A method for processing a chemical stream includes contacting a feed stream with a catalyst in a reactor portion of a reactor system that includes a reactor portion and a catalyst processing portion. The catalyst includes platinum, gallium, or both and contacting the feed stream with the catalyst causes a reaction which forms an effluent stream. The method includes separating the effluent stream from the catalyst, passing the catalyst to the catalyst processing portion, and processing the catalyst in the catalyst processing portion. Processing the catalyst includes passing the catalyst to a combustor, combusting a supplemental fuel in the combustor to heat the catalyst, treating the heated catalyst with an oxygen-containing gas to produce a reactivated catalyst, and passing the reactivated catalyst from the catalyst processing portion to the reactor portion. The supplemental fuel may include a molar ratio of hydrogen to other combustible fuels of at least 1:1.

Provided is a method for producing a lithium transition metal oxide, comprising, A) mixing a lithium salt and a precursor, adding the mixture into a reactor for precalcination; the lithium salt has a particle size D50 of 10-20 μm and the precursor has a particle size D50 of 1-20 μm, and the precursor is one or more selected from transition metal oxyhydroxide, transition metal hydroxide and transition metal carbonate; and B) adding the product obtained from the precalcination into a fluidized bed reactor, subjecting to a first calcination and a second calcination to obtain the lithium transition metal oxide. Raw materials for the lithium transition metal oxide further includes a main-group metal compound containing oxygen, which is added in the precalcination, the first calcination or the second calcination; and the main-group metal compound containing oxygen has an average particle size of 10-100 nm. A fluidized bed reactor is also provided.

Provided is a method for producing a lithium transition metal oxide, comprising, A) mixing a lithium salt and a precursor, adding the mixture into a reactor for precalcination; the lithium salt has a particle size D50 of 10-20 μm and the precursor has a particle size D50 of 1-20 μm, and the precursor is one or more selected from transition metal oxyhydroxide, transition metal hydroxide and transition metal carbonate; and B) adding the product obtained from the precalcination into a fluidized bed reactor, subjecting to a first calcination and a second calcination to obtain the lithium transition metal oxide. Raw materials for the lithium transition metal oxide further includes a main-group metal compound containing oxygen, which is added in the precalcination, the first calcination or the second calcination; and the main-group metal compound containing oxygen has an average particle size of 10-100 nm. A fluidized bed reactor is also provided.

A method for recovering an active metal of a lithium secondary battery according to exemplary embodiments comprises preparing a preliminary cathode active material mixture including a lithium composite oxide and a binder, forming a cathode active material mixture by removing the binder from the preliminary cathode active material mixture through a heat treatment in a fluidized bed reactor, and recovering a lithium precursor from the cathode active material mixture. Accordingly, the active metal of the lithium secondary battery can be recovered with high purity and high efficiency.

The invention provides a slow-release material comprising particles, wherein the particles comprise a core comprising an active component and a multilayer shell, wherein the multi-layer shell comprises a molecular layer deposition (MLD) multi-layer, wherein the active component comprises one or more of a pharmaceutical compound and a nutraceutical compound, for use in the treatment of a disease.

A process for producing direct reduced iron (“DRI”) from iron ore and biomass in a single stage fluidised bed includes injecting (a) iron ore, (b) gaseous oxygen and (c) a solid reductant including biomass into a reaction zone of the fluidized bed operating in a temperature range of 750-850#C and reducing iron ore and forming DRI in the fluidized bed and discharging DRI having a metallisation of at least 70% from the fluidised bed.

Systems for preparing butenes are provided. The systems can include a reactor inlet coupled to both a reactor and at least one reactant reservoir; at least one of the reactant reservoirs containing one or both of an aldehyde and/or ethanol; a catalyst within the reactor, the catalyst comprising a metal component and an acidic support material; and a reactor outlet operationally configured to convey a butene-rich reaction product to a product reservoir. Methods for preparing butenes are also provided. The methods can include exposing one or both of ethanol and/or an aldehyde to a catalyst comprising a metal component and an acidic support to form a butene-rich product that comprises one or both of 1-butene and/or 2-butene.

Systems for preparing butenes are provided. The systems can include a reactor inlet coupled to both a reactor and at least one reactant reservoir; at least one of the reactant reservoirs containing one or both of an aldehyde and/or ethanol; a catalyst within the reactor, the catalyst comprising a metal component and an acidic support material; and a reactor outlet operationally configured to convey a butene-rich reaction product to a product reservoir. Methods for preparing butenes are also provided. The methods can include exposing one or both of ethanol and/or an aldehyde to a catalyst comprising a metal component and an acidic support to form a butene-rich product that comprises one or both of 1-butene and/or 2-butene.

Polyolefin polymerization performed by contacting in a reactor an olefin monomer and optionally a comonomer with a catalyst system in the presence of induced condensing agents (ICA) and optionally hydrogen. The ICA may include two or more ICA components where the composition of the ICA (i.e., the concentration of each ICA component) may affect the polyolefin production rate. Changes to the relative concentration of the two or more ICA components may be according to ICA equivalency factors that allow for increasing the polyolefin production rate while maintain a sticking temperature, increasing polyolefin production rate while increasing the dew point approach temperature of the ICA, or a combination thereof.

Polyolefin polymerization performed by contacting in a reactor an olefin monomer and optionally a comonomer with a catalyst system in the presence of induced condensing agents (ICA) and optionally hydrogen. The ICA may include two or more ICA components where the composition of the ICA (i.e., the concentration of each ICA component) may affect the polyolefin production rate. Changes to the relative concentration of the two or more ICA components may be according to ICA equivalency factors that allow for increasing the polyolefin production rate while maintain a sticking temperature, increasing polyolefin production rate while increasing the dew point approach temperature of the ICA, or a combination thereof.