Methods for operating a system having two downflow high-severity FCC units for producing products from a hydrocarbon feed includes introducing the hydrocarbon feed to a feed separator and separating it into a lesser boiling point fraction and a greater boiling point fraction. The greater boiling point fraction is passed to the first FCC unit and cracked in the presence of a first catalyst at 500 C. to 700 C. to produce a first cracking reaction product and a spent first catalyst. The lesser boiling point fraction is passed to the second FCC unit and cracked in the presence of a second catalyst at 500 C. to 700 C. to produce a second cracking reaction product and a spent second catalyst. At least a portion of the spent first catalyst or the spent second catalyst is passed back to the first FCC unit, the second FCC unit or both.

Methods for operating a system having two downflow high-severity FCC units for producing products from a hydrocarbon feed includes introducing the hydrocarbon feed to a feed separator and separating it into a lesser boiling point fraction and a greater boiling point fraction. The greater boiling point fraction is passed to the first FCC unit and cracked in the presence of a first catalyst at 500 C. to 700 C. to produce a first cracking reaction product and a spent first catalyst. The lesser boiling point fraction is passed to the second FCC unit and cracked in the presence of a second catalyst at 500 C. to 700 C. to produce a second cracking reaction product and a spent second catalyst. At least a portion of the spent first catalyst or the spent second catalyst is passed back to the first FCC unit, the second FCC unit or both.

Flash chemical ionizing pyrolysis (FCIP) process. The FCIP includes mixing an iron source material, an alkali or alkaline earth metal chloride source material, an aqueous phase, and an oil component to form a feed emulsion; introducing the feed emulsion into an FCIP reactor at a temperature greater than about 400 C. up to about 600 C., a pressure from 10 to 50 psia and a residence time of 0.1 to 10 seconds, to form an FCIP effluent; and condensing a liquid ionizing pyrolyzate (LIP) from the effluent. The feed emulsion can be free of added solids other than the iron source material, the alkali or alkaline earth metal chloride source material, and any sediment in the oil component.

Flash chemical ionizing pyrolysis (FCIP) process. The FCIP includes mixing an iron source material, an alkali or alkaline earth metal chloride source material, an aqueous phase, and an oil component to form a feed emulsion; introducing the feed emulsion into an FCIP reactor at a temperature greater than about 400 C. up to about 600 C., a pressure from 10 to 50 psia and a residence time of 0.1 to 10 seconds, to form an FCIP effluent; and condensing a liquid ionizing pyrolyzate (LIP) from the effluent. The feed emulsion can be free of added solids other than the iron source material, the alkali or alkaline earth metal chloride source material, and any sediment in the oil component.

Methods of chemical looping include introducing a hydrocarbon-containing feed stream into a first reaction zone. The first reaction zone includes a moving catalyst bed reactor. The moving catalyst bed reactor includes a heterogeneous catalyst, and the heterogeneous catalyst includes a heat-generating metal oxide component. The method further includes cracking the hydrocarbon-containing feed stream in the presence of the heterogeneous catalyst of the moving catalyst bed reactor, reducing the metal oxide heat-generating component of the heterogeneous catalyst with hydrogen from a product stream to generate heat, and utilizing the heat to drive additional cracking of the hydrocarbon-containing feed stream. A chemical looping system includes at least one reduction reactor, which includes a moving catalyst bed reactor and a heterogeneous catalyst, and at least one oxidation reactor fluidly coupled to the reduction reactor.

Methods of chemical looping include introducing a hydrocarbon-containing feed stream into a first reaction zone. The first reaction zone includes a moving catalyst bed reactor. The moving catalyst bed reactor includes a heterogeneous catalyst, and the heterogeneous catalyst includes a heat-generating metal oxide component. The method further includes cracking the hydrocarbon-containing feed stream in the presence of the heterogeneous catalyst of the moving catalyst bed reactor, reducing the metal oxide heat-generating component of the heterogeneous catalyst with hydrogen from a product stream to generate heat, and utilizing the heat to drive additional cracking of the hydrocarbon-containing feed stream. A chemical looping system includes at least one reduction reactor, which includes a moving catalyst bed reactor and a heterogeneous catalyst, and at least one oxidation reactor fluidly coupled to the reduction reactor.

Novel catalysts comprising nickel oxide nanoparticles supported on alumina nanoparticles, methods of their manufacture, heavy oil compositions contacted by these nanocatalysts and methods of their use are disclosed. The novel nanocatalysts are useful, inter alia, in the upgrading of heavy oil fractions or as aids in oil recovery from well reservoirs or downstream processing.

Novel catalysts comprising nickel oxide nanoparticles supported on alumina nanoparticles, methods of their manufacture, heavy oil compositions contacted by these nanocatalysts and methods of their use are disclosed. The novel nanocatalysts are useful, inter alia, in the upgrading of heavy oil fractions or as aids in oil recovery from well reservoirs or downstream processing.

Novel catalysts comprising nickel oxide nanoparticles supported on alumina nanoparticles, methods of their manufacture, heavy oil compositions contacted by these nanocatalysts and methods of their use are disclosed. The novel nanocatalysts are useful, inter alia, in the upgrading of heavy oil fractions or as aids in oil recovery from steam-assisted well reservoirs.

Novel catalysts comprising nickel oxide nanoparticles supported on alumina nanoparticles, methods of their manufacture, heavy oil compositions contacted by these nanocatalysts and methods of their use are disclosed. The novel nanocatalysts are useful, inter alia, in the upgrading of heavy oil fractions or as aids in oil recovery from steam-assisted well reservoirs.