A cyclic metals deactivation system unit for the production of equilibrium catalyst materials including a cracker vessel configured for cracking and stripping a catalyst material; and a regenerator vessel in fluid communication with the cracker vessel, the regenerator vessel configured for regeneration and steam deactivation of the catalyst material.

In an apparatus for fluid catalytic cracking a riser having a top and a bottom for fluidizing and cracking a hydrocarbon feed stream by contact with catalyst exits an outlet at the top of the riser. A downer in communication with the outlet of the riser receives cracked hydrocarbon product and catalyst. A swirl duct in communication with the downer has a discharge opening below the outlet for discharging said cracked hydrocarbon product and catalyst. A stream of hydrocarbon feed and a catalyst is passed upwardly in a riser. A stream of gaseous hydrocarbon products and catalyst is directedly downwardly and then the stream of gaseous hydrocarbon products and catalyst are directed to flow in an angular direction to separate gaseous hydrocarbon products from the catalyst.

A process for the hydroconversion of heavy oil products includes the following steps where heavy oil products and hydrogen are supplied to a slurry hydroconversion section having a molybdenum-based catalyst: separating the reaction effluent into a vapour phase and a slurry phase; and sending the slurry phase to a separation section having the function of separating the Vacuum Gas Oil, Heavy Vacuum Gas Oil, Light Vacuum Gas Oil, and Atmospheric Gas Oil fractions, from a stream of heavy organic products which contains asphaltenes, unconverted feed, catalyst, and solid formed during the hydroconversion reaction. This stream is partly sent to the reaction section and partly forms a purge stream, which is heated and made fluid between 185° C.-220° C., and subjected to a static settling unit up to at least 100° C. From the settling unit two new products, clarified component and cake, are obtained. The clarified component is recycled to the hydroconversion reaction section.

The present disclosure is directed to a non-destructive process for removing metals, metal ions and metal oxides in alumina-based materials without destroying alumina, allowing the regeneration of alumina-based catalysts. The non-destructive process uses an extracting agent that sequesters metals, metal ions and/or metal oxides present in alumina-based materials without destroying the alumina, allowing the regeneration of alumina-based catalysts.

A process for recovering catalyst from a fluidized catalytic reactor effluent is disclosed comprising reacting a reactant stream by contact with a stream of fluidized catalyst to provide a vaporous reactor effluent stream comprising catalyst and products. The vaporous reactor effluent stream is contacted with a liquid coolant stream to cool it and transfer the catalyst into the liquid coolant stream. A catalyst lean vaporous reactor effluent stream is separated from a catalyst rich liquid coolant stream. A return catalyst stream is separated from the catalyst rich liquid coolant stream to provide a catalyst lean liquid coolant stream, and the return catalyst stream is transported back to said reacting step.

Processes of catalytically pyrolyzing solid hydrocarbonaceous materials in a downflow fluid bed reactor and regenerating the catalyst in an upflow fluidized bed reactor are described. Systems and compositions useful in the catalytic pyrolysis of plastics are also described.

A cyclic metals deactivation system unit for the production of equilibrium catalyst materials including a cracker vessel configured for cracking and stripping a catalyst material; and a regenerator vessel in fluid communication with the cracker vessel, the regenerator vessel configured for regeneration and steam deactivation of the catalyst material.

A process for rejuvenating an at least partially spent catalyst resulting from a hydrodesulfurization process of a sulfur-containing olefinic gasoline cut, where the at least partially spent catalyst result is from a fresh catalyst a metal from group VIII, a metal from group VIb, and an oxide support, where the process includes a) regenerating the at least partially spent catalyst in an oxygen-containing gas stream at a temperature between 350° C. and 550° C., b) the regenerated catalyst is brought into contact with an impregnation solution containing a compound containing a metal from group VIb, the molar ratio of the metal from group VIb added per metal from group VIb already present in the regenerated catalyst being between 0.15 and 2.5 mol/mol, c) a drying stage is carried out at a temperature of less than 200° C., and
the use of the rejuvenated catalyst in a hydrodesulfurization process.

A process for the hydroconversion of heavy oil products includes the following steps where heavy oil products and hydrogen are supplied to a slurry hydroconversion section having a molybdenum-based catalyst: separating the reaction effluent into a vapour phase and a slurry phase; and sending the slurry phase to a separation section having the function of separating the Vacuum Gas Oil, Heavy Vacuum Gas Oil, Light Vacuum Gas Oil, and Atmospheric Gas Oil fractions, from a stream of heavy organic products which contains asphaltenes, unconverted feed, catalyst, and solid formed during the hydroconversion reaction. This stream is partly sent to the reaction section and partly forms a purge stream, which is heated and made fluid between 185° C.-220° C., and subjected to a static settling unit up to at least 100° C. From the settling unit two new products, clarified component and cake, are obtained. The clarified component is recycled to the hydroconversion reaction section.

A liquid-solid radial moving bed reaction apparatus and a solid acid alkylation process by using the liquid-solid radial moving bed reaction apparatus, the liquid-solid radial moving bed reaction apparatus comprises:

A radial moving bed reactor, a spent catalyst receiver, a catalyst regenerator, and a regenerated catalyst receiver that are successively connected, wherein the catalyst discharging outlet of the regenerated catalyst receiver is communicated with the catalyst inlet of the radial moving bed reactor; a reaction stream distribution zone, a catalyst bed, and a stream-after-the-reaction collection zone are arranged in the radial moving bed reactor from the inside to the outside or from the outside to the inside, the reaction stream distribution zone is communicated with the reaction stream feeding pipeline; the stream-after-the-reaction collection zone is communicated with the stream-after-the-reaction withdrawing pipe;

A component-based mixer is arranged on the reaction stream feeding pipeline; the component-based mixer consists of an upper recycled stream pipe, a lower reaction stream feeding pipe, and a fresh feedstock feeding pipe extending into the reaction stream feeding pipeline, a nozzle of the feeding pipe is arranged at the outlet of the fresh feedstock feeding pipe, a filler and/or a mixing fin is arranged in the reaction stream feeding pipeline, wherein the component-based mixer is located out of the radial moving bed reactor.