The present invention relates to a hydrocarbon conversion catalyst, comprising: a first composition comprising a dehydrogenation active metal on a solid support, and a second composition comprising a transition metal and a doping agent, wherein the doping agent is selected from zinc, gallium, indium, lanthanum, and mixtures thereof, on an inorganic support.

Hydrocarbon composition plays vital role in fuel quality. For gasoline/motor spirit applications the hydrocarbon should have more octane-possessing molecules from the groups of aromatics, naphthenics and isoparaffins, while n-paraffins are not preferred due to their poor octane. Among the high-octane groups, again aromatics occupy the top but not more than 35 vol % aromatics can be mixed in gasoline for engine applications to avoid harmful emission, But there is no single process that addresses so far the issue of co-producing all the desired hydrocarbon components in a single process. Thus, it is interesting to have a single once-through process working on single catalyst system to produce mixture of all three high-octane molecules namely, aromatics, naphthenics and isoparaffins directly from low-value, low-octane n-paraffin feed. Herein, we report a novel single-step catalytic process for the simultaneous production of aromatics, naphthenics and isoparaffins for gasoline and petrochemical applications.

A C.sub.10 hydrocarbon composition of greater than 55 wt. % C.sub.10 mono-olefins containing from 11 to 45 wt. % 1-decene, at least 0.5 wt. % 2-butyl-1-hexene, at least 1 wt. % 3-propyl-1-heptene, from 0.5 to 12 wt. % 4-ethyl-1-octene, at least 4 wt. % 4-penten-1-yl-cyclopentane, and from 2 to 40 wt. % 5-methyl-1-nonene. A C.sub.12 hydrocarbon composition of greater than 60 wt. % C.sub.12 mono-olefins containing at least 8 wt. % 1-dodecene and at least 0.5 wt. % 6-hepten-1-yl-cyclopentane, and the composition also containing heptylcyclopentane and n-dodecane at a weight ratio of heptylcyclopentane to n-dodecane from 0:3:1 to 8:1. A C.sub.14 hydrocarbon composition of greater than 60 wt. % C.sub.14 mono-olefins containing at least 12 wt. % 1-tetradecene and at least 0.5 wt. % 8-nonen-1-yl-cyclopentane, and the composition also containing from 3 to 30 wt. % of n-tetradecane and nonylcyclopentane.

Systems and processes are disclosed for producing petrochemical products, such as ethylene, propene and other olefins from crude oil in high severity fluid catalytic cracking (HSFCC) units. Processes include separating a crude oil into a light fraction and a heavy fraction, cracking the light fraction and heavy fraction in separation separate cracking reaction zones, and regenerating the cracking catalysts in a two-zone having a first regeneration zone for the first catalyst (heavy fraction) and a second regeneration zone for the second catalyst (light fraction) separate from the first regeneration zone. Flue gas from the first catalyst regeneration zone is passed to the second regeneration zone to provide additional heat to raise the temperature of the second catalyst of the light fraction side. The disclosed systems and processes enable different catalysts and operating conditions to be utilized for the light fraction and the heavy fraction of a crude oil feed.

New/fresh catalyst is added to a dehydrogenation unit and aged catalyst is removed from the dehydrogenation unit on a continuous or semi-continuous basis while the dehydrogenation unit is in operation. The conversion achieved by the higher activity catalyst results in the production rate of olefin product being maintained at near start-of-run production for longer, with a slower rate of decline. The higher activity catalyst extends run time, reduces feed consumption for each unit of olefin product, and minimizes fresh catalyst expenses.

According to one more embodiments, petrochemical products may be produced from a hydrocarbon material by a process that may comprise separating the hydrocarbon material into at least a lesser boiling point fraction, a medium boiling point fraction, and a greater boiling point fraction. The process may further comprise cracking at least a portion of the lesser boiling point fraction and the medium boiling point fraction in a second reactor unit in the presence of a second catalyst at a reaction temperature of from 500° C. to 700° C. to produce a second cracking reaction product, wherein the lesser boiling point fraction enters the second reactor unit upstream of wherein the medium boiling point fraction enters the second reactor.

Methods are provided for refining natural oil feedstocks. The methods comprise reacting the feedstock in the presence of a metathesis catalyst under conditions sufficient to form a metathesized product comprising olefins and esters. In certain embodiments, the methods further comprise separating the olefins from the esters in the metathesized product. In certain embodiments, the methods further comprise hydrogenating the olefins under conditions sufficient to form a fuel composition. In certain embodiments, the methods further comprise transesterifying the esters in the presence of an alcohol to form a transesterified product.

Disclosed herein is a fluid catalyst cracking (FCC) catalyst composition that includes a first component and a second component. The first component includes zeolite Y and a first matrix that includes a metal passivating constituent. The second component includes beta zeolite and a second matrix. Also disclosed herein are methods of preparing the FCC catalyst composition and method of using the FCC catalyst composition.

A high-temperature plastic pyrolysis process that can produce high yields of ethylene, propylene and other light olefins from waste plastics is disclosed. The plastic feed is pyrolyzed at a high temperature of about 600 to about 900° C. directly to monomers, such as ethylene and propylene. During pyrolysis, the plastic feed is contacted with a diluent gas stream at a mole ratio of carbon feed to diluent gas of 0.6 to 20.

A high-temperature plastic pyrolysis process that can produce high yields of ethylene, propylene and other light olefins from waste plastics is disclosed. The plastic feed is pyrolyzed at a high temperature of about 600 to about 900° C. directly to monomers, such as ethylene and propylene. The pyrolysis reaction can be conducted in a fluidized manner which requires separation of heat carrier particles from pyrolysis gases.