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: Apparatus for regenerating zeolite-type catalyst used in fixed bed hydrocarbon conversion processes, such as the conversion of olefins to gasoline and diesel fuel. Regeneration is achieved using a portion of a flue gas stream to regenerate catalyst and preheat feedstock. Economies in equipment and operation are realized by employing a once-through configuration for the regenerator gas stream.

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: A process and reactor system is disclosed for hydrotreating a low sulfur containing olefinic distillate and conventional feedstock to a catalytic hydrodesulfurization. The process comprises passing a minor portion of the olefinic distillate to a first hydrotreating zone in admixture with conventional CHD feedstock. A major portion of the olefinic distillate is passed to a second hydrotreating zone in combination with the effluent from the first zone. In this manner the exotherm attributable to olefins hydrogenation is controlled within limits sufficient to avoid very frequent catalyst regeneration.

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: Lower alkanes are converted to olefins in a `third bed` external catalyst cooler (ECC) in which hot catalyst, from a first regenerator (`second bed`) operating in conjunction with a fluid catalytic cracker (`first bed`), thermally cracks and dehydrogenates the alkanes. Because this is an endothermic reaction, the catalyst is autogeneously cooled before it is recirculated to the FCC regenerator. The cracking catalyst is the catalyst of choice in the FCC reactor. Maximum conversion of alkanes to olefins is sought, and can be maintained because the FCC regenerator burns the coke made during alkane dehydrogenation. The olefins produced are then oligomerized in an oligomerization reactor ("fourth" bed) operating in conjunction with a second regenerator ("fifth" bed) to produce a gasoline range stream.

Abstract: Apparatus for converting crude aqueous oxygenate feedstock, such methanol or the like, to liquid hydrocarbons in contact with a medium pore shape selective crystalline acid zeolite catalyst, such as HZSM-5. In a preferred embodiment, the novel technique comprises means for: (a) contacting a crude methanol feedstock containing a minor amount of water with a liquid hydrocarbon extraction stream under extraction conditions favorable to selective extraction of the methanol, thereby providing an extract liquid stream rich in methanol and an aqueous raffinate stream lean in methanol; (b) charging the extracted methanol substantially free of water to said reaction zone under process conditions to convert substantially all methanol to hydrocarbons; (c) cooling reaction effluent to recover aqueous liquid byproduct stream, gas rich in C.sub.2.sup.- hydrocarbons, liquid rich in C.sub.3 -C.sub.4 hydrocarbons and C.sub.5.sup.

Abstract: An integrated process for the production of aromatics rich an MTBE and TAME rich high octane gasoline fractions is described. Etherifications of iso-olefins is conducted in the presence of excess methanol. Unreacted methanol is passed to a fixed, fluid or moving bed aromatization zone in contact with ZSM-5 catalyst and olefin and paraffin feedstream to produce high octane gasoline.

Abstract: A process is disclosed for combining the operation of (i) a primary reactor (referred to as a "MOG" reactor), in which an olefin-containing light gas or light naphtha is oligomerized to gasoline range hydrocarbons, and, (ii) a high pressure secondary reactor (referred to as a "MODL" reactor), to make distillate or lubes, using the effluent (primary effluent) from the MOG reactor as feed for the MODL reactor. In the distillate mode, the primary effluent is tailored so as to be substantially free (less than 3 mol %) of C.sub.10.sup.+ components. Because the C.sub.10.sup.+ "make" from the MOG reactor is spared passage through the MODL reactor, conversion of the C.sub.10.sup.+ components typically experienced due to cracking and oligomerization in the MODL is avoided. Because the C.sub.4.sup.- light components which are highly paraffinic, are separated from the primary effluent in a debutanizer to provide a mainly C.sub.5 -C.sub.

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.

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 either a reactor vessel or catalyst regenerator. These particles can be withdrawn from the temporary retaining area, which takes them out of the active catalyst inventory within the reactor/regenerator system. The 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 withdrawal of "fines" from either the regenerator or the reactor vessels and the secondary cyclones contained in each of these vessels.

Abstract: Method and means are described for the conversion of lower molecular weight paraffins and olefins to high octane gasoline rich in alkylated aromatics. In a two stage process catalyzed by metallosilicate, crystalline, shape selective zeolite comprising a high temperature first stage and a lower temperature second stage, the ratio of olefins to paraffins in the second stage is maintained at a level sufficient to maintain essentially isothermal reaction conditions. Novel means for effecting the conversion include transport riser reactor and turbulent bed reactor combination.

Abstract: An oligomerization system is provided for upgrading lower olefins to distillate hydrocarbons, especially useful as high quality jet or diesel fuels. Thye olefinic feedstock is reacted over a shape selective acid zeolite, such as ZSM-5, to oligomerize feedstock olefins and further convert recycled hydrocarbons. Reactor effluent is fractionated to recover a light-middle distillate range product stream and to obtain gasoline and heavy hydrocarbon streams for recycle.

Abstract: Lower alkanes are converted to olefins in a `third bed` external catalyst cooler (ECC) in which hot catalyst, from the regenerator (`second bed`) operating in conjunction with a fluid catalytic cracker (`first bed`), thermally cracks and dehydrogenates the alkanes. Because this is an endothermic reaction, the catalyst is autogeneously cooled before it is recirculated to the FCC regenerator. The cracking catalyst is the catalyst of choice in the FCC reactor. The most evident benefit of using the ECC is that it eliminates internal regenerator coils for steam regeneration. Among several additional benefits is that the ECC allows flexibility in design of its fluid `third bed` for optimum weight hourly space velocity (WHSV), and control of the dehydrogenation temperature so as to get maximum conversion of alkanes. This conversion can be maintained because the FCC regenerator burns the coke made during alkane dehydrogenation.

Abstract: An integrated process for the production of alkylate and etherate rich high octane gasoline streams comprising the etherification to produce MTBE and TAME in the presence of a high stoichiometric excess of methanol followed by the conversion of unreacted methanol in contact with zeolite-type catalyst in the presence of aromatics to produce alkylated aromatics in gasoline. The light paraffinic effluent from the methanol conversion zone is reacted in contact with zeolite catalyst under aromatization conditions to produce an aromatics feedstream for the methanol conversion reaction. A supplemental olefinic feedstream is provided to the methanol conversion zone after optionally serving as stripping medium for the separation of methanol and etherate-rich C.sub.5 + gasoline from the etherification reaction.

Abstract: A multistage reactor system and operating technique for converting ethene-rich olefinic feedstock to heavier hydrocarbons, particularly gasoline and distillate range products. By employing low temperature and high temperature separators, an economic recycle is provided for each stage.

Abstract: A heat balanced system for converting an olefinic feedstock comprising ethylene and C.sub.3.sup.+ olefins to heavier liquid hydrocarbon product in a catalytic exothermic process. Means are provided for prefractionating the olefinic feedstock to obtain a gaseous stream rich in ethylene and a liquid stream containing C.sub.3.sup.+ olefin, and a reactor for contacting an olefinic feedstock stream from the prefractionating step with ZSM-5 type oligomerization catalyst in a series of exothermic catalytic reactors to provide a heavier hydrocarbon effluent stream comprising distillate, gasoline and lighter hydrocarbons. In a preferred embodiment a catalytic system is provided for making gasoline or diesel fuel from an olefinic feedstock containing ethylene and C.sub.3.sup.+ lower olefins comprising a prefractionation system for separating and recovering ethylene and a liquid stream rich in C.sub.3.sup.