Abstract: A method and apparatus are disclosed to reduce the amount of unstripped hydrocarbon flowing to the regenerator in a riser reactor FCC unit. The catalyst stripper section is heated by indirect heat exchange with a mixture of hot regenerator flue gas and regenerated catalyst. In the preferred embodiment, the regenerator is operated under partial combustion conditions and the resulting carbon monoxide-containing flue gas is burned in a catalyst stripper heat exchanger.

Abstract: A paraffinic feedstream is aromatized in an FCC external catalyst cooler by contacting the paraffinic feedstream with hot regenerated cracking and additive catalysts.

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 process and apparatus for fluid catalytic cracking (FCC) of a hydrocarbon feed. The process and apparatus includes a riser which upwardly discharges into a deflector baffle located within a stripping vessel. The stripping vessel is located within a disengaging vessel. The deflector baffle is spaced from the riser and the stripping vessel. Preferably, the deflector baffle is shaped similarly to a large bubble cap. Catalyst passes downwardly from the baffle into a stripping zone within a lower portion of the stripping vessel. Hydrocarbons stripped from the catalyst pass upwardly away from the stripping zone, then pass to a cyclone located outside the stripping vessel and then discharge from the disengaging vessel.

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 invention is a fluid catalytic cracking process in which reduced catalyst to petroleum feed contact times at high catalytic cracking temperatures are afforded. The catalytic cracking conditions provide olefinic gasoline product with reduced coke make.

Abstract: A process is disclosed for decreasing the emission of airborne pollutants from an oil refinery and for upgrading a paraffinic feedstream to olefins and/or aromatics. Flue gas from a fluid catalytic cracking process catalyst regenerator is cooled to supply the endothermic heat of reaction for a paraffin upgrading reaction, eliminating the need for an additional process furnace. The process further decreases airborne pollutant emissions by upgrading paraffinic fractions which would otherwise be burned as fuel.

Abstract: A method and apparatus are disclosed for transferring heat to a reaction zone in which hot flue gas is passed through a heat exchanger positioned inside the reaction zone. The flue gas may be generated in a catalyst regenerator, a combustion chamber, or both. The combustion chamber may be external or internal to the heat exchanger. The invention is particularly useful for transferring heat to an endothermic fluid-bed catalytic reaction such as dehydrogenation or aromatization.

Abstract: A process and apparatus are disclosed for the production of gasoline from a C.sub.4.sup.- fuel gas containing ethene and propene and catalytic reformate containing C.sub.6 to C.sub.8 aromatics. The C.sub.4.sup.- fuel gas is contacted with debutanized catalytic reformate over a zeolite catalyst under process conditions to convert ethene and propene in the C.sub.4.sup.- fuel gas to C.sub.5.sup.+ aliphatic and aromatic hydrocarbon gasoline and to convert C.sub.6 to C.sub.8 aromatics in the reformate to C.sub.7 to C.sub.11 aromatic hydrocarbon gasoline. Reformer fractionation system containing debutanizer column and separator stabilizes effluent gasoline and recycles unconverted light aromatics.

Abstract: A process is disclosed for increasing the octane number of an FCC unit gasoline pool by upgrading selected gasoline boiling-range streams. FCC gasoline is mixed with the feed to a light olefin upgrading reactor. Upgraded gasoline is then fractionated in an existing FCC gas plant.

Abstract: A process is disclosed for the conversion of an aliphatic feedstream in which an oxygen-deficient flue gas is used to directly transfer heat to the primary conversion reaction. Hydrogen, carbon monoxide and carbon dioxide from the primary conversion reactor effluent are converted to methanol or Fischer-Tropsch liquid and may be recycled to the primary conversion reactor. Preferred primary conversion reactions include dehydrogenation and aromatization of aliphatics.

Abstract: A process is disclosed for stripping and regenerating a zeolite catalyst at relatively low pressure compared to that of an oligomerization reactor operated with a turbulent fluid-bed at above about 515 kPa (60 psig). The reactor operates either with hydrocarbons in the gas phase, or, under near-critical or supercritical conditions, when they are in the super-dense phase. The super-dense phase exists outside a critical region in the phase envelope of the hydrocarbon mixture in the reactor, under conditions at which a liquid phase may not form (hence "non-liquid"). Whether the fluid-bed reactor is operated in the C.sub.5 -C.sub.10 gasoline producing mode, the C.sub.10.sup.+ distillate mode, or, the C.sub.22.sup.+ lubes mode, continuous operation of a regenerator (for deactivated catalyst withdrawn from the reactor) at relatively low pressure, preferably less than 445 kPa (50 psig), is possible.

Abstract: An integrated reforming/aromatization process is disclosed which improves the octane number and C.sub.5 + liquid yield of a catalytic reforming unit by integrating a catalytic aromatization zone into a catalytic reforming unit gas plant fractionator overhead condenser reflux circuit. The fractionator may be operated as a debutanizer to maximize C.sub.5+ gasoline product volume or a depentanizer to maximize C.sub.5+ gasoline product octane number.

Abstract: A continuous multistage process for preparing gasoline and/or distillate range hydrocarbons from lower molecular weight oxygenate feedstock wherein hydrocarbon yield is increased by recovering a vapor stream rich in ethene from an oxygenates conversion stage and reacting the ethene in a high severity reaction zone containing high activity zeolite catalyst.

Abstract: Disclosed is a method of and apparatus for reducing the level of extremely small catalyst particles ("fines") in an FCC system by temporarily retaining particles separated from the secondary cyclone separator in a reactor vessel or catalyst regenerator. These particles can be intermittently withdrawn from the temporary retaining area in order to achieve particle flow at a low volume rate, which takes them out of the active catalyst inventory within the reactor/regenerator system. The intermittent withdrawing of catalyst "fines" reduces the particulate contamination both in flue gas exhausted to the atmosphere from the catalyst regenerator and in the main column bottom (MCB) products from the fractionation stage. Preferred embodiments include intermittent withdrawal of "fines" from either the regenerator or the reactor vessels and the secondary cyclones contained in each of these vessels.

Abstract: An integrated process for converting methanol and other lower molecular weight oxygenates to gasoline and distillate range liquid hydrocarbons and ethene is disclosed. When it is desirable to increase ethene yield, an auxiliary methanol-to-olefins (MTO) fixed bed reactor unit is activated in conjunction with a continuously operated primary MTO fluidized bed reactor.

Abstract: An improved fluid-bed reaction process and apparatus are disclosed in which feedstock is preheated and may be at least partially converted by contacting the feedstock with spent catalyst in a preheat zone. Additional benefits include a reduction in catalyst poisons and coke production in the reaction zone. By contacting the fresh feed with hot spent catalyst, at least a portion of the coke which would otherwise form in the reactor is deposited on the spent catalyst. Temporary catalyst poisons are also sorbed onto the spent catalyst. The spent catalyst is then withdrawn from the preheat zone, stripped of entrained hydrocarbon and regenerated.

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: A method and apparatus for improving the stripping of hydrocarbons from catalyst particles in a fluidized catalytic cracking (FCC) unit. A stripper vessel is located directly adjacent the exhaust barrel of a separator and immediately begins stripping hydrocarbon from catalyst particles. The stripper is sealed at the catalyst exit by a catalyst seal pot, with the drain sized so as to permit only a portion of catalyst flow to pass therethrough, with the remainder catalyst overflowing the seal pot. The location of the stripper adjacent the separator exhaust and the provision of a catalyst seal pot, in other embodiments, can be combined either separately or together with a short contact time (SCT) stripper and/or a catalyst particle deflector in order to reduce the "residence" time of hydrocarbons with catalyst particles.