Methods are provided for activation of catalysts comprising low amounts of a hydrogenation metal, such as low amounts of a Group 8-10 noble metal. The amount of hydrogenation metal on the catalyst can correspond to 0.5 wt % or less (with respect to the weight of the catalyst), or 0.1 wt % or less, or 0.05 wt % or less. Prior to loading a catalyst into a reactor, the corresponding catalyst precursor can be first activated in a hydrogen-containing atmosphere containing 1.0 vppm of CO or less. The thus first-activated catalyst can be transferred to a reactor with optional exposure to oxygen during the transfer, where it can be further activated using a hydrogen-containing atmosphere containing 3.0 vppm of CO or higher, to yield a twice-activated catalyst with high performance. The catalyst can be advantageously a transalkylation catalyst or an isomerization catalyst useful for converting aromatic hydrocarbons.

A method for the recovery paraxylene with reduced crystallization. Paraxylene is recovered from a mixture of C8 aromatic hydrocarbons in a pressure swing adsorption zone and a crystallization zone. The invention provides for lower throughput through the crystallization zone, resulting in lower capital costs, reduced electricity in operating separation equipment, as well as reduced refrigeration duty.

A method for the recovery paraxylene with reduced crystallization. Paraxylene is recovered from a mixture of C8 aromatic hydrocarbons in a pressure swing adsorption zone and a crystallization zone. The invention provides for lower throughput through the crystallization zone, resulting in lower capital costs, reduced electricity in operating separation equipment, as well as reduced refrigeration duty.

Disclosed herein are processes and systems that utilize olefin cross metathesis of triglycerides to produce jet fuel such as hydrocarbons with carbons numbers from C9 to C16. Jet range hydrocarbons may include paraffins, naphthenes, and aromatics with carbon numbers from 9 to 16 (C9-C16), and isomers thereof. The process described herein is versatile and may be suitable for producing jet range hydrocarbons from many different grades and sources of triglycerides. Further, the process described herein may be selective to jet range hydrocarbons which may result in increased yield as compared to hydrocracking or other processes for producing jet range hydrocarbons from triglycerides.

Disclosed herein are processes and systems that utilize olefin cross metathesis of triglycerides to produce jet fuel such as hydrocarbons with carbons numbers from C9 to C16. Jet range hydrocarbons may include paraffins, naphthenes, and aromatics with carbon numbers from 9 to 16 (C9-C16), and isomers thereof. The process described herein is versatile and may be suitable for producing jet range hydrocarbons from many different grades and sources of triglycerides. Further, the process described herein may be selective to jet range hydrocarbons which may result in increased yield as compared to hydrocracking or other processes for producing jet range hydrocarbons from triglycerides.

Processes for the hydrogenolysis of butane are described. A process can include (a) introducing a butane feed and hydrogen to a first hydrogenolysis reactor comprising a hydrogenolysis catalyst, and (b) contacting the butane feed and hydrogen with the hydrogenolysis catalyst at conditions sufficient to produce a first hydrogenolysis product stream. The introduction of the butane feed stream and hydrogen to the first hydrogenolysis reactor can be controlled to maintain a hydrogen to butane molar ratio in the reactor inlet of 0.3:1 to 0.8:1.

Processes for the hydrogenolysis of butane are described. A process can include (a) introducing a butane feed and hydrogen to a first hydrogenolysis reactor comprising a hydrogenolysis catalyst, and (b) contacting the butane feed and hydrogen with the hydrogenolysis catalyst at conditions sufficient to produce a first hydrogenolysis product stream. The introduction of the butane feed stream and hydrogen to the first hydrogenolysis reactor can be controlled to maintain a hydrogen to butane molar ratio in the reactor inlet of 0.3:1 to 0.8:1.

Processes for the hydrogenolysis of butane are described. A process can include (a) introducing a butane feed and hydrogen to a first hydrogenolysis reactor comprising a hydrogenolysis catalyst, and (b) contacting the butane feed and hydrogen with the hydrogenolysis catalyst at conditions sufficient to produce a first hydrogenolysis product stream. The introduction of the butane feed stream and hydrogen to the first hydrogenolysis reactor can be controlled to maintain a hydrogen to butane molar ratio in the reactor inlet of 0.3:1 to 0.8:1.

A method of making a xylene isomerization catalyst comprises the steps of (i) contacting a ZSM-5 zeolite starting material having a silica to alumina molar ratio of 20 to 50 and having a mesopore surface area in the range of 50 m.sup.2/gram to 200 m.sup.2/gram in a reactor with a base to provide an intermediate zeolite material; (ii) recovering the intermediate ZSM-5 zeolite material of step (i); (iii) contacting the intermediate zeolite material with an acid to provide an acid treated ZSM-5 zeolite product; (iv) recovering the acid treated ZSM-5 zeolite material; and (v) calcining the acid treated ZSM-5 zeolite material to provide a desilicated ZSM-5 zeolite product having a silica to alumina molar ratio of 20 to 150 and having a mesopore surface area in the range of 100 m.sup.2/gram to 400 m.sup.2/gram.

A method is disclosed for upgrading a bio-based material, the method including pretreating bio-renewable oil(s) and/or fat(s) to provide a bio-renewable raw material, deoxygenating the bio-renewable raw material, followed by separation, to provide a propane feed, and subjecting the propane feed to dehydrogenation and to separation to provide a propylene material.