A process to efficiently convert organic feedstock material into liquid non-oxygenated hydrocarbons in the C.sub.5 to C.sub.12 carbon skeleton range is disclosed. The process can utilize gaseous, liquid or solid organic feedstocks containing carbon, hydrogen and, optionally, oxygen. The feedstock may require preparation of the organic feedstock for the process and is converted first into a synthesis gas containing carbon monoxide and hydrogen. The synthesis gas is then cleaned and conditioned and extraneous components removed, leaving substantially only the carbon monoxide and hydrogen. It is then converted via a series of chemical reactions into the desired liquid hydrocarbons. The hydrocarbons are suitable for combustion in a vehicle engine and may be regarded a replacement for petrol made from fossil fuels in the C.sub.5 to C.sub.2 carbon backbone range. The process also recycles gaseous by-products back through the various reactors of the process to maximize the liquid hydrocarbon in the C.sub.5 to C.sub.12 carbon skeleton range yield.

A hydrogenolysis bimetallic supported catalyst comprising a first metal, a second metal, and a zeolitic support; wherein the first metal and the second metal are different; and wherein the first metal and the second metal can each independently be selected from the group consisting of iridium (Ir), platinum (Pt), rhodium (Rh), ruthenium (Ru), palladium (Pd), molybdenum (Mo), tungsten (W), nickel (Ni), and cobalt (Co).

A process for producing a monoalkylated benzene comprises the step of contacting benzene with a mixture comprising dialkylated and trialkylated benzenes in the presence of a transalkylation catalyst composition under transalkylation conditions effective to convert at least part of the dialkylated and trialkylated benzene to monoalkylated benzene, wherein the transalkylation catalyst, composition comprises zeolite beta having an external surface in excess of 350 m2/g as determined by the t-plot method for nitrogen physisorption.

According to one or more embodiments of the present disclosure, chemical streams may be processed by a method which may comprise operating a first chemical process, stopping the first chemical process and removing the first catalyst from the reactor, and operating a second chemical process. The reaction of the first chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The reaction of the second chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The first reaction and the second reaction may be different types of reactions.

Methods for cracking a hydrocarbon feed stream include contacting a hydrocarbon feed stream with a catalyst system in a catalytic cracking unit having a flowing gas stream to obtain a cracking product containing light olefins. The catalyst system includes at least a base catalyst. The base catalyst includes a pentasil zeolite. The pentasil zeolite includes from 0.01% to 5% by mass lithium atoms, as calculated on an oxide basis, based on the total mass of the pentasil zeolite. The flowing gas stream comprises hydrogen and, optionally, at least one additional carrier gas.

Processes for converting one or more C.sub.1-C.sub.5 linear or branched alcohols to one or more C.sub.2-C.sub.5 olefins are provided. In one exemplary embodiment, the process can be a single stage process for the direct conversion of C.sub.1-C.sub.5 alcohols to olefinic mixtures (e.g., C.sub.2-C.sub.5) carried out in a reactor using a catalyst that includes zeolite doped with boron and phosphor. Systems for carrying out these processes are also provided.

A catalyst for dehydrogenation of hydrocarbons includes a support including zirconium oxide and Linde type L zeolite (L-zeolite). A concentration of the zirconium oxide in the catalyst is in a range of from 0.1 weight percent (wt. %) to 20 wt. %. The catalyst includes from 5 wt. % to 15 wt. % of an alkali metal or alkaline earth metal. The catalyst includes from 0.1 wt. % to 10 wt. % of tin. The catalyst includes from 0.1 wt. % to 8 wt. % of a platinum group metal. The alkali metal or alkaline earth metal, tin, and platinum group metal are disposed on the support.

A method of producing p-xylene comprising the steps of separating the reformate feed in the reformate splitter to produce a benzene stream, a combined heavy stream, a xylene stream, and a toluene stream, converting the C9+ aromatic hydrocarbons in the presence of a dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, separating the dealkylation effluent in the dealkylation splitter to produce a C9 stream and a C10+ stream, reacting the C9 stream, the toluene stream, the benzene stream, and the hydrogen stream in the presence of a transalkylation catalyst in the transalkylation reactor to produce a transalkylation effluent, separating the p-xylenes from the xylene stream in the p-xylene separation unit to produce a p-xylene product and a p-xylene depleted stream, converting the m-xylene and o-xylene in the p-xylene depleted stream in the isomerization unit to produce an isomerization effluent.

The invention relates to C.sub.5+ hydrocarbon conversion. More particularly, the invention relates to separating a vapor phase product and a liquid phase product from a heated mixture that includes steam and C.sub.5+ hydrocarbons, catalytically cracking the liquid phase product and steam cracking the vapor phase product.

This disclosure provides improved processes for converting benzene/toluene via methylation with methanol/dimethyl ether for producing, e.g., p-xylene. In an embodiment, a process comprises contacting a methylation agent feed with an aromatic hydrocarbon feed in the presence of a methylation catalyst in a methylation reactor at increased pressure. Reduced methylation catalyst deactivation can be achieved with increased pressure in the methylation reactor.