Abstract: Catalyst regenerators and methods of their use are provided. A method includes combusting coke from the catalyst in a second stage regenerator to produce a second flue gas, where the second stage regenerator includes a second combustion chamber and a top having a top cross-sectional area. The coke is partially combusted from the catalyst in a first stage regenerator with a first combustion chamber having a first combustion chamber cross-sectional area greater than the top cross-sectional area. The first stage regenerator is positioned above the top of the second stage regenerator. The first combustion chamber includes a cylindrical section directly over the top and an annular section surrounding the cylindrical section. The second flue gas is vented into the first stage regenerator through a vent tube, and a portion of the second flue gas is dispersed into the annular section of the first combustion chamber.

Abstract: A process for regenerating a coked catalytic cracking catalyst which the carbon-containing deposits on the catalyst contains at least 1 wt % bio-carbon, based on the total weight of carbon present in the carbon-containing deposits is provided. Such coked catalytic cracking catalyst is contacted with an oxygen containing gas at a temperature of equal to or more than 550° C. in a regenerator to produce a regenerated catalytic cracking catalyst, heat and carbon dioxide.

Abstract: A method of operating a continuous or semi-continuous system for a catalyst regeneration process. The system comprises a regenerator, the regenerator comprising a combustion zone and a halogenation zone. The catalyst is fed into the regenerator. A circulating regeneration gas is introduced into a regenerator circuit including oxygen, the circulating regeneration gas having a nitrogen concentration that is less than air. Oxygen from the circulating regeneration gas reacts with the coke to provide water and carbon dioxide. Water and the carbon dioxide formed in this first reaction then further react with the coke to form carbon monoxide and hydrogen.

Abstract: A method of operating a continuous or semi-continuous system for a catalyst regeneration process. The system comprises a regenerator, the regenerator comprising a combustion zone and a halogenation zone. The catalyst is fed into the regenerator. A circulating regeneration gas is introduced into a regenerator circuit including oxygen, the circulating regeneration gas having a nitrogen concentration that is less than air. Oxygen from the circulating regeneration gas reacts with the coke to provide water and carbon dioxide. Water and the carbon dioxide formed in this first reaction then further react with the coke to form carbon monoxide and hydrogen.

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: Disclosed is a catalyst distributor and process for mixing spent catalyst and recycled regenerated catalyst in a regenerator vessel. Mixing is conducted in a confined space to which catalyst is delivered from catalyst conduits protruding through the wall of the regenerator.

Abstract: An apparatus and process are presented for drying a catalyst in a reactor-regenerator system. The process includes a continuous operating system with catalyst circulating between a reactor and regenerator, and the catalyst is dried before returning the catalyst to the reactor. The process uses air that is split between the drying stage and the combustion stage without adding equipment outside of the regenerator, minimizing energy, capital cost, and space requirements.

Abstract: A process for regenerating a coked catalytic cracking catalyst which the carbon-containing deposits on the catalyst contains at least 1 wt % bio-carbon, based on the total weight of carbon present in the carbon-containing deposits is provided. Such coked catalytic cracking catalyst is contacted with an oxygen containing gas at a temperature of equal to or more than 550° C. in a regenerator to produce a regenerated catalytic cracking catalyst, heat and carbon dioxide.

Abstract: Disclosed is a catalyst distributor and process for spreading catalyst over a regenerator vessel. Nozzles disposed angular to a header of the distributor spread catalyst throughout a full cross section of the catalyst bed.

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: Systems and methods of reducing refinery carbon dioxide emissions by improving the overall synthesis gas yield in a fluid catalytic cracking unit having a reactor and a regenerator are discussed. In one example, a method comprises introducing spent catalyst and a feed gas comprising oxygen to the regenerator at gasification conditions. The method further comprises heating the spent catalyst to burn coke therefrom to produce a synthesis gas. The method further comprises combining the synthesis gas with a dry gas comprising hydrogen, creating the overall synthesis gas and thereby increasing the yield of the overall synthesis gas produced in the FCC unit.

Abstract: Systems and methods of improving synthesis gas quality in a fluid catalytic cracking unit are disclosed. In one example, a method comprises reacting a first stage regeneration gas comprising oxygen with spent catalyst from a reactor in a first stage of a regenerator to consume the oxygen in the first stage regeneration gas. This reaction produces a synthesis gas output and partially regenerated catalyst. The method further comprises reacting a second stage regeneration gas comprising oxygen with the partially regenerated catalyst in a second stage of the regenerator to regenerate the partially regenerated catalyst. This reaction produces the first stage regeneration gas for reaction with the spent catalyst in the first stage of the regenerator. Through the first and second stage reactions, the spent catalyst is regenerated and the synthesis gas quality is improved.

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: Processes are disclosure which comprise alternately contacting an oxygen-carrying catalyst with a reducing substance, or a lower partial pressure of an oxidizing gas, and then with the oxidizing gas or a higher partial pressure of the oxidizing gas, whereby the catalyst is alternately reduced and then regenerated to an oxygenated state. In certain embodiments, the oxygen-carrying catalyst comprises at least one metal oxide-containing material containing a composition having one of the following formulas: (a) CexByB?zB?O?, wherein B=Ba, Sr, Ca, or Zr; B?=Mn, Co, or Fe; B?=Cu; 0.01<x<0.99; 0<y<0.6; 0<z<0.5; and 1<?<2.2; (b) SrvLawBxB?yB?zO?, wherein B=Co or Fe; B?=Al or Ga; B?=Cu; 0.01<v<1.4; 0.1<w<1.6; 0.1<x<1.9; 0.1<y<0.9; 0<z<2.2; and 3<?<5.5).

Abstract: A system employing a regenerable zinc-oxide based sorbent to remove one or more contaminants from an incoming gas stream. The contaminant-depleted gas stream can then be used for any subsequent application, while at least a portion of the contaminant-laden sorbent can be regenerated via a step-wise regeneration process. In one embodiment, sorbent regenerated via the step-wise regeneration process can comprise less sorbent-damaging compounds than traditional sorbents exposed to conventional regeneration processes.

Abstract: A method of reclaiming a titanosilicate from a deactivated or spent oxidation catalyst containing a titanosilicate having deposited thereon one or more catalytic metals, such as gold, and optionally, one or more promoter metals, the method involving treating the deactivated catalyst with an oxidant; contacting the oxidant-treated catalyst with acid, preferably aqua regia; washing the titanosilicate to remove residual acid; and optionally drying and/or calcining. A method of reconstituting an active oxidation catalyst from a spent or deactivated oxidation catalyst, the method involving reclaiming the titanosilicate as noted above, and then depositing one or more catalytic metals and, optionally, one or more promoter metals onto the reclaimed titanosilicate.

Abstract: Systems and methods of improving synthesis gas quality in a fluid catalytic cracking unit are disclosed. In one example, a method comprises reacting a first stage regeneration gas comprising oxygen with spent catalyst from a reactor in a first stage of a regenerator to consume the oxygen in the first stage regeneration gas. This reaction produces a synthesis gas output and partially regenerated catalyst. The method further comprises reacting a second stage regeneration gas comprising oxygen with the partially regenerated catalyst in a second stage of the regenerator to regenerate the partially regenerated catalyst. This reaction produces the first stage regeneration gas for reaction with the spent catalyst in the first stage of the regenerator. Through the first and second stage reactions, the spent catalyst is regenerated and the synthesis gas quality is improved.

Abstract: Hydrogenated vegetable oil exhibiting superior thermal stability and containing reduced levels of saturates and trans fatty acids are produced using an activated hydrogenation catalyst and/or an improved hydrogenation process incorporating high shear. The use of a high shear mechanical device incorporated into the hydrogenation process as a reactor device is shown to be capable of enabling reactions that would normally not be feasible under a given set of reaction pressure and temperature conditions. For example, the hydrogenation process described herein enables a reduction of hydrogenation time, and operation at lower temperatures than current processes. The resulting hydrogenated vegetable oil is particularly useful in frying, confectionery baking, and other applications where a product with a low trans fat content or higher thermal stability is desirable. The hydrogenated oil produced may comprise less than 10 weight % of trans fatty acids with less than 5 weight % of linolenic acid (C18:3).

Abstract: An improved oxidizer for liquid reduction-oxidation desulphurization processes uses a hollow fiber membrane contactor. A pressurized, oxygen containing gas stream is introduced into the interior of the hollow fiber membrane while a liquid reduction-oxidation catalyst solution contacts the exterior of the membrane. Oxygen diffuses through the membrane into the liquid reduction-oxidation catalyst solution whereby the solution is oxidized and can be recycled for further us in a desulphurization process.

Abstract: The invention relates to a process for removing sulfur particles from an aqueous catalyst solution used to remove hydrogen sulfide from a gas stream (1, 5), comprising the steps of directing a flow of a suspension (12) comprising reduced catalyst solution and sulfur particles to an oxidizer zone (20), where the catalyst solution is regenerated by contacting said suspension with a gas (22) containing oxygen; and removing sulfur from said suspension at least by gravity sedimentation at a bottom (21) of said oxidizer zone (20). According to the invention a flow deflecting means (34) is disposed at least at an outlet (35) for the oxidized catalyst solution leaving said oxidizer zone (20) such as to prevent any turbulent state caused at least by a stream of oxidized catalyst solution leaving said oxidizer zone (20).

Abstract: An improved oxidizer for liquid reduction-oxidation desulphurization processes uses a hollow fiber membrane contactor. A pressurized, oxygen containing gas stream is introduced into the interior of the hollow fiber membrane while a liquid reduction-oxidation catalyst solution contacts the exterior of the membrane. Oxygen diffuses through the membrane into the liquid reduction-oxidation catalyst solution whereby the solution is oxidized and can be recycled for further us in a desulphurization process.

Abstract: A method for reducing the amount of mercury affixed to a sorbent and/or fly ash is disclosed. The method includes the steps of providing an amount of sorbent and/or fly ash wherein at least a portion of the amount of sorbent and/or fly ash has particulates having mercury compounds affixed to the particulates; and exposing the amount of sorbent and/or fly ash to heated flowing air until mercury compounds are liberated from at least some of the particulates. Preferably, the amount of sorbent and/or fly ash is maintained in the heated flowing air until the sorbent reaches a temperature of at least 700° F. (372° C.). When the sorbent is activated carbon, it is preferred that the amount of sorbent and/or fly ash is maintained in the heated flowing air until the activated carbon reaches a temperature in the range of 700° F. (372° C.) to 1000° F. (538° C.).

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: The present invention provides a catalytic cracking process. The process includes introducing at least one species of a natural or synthetic residuum containing feedstock and a catalyst into a catalytic cracker reaction zone, and thereafter cracking the feedstock into a lower molecular weight gaseous product and spent cracking catalyst with hydrocarbonaceous product deposited thereon. Among others, the lower molecular weight gaseous product includes ethylene or propylene. The spent cracking catalyst obtained from the catalytic cracker reaction zone may then be regenerated using a first and a second regeneration zone. The first regeneration zone may be operated in an oxidizing mode resulting in a remaining coke of reduced hydrogen content which lowers the moisture content of flue gas in subsequent regeneration zones.

Abstract: The present invention provides a method of producing a synthesis gas from a regeneration of a spent cracking catalyst. The method includes introducing a spent cracking catalyst into a first regeneration zone in a presence of a first atmosphere comprising a first oxygen containing gas at a first regeneration temperature. For example, a temperature that does not exceed about 1400° F., and more preferable, a temperature that ranges from about 1150° F. to about 1400° F., may be used as the first regeneration temperature. The method further includes introducing the spent cracking catalyst from the first regeneration zone into a second regeneration zone. The spent cracking catalyst is introduced into the second regeneration zone in a presence of a second atmosphere comprising a second oxygen containing gas and a carbon dioxide rich stream, and at a second regeneration temperature substantially greater than the first regeneration temperature.

Abstract: An distributor arrangement introduces spent FCC catalyst more uniformly across the dense bed of the regenerator to provide more even contact with regeneration gas in order to avoid hot spots and zones of incomplete combustion. The invention forms a fluidized hopper to collect spent catalyst and a horizontally extended header with multiple horizontally extended outlet arms to place catalyst into the regenerator. The invention may use an aeration means to fluidize the header to further assist catalyst flow. Furthermore, the spent catalyst delivered to the top of the regenerator dense reduces NOx emissions in the flue gas.

Abstract: The present invention provides a method of producing a synthesis gas from a regeneration of spent cracking catalyst. The method includes introducing a spent cracking catalyst into a first regeneration zone in a presence of a first oxygen and carbon dioxide atmosphere and at a first regeneration temperature. For example, a temperature that does not exceed about 1400° F., and more preferable a temperature that ranges from about 1150° F. to about 1400° F., may be used as the first regeneration temperature. The method further includes introducing the spent cracking catalyst from the first regeneration zone into a second regeneration zone in a presence of a second oxygen and carbon dioxide atmosphere, and producing a synthesis gas from cracking deposits located on the spent cracking catalyst within the second regeneration zone at a second regeneration temperature substantially greater than said first regeneration temperature.

Abstract: The present invention provides a method of producing a synthesis gas from a regeneration of spent cracking catalyst. The method includes introducing a spent cracking catalyst into a first regeneration zone in a presence of a first oxygen and carbon dioxide atmosphere and at a first regeneration temperature. For example, a temperature that does not exceed about 1400° F., and more preferable a temperature that ranges from about 1150° F. to about 1400° F., may be used as the first regeneration temperature. The method further includes introducing the spent cracking catalyst from the first regeneration zone into a second regeneration zone in a presence of a second oxygen and carbon dioxide atmosphere, and producing a synthesis gas from cracking deposits located on the spent cracking catalyst within the second regeneration zone at a second regeneration temperature substantially greater than said first regeneration temperature.

Abstract: Catalyst activation of a platinum reforming catalyst system contained in a multiple reactor system by simultaneously reducing the catalyst with hydrogen while introducing a nonmetallic chlorine-containing compound into a reactor of the multiple reactor system in an amount to add from about 0.05 to about 0.3 weight percent chlorine to the catalyst and thereafter purging the system with about 100 to about 50,000 cubic feet of hydrogen per cubic foot of catalyst resulting in a reforming system having increased activity and providing enhanced RON values with reduced cracking of feedstock.

Abstract: The method of the present invention involves the in situ formation of metal-molybdate catalyst particles active for methanol oxidation to formaldehyde, with iron as an example, the catalyst is made by mixing particulate forms of Fe2O3 and MoO3 which form an active Fe2(MoO4)3/MoO3 component inside the reactor during methanol oxidation.

Abstract: The present invention relates to a process for preparing a hydroprocessing catalyst comprising the steps of subjecting a spent hydroprocessing catalyst comprising carbonaceous and sulphurous deposits to a thermal treatment to remove at least part of said deposits, grinding the thus obtained spent catalyst, mixing the ground hydroprocessing catalyst with at least one additive, and shaping the mixture of additive and ground hydroprocessing catalyst to form particles of a new hydroprocessing catalyst, with the spent hydroprocessing catalyst being subjected to a high-temperature calcination step carried out at a temperature in the range of 550-1000.degree. C. for a period sufficient to increase the MPD of the spent catalyst by at least 0.5 nm.The process according to the invention is particularly suitable for preparing ebullated bed catalysts from spent hydroprocessing catalysts.

Abstract: A process of regenerating a sulfided sorbent is provided. According to the process of the invention, a substantial portion of the energy necessary to initiate the regeneration reaction is provided by the combustion of a particulate metal sulfide additive. In using the particulate metal sulfide additive, the oxygen-containing gas used to regenerate the sulfided sorbent can be fed to the regeneration zone without heating or at a lower temperature than used in conventional processes wherein the regeneration reaction is initiated only by heating the oxygen-containing. The particulate metal sulfide additive is preferably an inexpensive mineral ore such as iron pyrite which does not adversely affect the regeneration or corresponding desulfurization reactions. The invention further includes a sorbent composition comprising the particulate metal sulfide additive in admixture with an active metal oxide sorbent capable of removing one or more sulfur compounds from a sulfur-containing gas stream.

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: A method and apparatus for desulfurizing a gas and regenerating a sorbent is disclosed. The sulfur-containing feed gas which can be an effluent gas from a coal gasification reactor, for example, is desulfurized with a particulated metallic oxide sorbent in a transport riser. The sulfided sorbent is than separated from a desulfurized effluent gas and regenerated by contact with an oxygen-containing gas in a transport riser. The regenerated sorbent is separated from an SO.sub.2 containing offgas and recycled to the desulfurization step. The degree of sorbent conversion in the desulfurization step is held at a low level and the sorbent regeneration rate is increased to avoid excessive temperature rise in the regeneration step. In such manner, sorbent cooling can be substantially eliminated. The regeneration riser preferably comprises a once-through lift riser to minimize the riser transport gas requirements to just oxidant gas or oxidant gas mixed with a reduced amount of diluent gas.

Abstract: Hydrocarbon fluid catalytic cracking (FCC) plants are debottlenecked by replacing air feed to the cracking catalyst regenerator with oxygen and carbon dioxide exhaust from the catalyst regenerator and removing methane and hydrogen from the wet gas stream leaving the main fractionator overhead receiver prior to its introduction into a wet gas compressor system. Nitrogen is removed from the exhaust gas and methane and hydrogen are removed from the wet gas in the same pressure swing adsorption (PSA) plant. During air replacement, exhaust gas is processed in the PSA plant and when the desired amount of nitrogen is removed from the exhaust gas, feed of exhaust gas to the PSA plant is terminated and flow of wet gas to the PSA plant is initiated.

Abstract: A method of regenerating V/P/O oxidation catalyst used for the partial oxidation of n-butane which comprises terminating the n-butane feed and contacting the catalyst with an oxygen containing gas, such as air for a sufficient period of time to regenerate the catalyst such that when the n-butane feed is restarted the yield is greater than just before the treatment.

Abstract: A method and apparatus for desulfurizing a gas and regenerating a sorbent is disclosed. The sulfur-containing feed gas which can be an effluent gas from a coal gasification reactor, for example, is desulfurized with a particulated metallic oxide sorbent in a transport riser. The sulfided sorbent is than separated from a desulfurized effluent gas and regenerated by contact with an oxygen-containing gas in a transport riser. The regenerated sorbent is separated from an SO.sub.2 containing offgas and recycled to the desulfurization step. The degree of sorbent conversion in the desulfurization step is held at a low level and the sorbent regeneration rate is increased to avoid excessive temperature rise in the regeneration step. In such manner, sorbent cooling can be substantially eliminated. The regeneration riser preferably comprises a once-through lift riser to minimize the riser transport gas requirements to just oxidant gas or oxidant gas mixed with a reduced amount of diluent gas.

Abstract: 1,1,1,2-Tetrafluoroethane (R134a) is purified to remove 50-10,000 wt. ppm of 2-chloro-1,1-difluoroethylene (R1122) by contacting with a zeolite or carbon molecular sieve having an average pore diameter of 3.8 to 4.8 Angstroms. The zeolite or carbon molecular sieve is regenerated by inert gas stripping residual R134a, followed by a regeneration at elevated temperatures using an inert gas. Regeneration of the zeolite or carbon molecular sieve is accomplished without the substantial reduction in capacity for impurities.

Abstract: A process for the regeneration of a catalyst by combustion of the coke deposited thereon during a hydrocarbon conversion reaction in which process more than 50 percent of the coke is burned in at least one regeneration chamber operating with a fluidized bed, wherein the upper portion of the fluidized bed the suspension of catalyst particles in said chamber is slowed down due to a substantial increase in the diameter of the regeneration chamber so that the superficial velocity of the rising fluids which no longer contain any oxygen is reduced to a value ranging from 0.5 to 1.5 meters/second, that is, to a value corresponding to the fluidization conditions in a dense fluidized bed.

Abstract: Novel sorbents comprising (a) an alumina substrate having a pore volume between 0.4 and 0.8 cc/g, and (b) an alkali or alkaline earth component, for example, sodium carbonate, wherein the amount of the alkali or alkaline earth component is between 50 and 400 .mu.g per m.sup.2 of the substrate. The sorbents of the present invention are outstandingly effective for the removal of nitrogen oxides, sulfur oxides and hydrogen sulfide from waste gas streams.

Abstract: The present invention is concerned with the method of regenerating the fluidizable, catalytic, particulate solids in the regenerator section of an FCC process, and RCC process or a metals removal system or "ART" type process. It is directed to the use of a conduit means for charging fluidizing gaseous material to a vertical cylindrical vessel for cooling fluidizable particulate solids flowing through said vertical cylindrical vessel, which conduit means comprises a horizontal header means having suspended therefrom a plurality of vertical and horizontally spaced apart conduits, each conduit having near its open end a restriction orifice. The header means is located near the top of the cylindrical cooling vessel. One portion of the vertical conduits has lower ends located in the upper half of the vessel and a second portion of the vertical conduits has lower ends located in a lower half of the vessel.

Abstract: A unique process arrangement is disclosed wherein the effluent flue gas from the removal of hydrocarbonaceous coke from particulate matter by combustion in a mixture of pure oxygen diluted with carbon dioxide is processed to provide a carbon dioxide-rich recycle gas stream to be mixed with oxygen as regenerator feed gas; and a net combustion product stream from which are recovered SO.sub.x and NO.sub.x to eliminate atmospheric emissions, and a pure CO.sub.2 product for export. An alternate embodiment also produces hydrogen or synthesis gas for export.

Abstract: An improved process for recovering energy via an expander turbine axial flow gas compressor set which utilizes hot regeneration gas recovered from the regeneration of fluidized catalytic cracking catalyst, and during turndown conditions when the output of the gas compressor is required to be increased by an excess amount to prevent surge and the excess amount is normally vented to the atmosphere prior to entering the regenerator to prevent afterburn, the process including the steps of:(1) adjusting air compressor air rate set point to at least 10% above surge; thereby(2) increasing air rate to an amount in excess of regeneration requirement;(3) flowing all air compressed to the regenerator;(4) by use of complete combustion catalyst, oxidizing essentially all coke to carbon dioxide,(5) driving the expander with all the hot flue gas produced and thereby;(6) driving the motor-generator thereby generating electricity.

Abstract: In a method for regeneration of moist powder adsorption agent, the moist-charged adsorption agent is first fed into the lower area of a fluidized bed which is provided with an aeration and heat-carrying material; the agent then is fed upwardly through the heat-carrying material while being simultaneously dried, and then the agent is withdrawn together with the vortex gas from the fluidized bed. The agent is separated from the vortex gas in a successively switched separator, and is then fed to a further fluidized bed which is provided with a further aeration and heat-carrying material. The agent is fed in that further bed upwardly through the further heat-carrying material and is simultaneously regenerated. The agent is then discharged together with the further vortex gas from the further fluidized bed. The vortex gases which are withdrawn can be reused as mixing gases during the vortex gas generation.

Abstract: A tungsten-containing catalyst associated with coke containing vanadium and nickel is recovered by a method which includes steam gasification, low temperature burning to remove at least a portion of the coke and selective extraction of the nickel and vanadium.

Abstract: The present invention is directed to a method and sequence of processing steps within an apparatus arrangement comprising two separate fluidized relatively dense catalyst beds undergoing regeneration to remove carbonaceous deposits wherein catalyst particles are circulated between catalyst beds to transfer heat from one bed to another and transfer partially regenerated catalyst from one bed to a second heat generating catalyst bed, said catalyst regeneration system arranged to maintain a desired heat balanced temperature restriction less than 787.degree. C. (1450.degree. F.) and the generation of a CO.sub.2 rich flue gas with utilization thereof to achieve reaction with carbon form carbon monoxide under endothermic reaction temperature conditions.

Abstract: A process is disclosed for the conversion of high boiling oil feeds having a significant level of Conradson carbon components and metals to form lighter oil products by contacting the feed under catalytic conversion conditions with a catalyst containing one of a select group of metal additives to catalyze the endothermic removal of carbon with CO.sub.2. Conversion conditions are such that hydrocarbonaceous material and metals are deposited to deactivate the catalyst in the conversion zone. Deactivated catalyst is partially regenerated in the presence of carbon dioxide containing gas before or after oxygen regeneration at a temperature below 1600.degree. F. to provide a regenerated catalyst which is recycled to the conversion zone for further contact with fresh feed. The metal additive is present on the catalyst in an amount sufficient to catalyze the endothermic removal of carbonaceous material in the presence of a carbon dioxide rich gas at regeneration temperature below 1500.degree. F.