A method for fluid catalytic cracking (FCC) of petroleum oil feedstock includes reacting the petroleum oil feedstock with a catalyst mixture in a reaction zone of an FCC unit to obtain a product stream including desulfurized hydrocarbon product, unreacted petroleum oil feedstock, and spent catalyst. During the reacting a process control system develops a process model based on data collected during the reacting, the process model characterizing a relationship among the feed rate of the base cracking catalyst, the feed rate of the FCC additive, the operating conditions, the composition of the product stream, and emissions from the reaction; and one or more of (i) a target feed rate of the base cracking catalyst, (ii) a target feed rate of the FCC additive, and (iii) one or more target operating conditions of the reaction in the reaction zone to reduce the emissions from the FCC unit and to increase a yield of the desulfurized hydrocarbon product in the product stream are determined.

Methylparaffins having limited methyl branching may be prepared by contacting at least one linear olefin with hydrogen in the presence of a dual-function supported catalyst comprising a solid acid component and a hydrogenation component under conditions sufficient to catalytically isomerize the at least one linear olefin into an intermediate product comprising one or more branched olefins, and hydrogenating the one or more branched olefins to form an isoparaffin product comprising one or more methylparaffins. Heat transfer fluids comprising such methylparaffins may be used in various thermal management systems, such as within various systems of electric vehicles, server farms, or other locales in need of efficient heat transfer.

The present invention concerns a method for processing a petrol containing sulfur and olefin compounds, comprising the following steps: a) a step of hydrodesulfurisation in the presence of a catalyst comprising an oxide support and an active phase comprising a metal from group VIB and a metal from group VIII, b) a step of separating the H.sub.2S formed, c) a step of hydrodesulfurisation at a higher temperature than that of step a), with a hydrogen/feedstock ratio less than that of step a), and in the presence of a hydrodesulfurisation catalyst comprising an oxide support and an active phase consisting of at least one metal from group VIII, d) a step of separating the H.sub.2S formed.

A process for hydrotreating recycled or renewable feedstocks with a catalytic microparticle slurry, and a process for manufacturing the catalytic microparticle slurry, are disclosed.

A bifunctional catalyst for example for conversion of oxygenates, the bifunctional catalyst comprising zeolite, alumina binder, Zn and P, wherein Zn is present at least partly as ZnAl.sub.2O.sub.4.

Petrochemical products may be produced from a hydrocarbon material by a process that may include separating the hydrocarbon material into at least a lesser boiling point fraction and a greater boiling point fraction, cracking the lesser boiling point fraction in a first reactor in the presence of a catalyst at a reaction temperature of from 500° C. to 700° C. to produce a first cracking reaction product, and cracking the greater boiling point fraction in a second reactor in the presence of the catalyst at a reaction temperature of from 500° C. to 700° C. to produce a second cracking reaction product. The hydrocarbon material may be crude oil. The first reactor may be a riser, and the second reactor may be a downer. The catalyst may be passed from the first reactor to the second reactor, from the second reactor to a regenerator, and from the regenerator to the first reactor, such that the catalyst is circulated between the first reactor, second reactor, and regenerator. An amount of coke may be reduced on the catalyst in the regenerator.

A catalyst regenerator for regenerating a coked catalyst produced along with a olefin by mixing naphtha and a catalyst with each other to cause a naphtha cracking reaction, and falling from a cyclone which separates the coked catalyst and the olefin produced from the naphtha cracking reaction, includes: a vessel accommodating a catalyst layer formed by stacking the catalyst; a partial oxidation burner producing a high-temperature gas containing solid carbon; and supply nozzles connected to the partial oxidation burner, installed on a bottom of the vessel toward the falling catalyst and the catalyst layer, and spraying the high-temperature gas containing the solid carbon to the catalyst and the catalyst layer.

A reverse water-gas shift catalyst that can be used at a high temperature is obtained, and a production method thereof is obtained. The reverse water-gas shift catalyst is obtained by at least supporting one or both of nickel and iron as a catalytically active component on a carrier containing a ceria-based metal oxide or a zirconia-based metal oxide as a main component, and a ratio of the carrier to the entire catalyst is 55% by weight or more.

This invention relates to an additive capable of increasing the gasoline octane (by 2-3 units) with minimum loss of gasoline. More specifically, the present invention discloses a fluid catalytic cracking additive composition capable of enhancing gasoline octane, said composition comprising 5-50 wt. % zeolite component, 0-15 wt % alumina, 5-20 wt % colloidal silica, 10-60 wt % kaolin clay, 5-15 wt % phosphate, and 0.1 to 5.0 wt. % of bivalent metal selected from Group-IIA or Group-IB, wherein the zeolite component comprises of medium pore pentasil zeolite in an amount of 1 to 50 wt. % and said zeolite consists of one or more MFI topology zeolite having SiO.sub.2/Al.sub.2O.sub.3 mole ratio in the range of 10-280. The present invention also discloses a process for preparation of the additive.

The present disclosure relates to an FCC catalyst composition and a process for preparing the same. In a first aspect, there is provided an FCC catalyst composition comprising 25 to 45 wt % Y-type zeolite, 20 to 40 wt % silicon oxide, 5 to 25 wt % alumina, 5 to 35 wt % of at least one clay and 0.5 to 3 wt % of at least one rare earth oxide. The weight % of each of the component is with respect to the total weight of the composition. The FCC catalyst composition has an average particle size in the range of 45-120μ. In a second aspect, there is provided a process for preparing the FCC catalyst composition, which uses ball milled pseudoboehmite having an average particle size in the range of 1 to 8 micron and the whole process is carried out at a pH value in the range of 6 to 7.