also when a vehicle speed is equal to or greater than a threshold value of the vehicle speed and a cumulative air amount is equal to or greater than a threshold value of the cumulative air amount, when a catalyst temperature is less than a first threshold temperature and equal to or greater than a second threshold temperature, when the catalyst temperature is equal to or greater than the first threshold temperature, when there is a braking request while the engine is operating.

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 combination of moving bed regeneration technology and CO oxidation technology is used in a novel moving bed regeneration apparatus containing an integral CO oxidation zone to solve the problem of regenerating a coke-containing catalyst that does not contain a CO oxidation promoter without generating an effluent flue gas stream containing hazardous and undesired amounts of CO. The CO oxidation zone is located in the flue gas collection zone within the moving bed regeneration apparatus and functions autogenously to eliminate the CO hazard by oxidizing CO to CO2 with a portion of the unreacted oxygen withdrawn from the coke combustion zone of the moving bed regeneration apparatus.

Abstract: A catalyst regenerator (100) has a first section (110) and a second section (120) and is operated such that carbon from a carbon-contaminated catalyst (140) is converted to carbon monoxide in the first section (110) and that carbon monoxide is converted to carbon dioxide in the second section (120). The residence time of the oxygen-containing gas in the first and second sections (110, 120) is regulated in preferred configurations by the shape (e.g., diameter) of the first and second sections (110, 120).

Abstract: Disclosed is an apparatus and process for disengaging regenerated catalyst from flue gas in a catalyst regenerator so as to avoid re-entrainment of catalyst that has settled into a bed in the catalyst regenerator using a disengaging device. A disengaging arm of the disengaging device has an outer shell that encloses the arm, an inner shell with a slot for allowing catalyst and flue gas to exit the arm and an outer baffle having a lower edge located below the opening in the outer wall. The baffle directs the catalyst and flue gas downwardly and limits radial flow. Catalyst and flue gas enter the disengaging arm through an opening in an outer wall of a riser section at a first superficial velocity and exits through a slot in a bottom of the disengaging arm at no more than 1.33 the first superficial velocity.

Abstract: A method for testing the performance of catalysts used for conversion of FCC regenerator gases comprises subjecting the catalyst simultaneously to a mixture of gases including an oxidizing gas and a reducing gas in more than one cycle in which the ratio of the oxidizing gas to the reducing gas varies over the time of the cycle. Test gases comprising O2, CO, CO2, steam, nitrogen-containing gases and sulfur-containing gases in which the ratio of O2 to CO varies over time for each cycle and in which the products of combustion formed during each cycle can be measured periodically over the cycle yields important data on the usefulness of the catalysts for treatment of regenerator flue gas.

Abstract: An improved spent catalyst regenerator which contains sub-troughs branching off from the main trough, distribution troughs which extend outward from the sides of the main trough and the sub-troughs, and downflow tubes extending downward from the bottom of the main trough and sub-troughs.

Abstract: An apparatus and process for regenerating cracking catalyst may include a regenerator, a distributor penetrating the bottom of the regenerator, a spent catalyst conduit, a return standpipe, and a recirculating standpipe, wherein the return standpipe and the recirculating standpipe are connected to the upper half of the regenerator. An apparatus for regenerating cracking catalyst may include a spent catalyst standpipe and a recirculation standpipe positioned on an inner side of the regenerator vessel.

Abstract: A regeneration process for olefin cracking reactor is presented. The process utilizes the nitrogen waste stream from an air separation plant and the partially combusted effluent stream from the olefin cracking reactor is used to heat the nitrogen waste stream. The control of the heating of the nitrogen waste stream can be achieved through redirection of a portion of the heat from combustion to generate steam.

Abstract: A hydrocarbon composition comprises at least 90 wt. % of C9 to C20 non-normal olefins, non-normal saturates or combinations thereof based on the weight of the hydrocarbon composition, at least 2 wt. % and not greater than 25 wt. % of C9 hydrocarbons based on the weight of the hydrocarbon composition, and less than 15 wt. % of C17+ hydrocarbons based on the weight of the hydrocarbon composition, wherein said hydrocarbon composition has a specific gravity at 15° C. of at least 0.730 and less than 0.775. The composition is produced by oligomerization of at least one C3 to C8 olefin and an olefinic recycle stream containing no more than 10 wt. % of C10+ non-normal olefins. The composition is useful in producing fuel blends, such as jet fuel and diesel fuel.

Abstract: A process for producing a hydrocarbon composition that comprises contacting a feed stream, that comprises at least one C3 to C8 olefin, and an olefinic recycle stream, that comprises a first olefinic recycle stream and no more than 10 wt % of C10+ non-normal olefins, with a molecular sieve catalyst in a reaction zone under olefin oligomerization conditions producing an oligomerization effluent stream; separating the oligomerization effluent stream to produce a first olefinic stream, that has a weight ratio of C4?/(C5-C8) molecules from about 0.8 to about 1.2 times the weight ratio of C4?/(C5-C8) molecules found in the oligomerization effluent stream, and a first hydrocarbon product stream, that comprises at least 1 wt % and no more than 30 wt % of C9 non-normal olefin; and splitting the first olefinic stream to produce the first olefinic recycle stream and a first purge stream.

Abstract: A hydrocarbon fluid composition that comprises species of at least two different carbon numbers, an aerobic biodegradability of greater than 40% at 28 days, a cetane number of less than 60, and a certain boiling point range; and a process for making the hydrocarbon fluid composition.

Abstract: A method for oxidizing carbon adsorbable organic compounds in a controlled manner within a bed of activated carbon. The bed of activated carbon is exposed to a source of molecular oxygen, such as air, and is controlled within a temperature range whereby the molecular oxygen is slowly oxidizing the activated carbon. Under this controlled set of conditions, the activated carbon will oxidize organic compounds present within the bed of activated carbon. This technique has widespread versatility for the controlled destruction of organic vapors and liquids by activated carbon and applications for the regeneration of spent activated carbons containing previously adsorbed organic compounds.

Abstract: The present invention provides a process for making an olefin product from an oxygenate feedstock which comprises: a) contacting the feedstock in a reaction zone with a catalyst comprising i) a molecular sieve having defined pore openings and ii) a CO oxidation metal, under conditions effective to convert the feedstock into an olefin product stream comprising C2–C3 olefins and to form carbonaceous deposits on the catalyst so as to provide a carbon-containing catalyst; b) contacting at least a portion of the carbon-containing catalyst with a regeneration medium comprising oxygen in a regeneration zone comprising a fluid bed regenerator having a dense fluid phase and a dilute fluid phase under conditions effective to obtain a regenerated catalyst portion, wherein the difference between the temperature of the dilute phase and the temperature of the dense phase is no greater than 100° C.; c) introducing said regenerated catalyst portion into said reaction zone; and d) repeating steps a)–c).

Abstract: Disclosed is an apparatus and process for prolonging the residence time of catalyst in a chamber for regenerating catalyst. Spent catalyst, perhaps from an FCC reactor, is introduced into a chamber of a regeneration vessel between lower and higher combustion gas distributors. The velocity of gas from the lower distributor is insufficient to entrain catalyst from the bed, and gas from the higher distributor when combined with gas rising from the lower distributor is sufficient to generate a fast fluidized flow condition. The second distributor elevates the location of the transition from turbulent bed to fast fluidized conditions.

Abstract: Compositions comprising a component containing (i) an acidic oxide support, (ii) an alkali metal and/or alkaline earth metal or mixtures thereof, (iii) a transition metal oxide having oxygen storage capability, and (iv) palladium promote CO combustion in FCC processes while minimizing the formation of NOx. The acidic oxide support preferably contains silica alumina. Ceria is the preferred oxygen storage oxide.

Abstract: The invention relates to a process and apparatus for controlling afterburning in the regenerator of a FCC unit. The process and apparatus inject steam into the dilute phase within a regenerator to promote combustion of carbon monoxide before it enters the regenerator cyclones, plenum, or flue gas transfer lines.

Abstract: The invention relates to a process and apparatus for controlling afterburning in the regenerator of a FCC unit. The process and apparatus inject steam into the dilute phase within a regenerator to promote combustion of carbon monoxide before it enters the regenerator cyclones, plenum, or flue gas transfer lines.

Abstract: Single-site catalyst systems useful for polymerizing olefins are disclosed. The catalyst systems comprise an organometallic complex and an activator. The complex includes a Group 3-10 transition metal, M, and at least one indenoindolyl ligand that is pi-bonded to M. The activator is a reaction product of an alkylaluminum compound and an organoboronic acid. Catalyst systems of the invention significantly outperform known catalyst systems that employ a metallocene complex and similar aluminoboronate activators.

Abstract: A process for regenerating a spent catalyst having coke deposits thereon in a catalyst regeneration vessel having a dense phase and a dilute phase, wherein the process comprises the steps of: (a) contacting the spent catalyst with a primary oxygen-containing gas in the dense phase, thereby combusting the coke, resulting in the formation of a combustion gas comprising nitrogen oxides and carbon monoxide which further reacts, thus reducing a majority of the nitrogen oxides to form elemental nitrogen; and (b) contacting the combustion gas with a secondary oxygen-containing gas, and typically a shield gas, at a location just above the interface between the dense phase and the dilute phase and also in the dilute phase, thereby oxidizing the remaining CO to CO2 without significant temperature rise in the dilute phase due to the after burn.

Abstract: A process for regenerating a spent catalyst having coke deposits thereon in a catalyst regeneration vessel having a dense phase and a dilute phase, wherein the process comprises the steps of: (a) contacting the spent catalyst with a primary oxygen-containing gas in the dense phase, thereby combusting the coke, resulting in the formation of a combustion gas comprising nitrogen oxides and carbon monoxide which further reacts, thus reducing a majority of the nitrogen oxides to form elemental nitrogen; and (b) contacting the combustion gas with a secondary oxygen-containing gas, and typically a shield gas, in the dilute phase, thereby oxidizing the remaining CO to CO2 without significant temperature rise in the dilute phase due to the after bum.

Abstract: Compositions comprising a component containing (i) an acidic oxide support, (ii) an alkali metal and/or alkaline earth metal or mixtures thereof, (iii) a transition metal oxide having oxygen storage capability, and (iv) palladium promote CO combustion in FCC processes while minimizing the formation of NOx. The acidic oxide support preferably contains silica alumina. Ceria is the preferred oxygen storage oxide.

Abstract: Compositions comprising a component containing (i) an acidic oxide support, (ii) an alkali metal and/or alkaline earth metal or mixtures thereof, (iii) a transition metal oxide having oxygen storage capability, and (iv) palladium promote CO combustion in FCC processes while minimizing the formation of NOx. The acidic oxide support preferably contains silica alumina. Ceria is the preferred oxygen storage oxide.

Abstract: A method for regenerating a hydrocarbon conversion catalyst wherein at least a portion of a halogen-containing compound is precombusted in a precombustion zone, and the catalyst is regenerated in the presence of the halogen. By precombusting the halogen-containing compound in a precombustion zone rather than in the regeneration zone, this invention decreases the risk of permanent catalyst deactivation and of costly equipment damage in the regeneration zone. This method is adaptable to many processes for the catalyst conversion of hydrocarbons in which deactivated catalyst particles are regenerated in a moving bed.

Abstract: Disclosed is a process for controlling combustion in a fluid catalytic cracking regenerator. More specifically, afterburning which occurs during the combustion process is controlled by adjusting oxygen concentration in at least one of two combustion streams which is injected into a fluid catalytic cracking regenerator. Preferably, the combustion streams used in the invention are asymmetrically injected into a dense phase catalyst bed within the regenerator.

Abstract: Coke is burned in the regenerator vessel of an FCC complex with a combustion medium consisting of a diluent gas, such as air, enriched with oxygen, The regenerator is operated in partial combustion mode and excess oxygen is introduced into the combustion zone of the regenerator. Emission of nitrogen oxides to the atmosphere is reduced.

Abstract: Spent FCC catalyst is regenerated under net reducing conditions in a regenerator to minimize the migration of vanadium on the spent FCC catalyst particles. Reducing conditions in at least the bottom 50% of the catalyst bed are maintained by using at least two air distribution grids located in the lower 50% of the catalyst bed.

Abstract: A regenerator in a FCC unit, with the reactor elevated above the regenerator and a side entry spent catalyst introduction to the regenerator, is modified by installing a spent catalyst distribution apparatus along a central vertical axis of the regenerator to radially discharge the spent catalyst and 10-50 percent of the regeneration air into the dense phase of the catalyst. The existing compressor may be used to supply the regeneration air to the spent catalyst distributor. The remaining 50-90 percent of the regeneration air is supplied to the air distribution grid. The retrofit improves spent catalyst distribution and mixing in the regenerator to avoid dilute phase CO combustion or afterburning in the offgas.

Abstract: Hydrogen or carbon monoxide in a carrier of nitrogen or steam is passed over a devitalized catalyst/carbonate or bicarbonate absorber which has absorbed or adsorbed nitrates and nitrites from engine exhaust to restore the carbonate form and regenerate the devitalized catalyst/absorber for reuse.

Abstract: Coke deposits are removed from particulates by combustion in a regenerator by a process in which air is initially used as the oxidant. The combustion gas is subjected to a separation process to remove nitrogen therefrom, and the remaining carbon dioxide-enriched gas stream is recycled to the regenerator together while substantially pure oxygen is introduced into the regenerator. As the level of carbon dioxide in the system increases, the amount of air being introduced into the regenerator is gradually reduced and, in compensation, the amount of oxygen flowing to the regenerator is gradually increased. Eventually, part or all of the air is replaced by oxygen and carbon dioxide recycle gas, and the level of oxygen and carbon dioxide are regulated to maintain the desired temperature in the regenerator.

Abstract: A method and system for cracking hydrocarbons and regeneration of the catalyst is described with particular emphasis directed to partially restoring the activity of the catalyst after an initial hydrocarbon conversion use by heat soaking the catalyst at an elevated temperature before use in a second hydrocarbon conversion zone.This case is a division of application Ser. No. 595,833, filed Jul. 14, 1975.

Abstract: An inertial/filtering separator in a single vessel and FCC process using same as a third stage separator are disclosed. Gas and fines are added tangentially to an annulus formed by a cylindrical insert in a vessel. Gas flows over the insert and down to filters in the vessel. Solids are withdrawn from the base of the annulus and periodically from the filter. Three types of solids collection--inertial, gravity settling and filtration--are practiced in a single vessel.

Abstract: Apparatus and processes are disclosed for carrying out chemical reactions of the type in which a fluidized particulate solid is contacted with reactants in a reaction vessel or conduit and then separated from the reactant products and regenerated in a regeneration process, such as combusting the carbonaceous deposit which accretes on fluid catalytic cracking catalyst particles. The regeneration reaction may change the temperature of the regenerated catalyst particles and in such case it is often required to subject the particles to heat exchange to provide them at a temperature suitable for recirculation to the reaction zone. The processes and apparatus of the invention essentially provide for dividing the fluidized solids regeneration bed into an uppermost bed zone and at least one lower bed zone by a horizontal occlusion zone disposed at a vertically intermediate portion of the bed.

Abstract: Oxides of nitrogen (NO.sub.x) emissions from FCC regenerators in complete CO combustion mode are reduced by degrading regenerator performance to increase the coke on regenerated catalyst. High zeolite content cracking catalyst, regenerated to contain more coke, gives efficient conversion of feed and reduces NO.sub.x emissions from the regenerator. Operating with less catalyst, e.g., 30-60% of the normal amount of catalyst in the bubbling dense bed, can eliminate most NO.sub.x emissions while increasing slightly plant capacity and reducing catalyst deactivation.

Abstract: A process and apparatus for regeneration of spent FCC catalyst in a bubbling bed regenerator having a stripper mounted over the regenerator. Spent catalyst is regenerated in a fast fluidized bed coke combustor heated by direct contact heat exchange with catalyst recycled to the coke combustor via an internal "trough" trap. Catalyst recycle flow to the combustor is controlled by varying gas flow in the trough trap.

Abstract: A process and apparatus for fluidized bed regeneration of FCC catalyst are disclosed. Oxides of nitrogen (NO.sub.x) emissions from an FCC regenerator operating in complete CO combustion mode, and hydrothermal catalyst deactivation, are reduced by reducing the average bed temperature. Dilute phase afterburning superheats catalyst entrained in the dilute phase region above the fluidized bed. Cyclone separators recover superheated, entrained catalyst and preferentially recycle this catalyst to the FCC reactor, permitting cooler operation of the dense phase fluidized bed.

Abstract: A process and apparatus for dense phase, at least partially co-current, fluidized bed regeneration of FCC catalyst are disclosed. Catalyst regeneration occurs in a dense phase fluidized bed, with catalyst flowing laterally from a spent catalyst inlet to a regenerated catalyst outlet. Regeneration air flows up through the dense bed into a dilute phase region defined at the base by the dense phase bed and at the top by a horizontal baffle. The plate has openings or baffles forcing the dilute phase, consisting of entrained catalyst and flue gas, to flow horizontally in the same direction as the lateral flow of catalyst in the dense bed. Concurrent flow of at least the dilute phase material and the dense bed material improves regeneration and can reduce NOx emissions.

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: 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: 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 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: Catalytic regenerators, nozzle designs and processes suitable for introducing regeneration air into a catalytic cracking unit which substantially reduce erosion induced nozzle failures include a plurality of nozzle elements having a roughness defined upon the outside surface of said nozzle elements so as to reduce erosion due to the impact of fluidized catalyst particles within the catalytic 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: 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.