In a reactor I a catalyst support impregnated with a solution of cobalt nitrate is oxidized at a calcining temperature comprised between 400 C. and 450 C. in order to produce a catalyst precursor comprising cobalt oxides. This catalyst precursor is contacted in reduction reactor A with reducing gas rich in hydrogen and with a low water content, by circulating the flow of reducing gas, so as to reduce the cobalt oxides to Co and to produce water. Water content is reduced to 200 ppmvol of the flow of reducing gas laden with water recovered at the outlet of the reactor A, and at least a part of the flow of reducing gas is recycled to the reactor A. In the process, the reducing gas is maintained at a water content less than 10,000 ppmvol in reactor A.

Catalysts and methods for catalytic hydrogenolysis of a polymer. The method comprises a) activating a catalyst with a hydrogen source to provide an activated catalyst, wherein the catalyst comprises: i) a MXene support of Formula I: M.sub.n+1X.sub.nT.sub.x (I); wherein each M is independently an early transition metal; X is carbon or nitrogen; T.sub.x is a surface functional group wherein x is 0-10; and n is 1, 2, 3, or 4; and ii) a supported metal, wherein loading of the supported metal on the MXene support is less than 5% w/w based on the weight of the catalyst; and b) contacting a mixture of the activated catalyst, hydrogen gas, and a polymer at a temperature of at least about 200 C. for a period of time that is sufficient for catalytic hydrogenolysis of the polymer; thereby converting the polymer to a fuel.

A fluidized bed reactor system including a fluidized bed reactor configured to receive a heated light hydrocarbon feed stream flowing upwards and a heated regenerated catalyst at a temperature sufficient to crack the heated light hydrocarbon feed stream to produce a product effluent stream containing hydrogen and spent catalyst having coke deposits, a catalyst regeneration unit operatively connected to a bottom portion of the fluidized bed reactor, the catalyst regeneration unit being configured to receive the spent catalyst flowing downwards and combust the coke deposits to produce the heated regenerated catalyst and a heated gas effluent for generating the heated light hydrocarbon feed stream, and a riser externally attached to the fluidized bed reactor and the catalyst regeneration unit, the riser being configured to receive the heated regenerated catalyst and a gas-based stream to flow the heated regenerated catalyst upwards to the fluidized bed reactor.

System and method for mixing a catalyst precursor into a carrier oil to form a diluted precursor mixture and mixing the diluted precursor mixture with a hydrocarbon feedstock to form a conditioned hydrocarbon feedstock containing at least one nonpetroleum-derived hydrocarbon material. Suitable mixing apparatus include static inline and high shear mixers. The conditioned hydrocarbon feedstock can be heated to thermally decompose the catalyst precursor and form dispersed active catalyst particles in situ. At least one of the carrier oil or hydrocarbon feedstock comprises a nonpetroleum-derived hydrocarbon material selected from biomass-derived material, nonpetroleum-derived oil or fat, polymer, fabric or textile, paper or cardboard, rubber, waste product, pyrolysis product of one or more of the foregoing, and combinations thereof. The hydrocarbon feedstock may be provided by primary and secondary hydrocarbon feedstocks that differ from each other by at least one of chemical composition, polarity, solubility, or physical state.

The application discloses a device and method for preparing aromatic hydrocarbons from naphtha, and the device comprises a fluidized bed reactor and a riser reactor; the fluidized bed reactor is used for introducing a naphtha raw material to make contact with a catalyst from the riser reactor and react to generate a BTX-containing product gas stream and a spent catalyst, the product gas stream is subjected to gas-solid separation, the product gas stream after separation is sent to a downstream working section, and unconverted naphtha after separation returns to the fluidized bed reactor as a raw material; and a part of low-carbon alkanes after separation return to the riser reactor as raw materials and are further converted into aromatic hydrocarbons and other components. According to the application, by connecting a high-temperature riser reactor and a relatively low-temperature fluidized bed reactor in series, a yield of low-carbon alkane is reduced and a yield of aromatic hydrocarbons is increased; and linear-chain and branched-chain aliphatic hydrocarbons can be efficiently converted into the aromatic hydrocarbons in a highly selective mode, and a content of p-xylene in a xylene mixture is greater than 50 wt %.

A method for converting hydrocarbons in a hydrocarbon stream includes contacting the hydrocarbon stream with steam and a catalyst system under steam enhanced catalytic cracking conditions to produce an effluent comprising olefins. The catalyst system includes a framework-substituted pentasil zeolite. The framework-substituted pentasil zeolite has a modified pentasil framework. The modified pentasil framework includes a pentasil aluminosilicate framework in which a portion of framework aluminum atoms of the pentasil aluminosilicate framework are substituted with Ce atoms and Fe atoms. At least a portion of the Fe atoms are monomeric.

A process for upgrading plastics to olefins, paraffins, and aromatics with a core-shell catalyst in a fluidized bed reactor is described.

A solid particle bed has a sea zone and at least one island zone distributed in the sea zone, and has an upper surface, a lower surface, an axial direction and a radial direction. The island zone extends along the axial direction of the solid particle bed but does not extend to the lower surface, and the voidage of the island zone is 110-300% of the voidage of the sea zone. In the solid particle bed, the oil preferentially enters the packing area with a small voidage through the tail section of the packing area with a large voidage. As the deposition amount increases, the oil gradually changes its way by entering the packing area with a small voidage through the side of the packing area with a large voidage.

Processes for activation of hydrogenolysis catalysts are described. A process can include contacting an oxidized catalyst with a butane containing stream in the presence of H.sub.2 to form a treated catalyst. The treated catalyst can then be contacted with H.sub.2 to form an activated hydrogenolysis catalyst. The source of the oxidized catalyst can be a fresh catalyst or deactivated catalyst that has been exposed to, for example, oxygen. Uses of the activated hydrogenolysis catalyst are also described.

The present invention relates to a process for the in situ regeneration of a hydroconversion catalyst. The invention also relates to a hydroconversion process comprising said regeneration process. The invention also relates to a system comprising a reaction section (40) comprising a hydroconversion reactor operating as an ebullating bed or as a moving bed; a regeneration section comprising a regeneration device (100); means for transfer of the hydroconversion catalyst between said reaction section (40) and said regeneration section comprising at least one fluidic connection; means for charging said regeneration device (100) as a fluidized bed or as a moving bed.