Systems for separating a contaminant trapping additive from a cracking catalyst may include a contaminant removal vessel having one or more fluid connections for receiving contaminated cracking catalyst, contaminated contaminant trapping additive, fresh contaminant trapping additive, and a fluidizing gas. In the contaminant removal vessel, the spent catalyst may be contacted with contaminant trapping additive, which may have an average particle size and/or density greater than the cracking catalyst. A separator may be provided for separating an overhead stream from the contaminant removal vessel into a first stream comprising cracking catalyst and lifting gas and a second stream comprising contaminant trapping additive. A recycle line may be used for transferring contaminant trapping additive recovered in the second separator to the contaminant removal vessel, allowing contaminant trapping additive to accumulate in the contaminant removal vessel. A bottoms product line may provide for recovering contaminant trapping additive from the contaminant removal vessel.

Embodiments of apparatuses and methods for controlling heat for rapid thermal processing of carbonaceous material are provided herein. The apparatus comprises a reheater for containing a fluidized bubbling bed comprising an oxygen-containing gas, inorganic heat carrier particles, and char and for burning the char into ash to form heated inorganic particles. An inorganic particle cooler is in fluid communication with the reheater to receive a first portion of the heated inorganic particles. The inorganic particle cooler is configured to receive a cooling medium for indirect heat exchange with the first portion of the heated inorganic particles to form first partially-cooled heated inorganic particles that are fluidly communicated to the reheater and combined with a second portion of the heated inorganic particles to form second partially-cooled heated inorganic particles. A reactor is in fluid communication with the reheater to receive the second partially-cooled heated inorganic particles.

Embodiments of apparatuses and methods for controlling heat for rapid thermal processing of carbonaceous material are provided herein. The apparatus comprises a reheater for containing a fluidized bubbling bed comprising an oxygen-containing gas, inorganic heat carrier particles, and char and for burning the char into ash to form heated inorganic particles. An inorganic particle cooler is in fluid communication with the reheater to receive a first portion of the heated inorganic particles. The inorganic particle cooler is configured to receive a cooling medium for indirect heat exchange with the first portion of the heated inorganic particles to form first partially-cooled heated inorganic particles that are fluidly communicated to the reheater and combined with a second portion of the heated inorganic particles to form second partially-cooled heated inorganic particles. A reactor is in fluid communication with the reheater to receive the second partially-cooled heated inorganic particles.

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor.

The invention is a method for chemical looping (CLC) oxidation-reduction combustion of liquid hydrocarbon feedstocks carried out in a fluidized bed. A liquid hydrocarbon feedstock (2) is partly vaporized on contact with a hot particle solid (1) to form a partly vaporized liquid feedstock and to form coke on the solid prior to contacting partial vaporized liquid feedstock (19) with a redox active mass of particles (12) to achieve combustion of the partially vaporized liquid feed (19). The hot solid particles can notably be from a second fluidized-bed particle circulation loop.

The invention is a method for chemical looping (CLC) oxidation-reduction combustion of liquid hydrocarbon feedstocks carried out in a fluidized bed. A liquid hydrocarbon feedstock (2) is partly vaporized on contact with a hot particle solid (1) to form a partly vaporized liquid feedstock and to form coke on the solid prior to contacting partial vaporized liquid feedstock (19) with a redox active mass of particles (12) to achieve combustion of the partially vaporized liquid feed (19). The hot solid particles can notably be from a second fluidized-bed particle circulation loop.

The invention relates to a method for drying a wet polymer composition obtained from a polymerization process, comprising: a) introducing the wet polymer composition and a drying gas into a fluidized bed dryer to form a fluidized bed of the wet polymer composition and b) heating the fluidized bed to obtain a dry polymer composition, wherein the fluidized bed further comprises an anti-fouling agent comprising inert nanoparticles.

The invention relates to a method for drying a wet polymer composition obtained from a polymerization process, comprising: a) introducing the wet polymer composition and a drying gas into a fluidized bed dryer to form a fluidized bed of the wet polymer composition and b) heating the fluidized bed to obtain a dry polymer composition, wherein the fluidized bed further comprises an anti-fouling agent comprising inert nanoparticles.

A reactor configuration is proposed for selectively converting gaseous, liquid or solid fuels to a syngas specification which is flexible in terms of H.sub.2/CO ratio. This reactor and system configuration can be used with a specific oxygen carrier to hydro-carbon fuel molar ratio, a specific range of operating temperatures and pressures, and a co-current downward moving bed system. The concept of a CO.sub.2 stream injected in-conjunction with the specified operating parameters for a moving bed reducer is claimed, wherein the injection location in the reactor system is flexible for both steam and CO.sub.2 such that, carbon efficiency of the system is maximized.

A bio-reforming reactor receives biomass to generate chemical grade syngas for a coupled downstream train of any of 1) a methanol-synthesis-reactor train, 2) a methanol-to-gasoline reactor train, and 3) a high-temperature Fischer-Tropsch reactor train, that use this syngas derived from the biomass in the bio-reforming reactor. A renewable carbon content of the produced gasoline, jet fuel, and/or diesel derived from the coupled downstream trains of any of 1) the methanol-synthesis-reactor train, 2) the methanol-to-gasoline reactor train, or 3) the high-temperature Fischer-Tropsch reactor train are optimized for recovery of renewable carbon content to produce fuel products with 100% biogenic carbon content and/or fuel products with 50-100% biogenic carbon content. A carbon-dioxide gas feedback loop cooperates with a CO2 separation unit to supply a fraction of the CO2 gas that is removed from the chemical grade syngas produced from the reactor output of the BRR to supply extracted CO2 gas to the biomass feed system.