Abstract: Disclosed are silicoaluminophosphates (SAPOs) having unique silicon distributions, a method for their preparation and their use as catalysts for the catalytic cracking of hydrocarbon feedstocks. More particularly, the new SAPOs have a high silica: alumina ratio, and are prepared from microemulsions containing surfactants.

Abstract: Disclosed are silicoaluminates (SAPOs) having unique silicon distributions, a method for their preparation and their use as naphtha cracking catalysts. More particularly, the new SAPOs have a high silica:alumina ratio and favorable Si atom distribution.

Abstract: Disclosed are silicoaluminophosphates (SAPOs) having unique silicon distributions, a method for their preparation and their use as catalysts for the catalytic cracking of hydrocarbon feedstocks. More particularly, the new SAPOs have a high silica:alumina ratio, and are prepared from microemulsions containing surfactants.

Abstract: Nickel-copper catalysts supported on an amorphous silica-alumina acidic carrier, preferably containing a binder, and having an iso-electric point of ≧6.5 are used to hydroisomerize paraffins, particularly Fischer-Tropsch paraffins, boiling at 350° F.+ into lighter, more valuable products.

Abstract: Disclosed are silicoaluminophosphates (SAPOs) having unique silicon distributions, a method for their preparation and their use as catalysts for the catalytic cracking of hydrocarbon feedstocks. More particularly, the new SAPOs have a high silica:alumina ratio, and are prepared from microemulsions containing surfactants.

Abstract: The present invention relates to an integrated fluid coking/hydrogen production process. The fluid coking unit is comprised of a fluid coker reactor, a heater, and a gasifier. Solids from the fluidized beds are recycled between the coking zone and the heater and between the heater and the gasifier. A separate stream of hot solids from the gasifier is passed to the scrubbing zone of the reactor. Methane and steam are introduced into the stream of hot solids passing from the gasifier to the scrubbing zone. The hot particles act to catalyze the conversion of methane to carbon monoxide and hydrogen in the presence of steam.

Abstract: High surface purity heat transfer solids are formed, suitably by washing and treating particulate refractory inorganic solids, notably alumina, which contains as impurities up to about 0.5 wt. % silicon and/or up to about 500 wppm boron, with an acid, or dilute acid solution sufficient to reduce the concentration of silicon and boron in the outer peripheral surface layer of the particles, e.g., as measured inwardly toward the center of a particle to a depth of about 50 .ANG. using X-ray photoelectron spectroscopy, to no greater than about 5 atom percent silicon and boron, preferably about 2 atom percent silicon and boron, based on the total number of cations within said outer peripheral surface layer, thereby reducing the tendency of said particles to sinter and agglomerate in the conversion of said hydrocarbon to hydrogen and carbon monoxide in a fluidized bed synthesis gas operation vis-a-vis particles otherwise similar except that the particles are not treated with the acid.

Abstract: A particulate, precalcined low silica content zirconia, especially one stabilizer with yttria, is useful as a catalyst support or as a heat transfer solids component for conducting chemical reactions at high temperature, in oxidizing, reducing or hydrothermal conditions, especially in syn gas operations. An admixture of precalcined particulate low silica content zirconia, particularly a low silica content yttria-stabilized zirconia, is employed in a preferred embodiment as a heat transfer solid, in concentrations ranging generally from about 10 wt. % to about 99.9 wt. % with a particulate catalyst notably a nickel-on-alumina catalyst, in concentration ranging generally from about 0. 1 wt. % to about 90 wt. %. Such an admixture provides a particularly useful catalytic contact mass in high temperature oxidizing, reducing and hydrothermal environments, notably in conducting synthesis gas generation operations.

Abstract: An integrated fluid coking/paraffin dehydrogenation process. The fluid coking unit is comprised of a fluid coker reactor and a heater with hot solids recycling between the coker reactor and the heater. A light paraffin stream is introduced into the line wherein the hot particles are recycled to the coking zone. The hot particles act to catalyze the dehydrogenation of the paraffins to olefins.

Abstract: Disclosed is a method which combines catalytic cracking and olefin production using a coked catalytic cracking catalyst as a dehydrogenation catalyst to dehydrogenate an alkane feed stream and form an olefin rich product stream. The method uses a staged backmixed regeneration system to form the dehydrogenation catalyst and to fully reactivate deactivated cracking catalyst for reuse in the cracking reaction. The catalyst preferably comprises a crystalline tetrahedral framework oxide component.

Abstract: The present invention relates to an integrated fluid coking/paraffin dehydrogenation process. The fluid coking unit is comprised of a fluid coker reactor, a heater, and a gasifier. Solids from the fluidized beds are recycled between the coking zone and the heater and between the heater and the gasifier. A separate stream of hot solids from the gasifier is passed to a satellite reactor. A light paraffin stream is introduced into directly into this stream of hot solids passing to the satellite reactor or into the satellite reactor. The hot particles act to catalyze the dehydrogenation of the paraffins to olefins.

Abstract: An integrated fluid coking/paraffin dehydrogenation process. The fluid coking unit is comprised of a fluid coker reactor, a heater, and a gasifier. Solids from the fluidized beds are recycled between the coking zone and the heater and between the heater and the gasifier. A separate stream of hot solids from the gasifier is passed to the scrubbing zone after first being reduced in temperature by introduction of an effective amount of diluent, such as steam. A light paraffin stream is introduced into this stream of hot solids between the point where the diluent is added and the scrubbing zone. The hot particles act to catalyze the dehydrogenation of paraffins to olefins.

Abstract: An integrated fluid coking/paraffin dehydrogenation process. The fluid coking unit is comprised of a fluid coker reactor, a heater, and a gasifier. Solids from the fluidized beds are recycled between the coking zone and the heater and between the heater and the gasifier. A separate stream of hot solids from the gasifier is diluted with hot solids from the heater then passed to the scrubbing zone of the coker reactor. A light paraffin stream is introduced into this stream of hot solids between the point where the heater solids are introduced and the scrubbing zone. The hot particles act to catalyze the dehydrogenation of the paraffins to olefins.

Abstract: An integrated fluid coking/paraffin dehydrogenation process. The fluid coking unit is comprised of a fluid coker reactor, a heater, and a gasifier. Solids from the fluidized beds are recycled between the coking zone and the heater and between the heater and the gasifier. A separate stream of hot solids from the gasifier is passed to the scrubbing zone or to a satellite fluidized reactor. A first stream containing an effective amount of C.sub.1 to C.sub.2 paraffins is introduced into this stream of hot solids between the point where the diluent is added and the scrubbing zone. The hot particles act to catalyze the dehydrogenation of paraffins to olefins. A second stream containing C.sub.3 to C.sub.10 paraffins is introduced downstream of the introduction of said first stream.

Abstract: Disclosed is a method which combines catalytic cracking and olefin production using a coked catalytic cracking catalyst to dehydrogenate an alkane feed stream and form an olefin rich product stream. Preferably, the coked catalytic cracking catalyst has a carbon content of about 0.2-10 wt. %. The catalyst preferably comprises a crystalline tetrahedral framework oxide component.

Abstract: A particulate, precalcined low silica content zirconia, especially one stabilized with yttria, is useful as a catalyst support or as a heat transfer solids component for conducting chemical reactions at high temperature, in oxidizing, reducing or hydrothermal conditions, especially in syn gas operations. An admixture of precalcined particulate low silica content zirconia, particularly a low silica content yttria-stabilized zirconia, is employed in a preferred embodiment as a heat transfer solid, in concentrations ranging generally from about 10 wt. % to about 99.9 wt. %, with a particulate catalyst, notably a nickel-on-alumina catalyst, in concentration ranging generally from about 0.1 wt. % to about 90 wt. %. Such an admixture provides a particularly useful catalytic contact mass in high temperature oxidizing, reducing and hydrothermal environments, notably in conducting synthesis gas generation operations.

Abstract: A structurally modified alumina useful as a catalyst support, or heat transfer solid for fluidized bed synthesis gas processing. A Group IIA metal, or metals, particularly magnesium and barium, is composited with a particulate alumina to provide a catalyst support, or alumina heat transfer solid, having increased resistance to sintering and agglomeration; properties which promote defluidization of the bed in conducting fluidized bed reactions at high temperatures. The particles of preference are represented by formulas (1) and (2), a composite particle being represented by formula (1), as follows:M.sub.x Al.sub.2 O.sub.3+x (1)with the core of the particle being represented by formula (2), as follows:M.sub.y Al.sub.2 O.sub.3+y (2)where in formulas (1) and (2) M is a Group IIA metal, x is a number ranging from about 0.01 to about 0.4 and is representative of the number of moles of the metal M per mole of Al.sub.2 O.sub.3 y is a number equal to or greater than zero, and x is greater than y.

Abstract: Distillate fuels with excellent cold flow properties are produced from waxy Fischer-Tropsch products by separating the product into a heavier and a lighter fraction, isomerizing the heavier fraction, hydrotreating and isomerizing the lighter fraction, and recovering products in jet and diesel fuel ranges.

Abstract: High surface purity heat transfer solids are formed, suitably by washing and treating particulate refractory inorganic solids, notably alumina, which contains as impurities up to about 0.5 wt. % silicon and/or up to about 500 wppm boron, with an acid, or dilute acid solution sufficient to reduce the concentration of silicon and boron in the outer peripheral surface layer of the particles, e.g., as measured inwardly toward the center of a particle to a depth of about 50 .ANG. using X-ray photoelectron spectroscopy, to no greater than about 5 atom percent silicon and boron, preferably about 2 atom percent silicon and boron, based on the total number of cations within said outer peripheral surface layer, thereby reducing the tendency of said particles to sinter and agglomerate in the conversion of said hydrocarbon to hydrogen and carbon monoxide in a fluidized bed synthesis gas operation vis-a-vis particles otherwise similar except that the particles are not treated with the acid.

Abstract: Alumina heat transfer solids are admixed with a catalyst, or catalysts, and used in conducting high temperature fluidized bed reactions, particularly in a process for the production of hydrogen and carbon monoxide from a low molecular weight hydrocarbon by contact with a fluidized bed of catalyst and said heat transfer solids at high temperature in the presence of oxygen, or steam, or both oxygen and steam. The particulate heat transfer solids are characterized as having a performance index, PI, greater than 20, preferably greater than 40, as characterized by the formula PI=[(i).times.(ii).times.(iii).times.(iv)].sup.-1 where (i) the peripheral outer surface of the particle contains <5 atom % (Si+B) as impurities, and (ii) <20 atom % Na, Fe, Ca and Ti as impurities, where the bulk concentrations of the (Si+B) is sufficient to migrate into and contaminate the outer surface layer of the particles at process conditions. Moreover the (iii) tapped bulk density of the particles range from about 1.