Abstract: There is provided an aluminum-containing aluminosilicate zeolite corresponding to the substantially aluminum free silicate zeolite described in the Hinnenkamp et al U.S. Pat. No. 4,376,757. Also provided are methods for making this aluminosilicate zeolite and methods for the catalytic conversion of organic charges to desired products with this aluminosilicate zeolite.

Abstract: The catalytic cracking of a hydrocarbon oil to provide a product of increased octane number and increased C.sub.5 + gasoline content is carried out employing a cracking catalyst composition containing both a large pore crystalline zeolite component and an MCM-22 zeolite component.

Abstract: A catalytic cracking process operates with enhanced stripper efficiency by subjecting spent catalyst to microwave radiation before catalyst regeneration. Preferably the microwave frequency is one which ignores the catalytic cracking catalyst and preferentially excites the hydrocarbon or coke on the spent catalyst, the stripping steam conventionally used, or both the stripping steam and the hydrocarbonaceous coke. In preferred embodiments, microwave frequencies are used which are selective for various impurities in the coke, such as sulfur and/or nitrogen impurities. Additives, such as ferrous materials, may be added to augment the efficiency of desulfurization during stripping. The process is applicable to fluidized catalytic cracking and moving bed catalytic cracking units.

Abstract: A catalytic cracking process is described featuring multiple risers in which a variety of hydrocarbon conversion reactions take place, a stripping unit in which entrained hydrocarbon material is removed from catalyst and a regeneration zone in which spent cracking catalyst is regenerated, which comprises:(a) catalytically cracking a relatively high boiling hydrocarbon charge material in a first riser in the presence of both a first catalyst component which is an amorphous cracking catalyst and/or a large pore crystalline cracking catalyst and a second catalyst component which is selected from zeolite Beta and/or medium pore crystalline silicate zeolite catalyst to provide a variety of products including naphtha and C.sub.3 and/or C.sub.4 olefin;(b) thermally cracking a C.sub.

Abstract: A catalytic cracking process is disclosed which comprises catalytically cracking a hydrocarbon charge stock in a catalytic cracking unit possessing at least one reaction zone, stripping zone and catalyst regeneration zone to provide a gasiform product employing as catalyst a mixed catalyst system which comprises, as a first catalyst component, particles of a cracking catalyst which requires relatively frequent regeneration and is relatively hydrothermally stable, and as a second catalyst component, particles of a catalyst which requires less frequent regeneration than the first catalyst component, physical characteristics(s) of particles of first catalyst component differing sufficiently from physical characteristics(s) of particles of second catalyst component as to permit their separation in the stripping zone.

Abstract: The use of a catalyst containing Mn, a large pore crystalline molecular sieve, and optionally rare earths in catalytic cracking is disclosed. This catalyst gives high gasoline selectivity with low coke yields and is suitable for either gas oil or resid cracking applications.

Abstract: A catalytic cracking catalyst mixture and process are disclosed. The mixture comprises (a) a cracking catalyst containing a matrix and a large pore molecular sieve and (b) separate additive catalysts comprising at least one of a shape selective paraffin cracking/isomerization zeolite and a shape selective aliphatic aromatization zeolite. An exemplary catalyst mixture comprises Dealuminized zeolite Y, optionally containing rare earth elements in an alumina-rich matrix, an additive catalyst of HZSM-5 in a matrix, and an additional additive catalyst of gallium ZSM-5 in a matrix. The alumina-rich matrix of the cracking catalyst acts as a sodium and metals sink. The large pore molecular sieve catalyst cracks large hydrocarbons to lighter paraffins and olefins. The shape selective paraffin cracking/isomerization component cracks/isomerizes the paraffins produced by the large pore molecular sieve. The shape selective aliphatic aromatization catalyst converts light paraffins and olefins into aromatics.

Abstract: A catalytic cracking process and apparatus operates with multiple feed injection points to a riser reactor with several enlarged regions. An elutriable catalyst mixture is used, comprising a conventionally sized cracking catalyst and a faster settling, shape selective additive cracking catalyst. Straight run naphtha, and a light, H.sub.2 -rich aliphatic stream are added to the base of a riser reactor. A resid feed is added higher up in the riser, with a gas oil and recycled heavy cycle oil and naphtha streams added even higher up in the riser. The riser has an elutriating base, and an elutriating upper portion, which increase residence time of the shape selective zeolite additive relative to the conventionally sized cracking catalyst.

Abstract: The present invention discloses a catalytic cracking operation featuring a single riser in which a variety of hydrocarbon conversion reactions takes place, a stripping unit in which entrained hydrocarbon material is removed from catalyst and a regeneration zone in which spent cracking catalyst is regenerated, which comprises:(a) converting a relatively high boiling charge material introduced to the riser at a lower level thereof in the presence of a first catalyst component which is an amorphous cracking catalyst and/or a large pore crystalline silicate cracking catalyst to provide lighter products including significant quantities of naphtha; and,(b) converting a naphtha charge material introduced to the riser at a higher level thereof in the presence of a second catalyst componet which is a shape selective medium pore crystalline silicate zeolite catalyst to provide a relatively high octane gasoline product.

Abstract: An improved process for stripping, or desorbing, entrained hydrocarbon material and, where present, sulfur-containing material, from a catalyst mixture recovered from a catalytic cracking reaction zone is described which comprises:(a) providing a quantity of catalyst mixture containing entrained hydrocarbon material and, optionally, sulfur-containing material, in at least one stripping zone in which a stripping gas removes said entrained hydrocarbon material and, where present, sulfur-containing material, the catalyst mixture comprising, as a first catalyst component, an amorphous and/or large pore crystalline cracking catalyst and, as a second catalyst component, a shape selective medium pore crystalline silicate zeolite catalyst, said first and second catalyst components being present in admixture within a common stripping zone or segregated into separate stripping zones; and,(b) conducting an exothermic reaction within the common stripping zone or within the separate stripping zone containing segregated se

Abstract: New catalyst compositions of superior hydrothermal stability, which evidence increased gasoline plus distillate yields, improved coke selectivity and reduced C.sub.4.sup.- gas yields, are based on framework dealuminated faujasitic zeolites having a framework silica to alumina molar ratio of from about 5 to 100. In a preferred embodiment, an "ultrastable Y" composited with a matrix, is subjected to a treatment with a source of aluminum and rare earth compounds followed by hydrothermal treatments to improve the hydrothermal stability and selectivity of the catalyst for catalytic cracking. This is evidenced by higher gasoline plus distillate yields and lower coke and gas production at lower catalyst useage per barrel of feed relative to commercial cracking catalysts currently being used.

Abstract: A catalytic cracking process is described featuring multiple risers in which a variety of hydrocarbon conversion reactions takes place, a stripping unit in which entrained hydrocarbon material is removed from catalyst and a regeneration zone in which spent cracking catalyst is regenerated, which comprises:(a) converting a relatively high boiling hydrocarbon charge material in a first riser in the presence of a catalyst mixture comprising, as a first catalyst component, an amorphous cracking catalyst and/or a large pore crystalline cracking catalyst and, as a second catalyst component, a shape selective medium pore crystalline silicate to provide lighter products including naphtha and C.sub.3 and/or C.sub.4 olefin;(b) converting an ethylene-rich charge material introduced to a second riser at a lower level thereof in the presence of said catalyst mixture to provide heavier products and to increase the temperature of the catalyst in said region; and,(c) converting C.sub.3 and/or C.sub.

Abstract: A catalytic cracking process is disclosed which comprises catalytically cracking a hydrocarbon charge stock in a catalytic cracking unit possessing at least one reaction zone, stripping zone and catalyst regeneration zone to provide a gasiform product employing as catalyst a mixed catalyst system which comprises, as a first catalyst component, particles of a cracking catalyst which requires relatively frequent regeneration and is relatively hydrothermally stable, and as a second catalyst component, particles of a catalyst which requires less frequent regeneration than the first catalyst component, physical characteristic(s) of particles of first catalyst component differing sufficiently from physical characteristic(s) of particles of second catalyst component as to permit their separation in the stripping zone.

Abstract: A process for catalytically cracking deep cut vacuum gas oils, resids, or other reduced crudes containing metal contaminants to increase gasoline octane. Hydrocarbon feedstocks which include vanadium and sodium contaminants are introduced into the reaction zone of a catalytic cracking unit. Catalytic cracking catalysts which include a ZSM-5 type catalytic component are contacted in the reaction zone with the metals-containing hydrocarbon feedstock. The hydrocarbon feedstock is cracked at high temperature by the cracking catalysts, resulting in increased gasoline octane, and surprising tolerance of the ZSM-5 type catalytic component to poisoning from the usually expected synergistically destructive combination of sodium and vanadium on Y-type zeolites.

Abstract: A multistage process for reducing NO.sub.x in flue gas from fluid catalytic cracking catalyst regeneration. Flue gas is preferably removed after each stage. NO.sub.x formed in each regeneration stage is converted to N.sub.2 prior to discharge from a stage by operating at least the downstream ends of each regeneration stage at oxygen-lean conditions. Staged regeneration can be achieved by passing spent catalyst through a transport reactor in plug type flow and sequentially contacting the catalyst with a plurality of oxygen-containing streams.

Abstract: A fluid catalytic cracking method which comprises:(a) cracking a hydrocarbon feed stock in the presence of a mixed catalyst system which comprises particles of a first, amorphous cracking catalyst and/or large crystalline cracking catalyst component which requires frequent regeneration in a catalyst regeneration zone and particles of a second, shape selective crystalline silicate zeolite catalyst component which is less coke deactivated than the first catalyst component and requires less frequent regeneration than the latter, there being a sufficient difference between one or more of the characterizing physical properties of each catalyst component that the rate of circulation of particles of second catalyst component through the regeneration zone is, on the average, less than that of particles of first catalyst component, said cracking providing a product rich in C.sub.2-6 olefins; and,b) catalytically converting C.sub.2 -C.sub.6 olefins obtained from step (a) to a product containing gasoline and distillate.

Abstract: The present invention discloses a catalytic cracking process featuring at least one riser reactor, at least one stripping unit and at least one regenerator, which comprises:(a) cracking a C.sub.

Abstract: A mixed catalyst system is disclosed which comprises particles of a first, component which requires frequent regeneration in a catalyst regeneration zone and particles of a second catalyst component which is less coke deactivated than the first catalyst component and requires less frequent regeneration than the latter, there being a sufficient difference between one or more of the characterizing physical properties of each catalyst component that the rate of circulation of particles of second catalyst component through the regeneration zone is, on the average, less than that of particles of first catalyst component.

Abstract: A catalytic cracking process is provided which comprises:(a) cracking a first heavy hydrocarbon feed in a first riser in the presence of a mixed catalyst composition comprising, as a first catalyst component, an amorphous cracking catalyst and/or a large pore crystalline cracking catalyst and, as a second catalyst component, a shape selective medium pore crystalline silicate zeolite, to provide gasoline boiling range material and one or more light hydrocarbons; and,(b) cracking a thermally treated second heavy hydrocarbon feed in a second riser in the presence of said mixed catalyst composition and in admixture with a gasiform material contributing mobile hydrogen species and/or carbon-hydrogen fragments at the reaction conditions employed to provide gasoline boiling range material in increased yield and/or of higher quality.

Abstract: A multistage process for reducing NO.sub.x in flue gas from fluid catalytic cracking catalyst regeneration. flue gas is preferably removed after each stage. A portion of NO.sub.x formed in an upstream portion of first and second regeneration stages is converted to N.sub.2, prior to discharge from the first and second stages, respectively, by operating downstream ends of the respective first and second stages at oxygen-lean conditions. The present invention also may provide staged regeneration, to reduce NO.sub.x in flue gas, by passing spent catalyst through a transport reactor in plug type flow and sequentially contacting the catalyst with a plurality of oxygen-containing streams.