A process for producing methyl tert-butyl ether (MTBE) comprising introducing a butane feed stream (n-butane, i-butane) and hydrogen to a hydrogenolysis reactor comprising a hydrogenolysis catalyst to produce a hydrogenolysis product stream comprising hydrogen, methane, ethane, propane, i-butane, and optionally n-butane; separating the hydrogenolysis product stream into a first hydrogen-containing stream, an optional methane stream, a C.sub.2 to C.sub.3 gas stream (ethane, propane), and a butane stream (i-butane, optionally n-butane); feeding the butane stream to a dehydrogenation reactor to produce a dehydrogenation product stream, wherein the dehydrogenation reactor comprises a dehydrogenation catalyst, and wherein the dehydrogenation product stream comprises hydrogen, i-butane, and isobutylene; and feeding the dehydrogenation product stream and methanol to an etherification unit to produce an unreacted methanol stream, an unreacted isobutylene stream, and an MTBE stream.

Catalysts and processes for producing catalysts for neopentane production are provided herein. A process includes reducing a catalyst precursor comprising a transition metal and an inorganic support at a temperature less than 500° C. to produce a catalyst. Also provided herein are processes to produce neopentane using the catalysts described herein and neopentane compositions produced therefrom.

Catalysts and processes for producing catalysts for neopentane production are provided herein. A process includes reducing a catalyst precursor comprising a transition metal and an inorganic support at a temperature less than 500° C. to produce a catalyst. Also provided herein are processes to produce neopentane using the catalysts described herein and neopentane compositions produced therefrom.

Catalysts and processes for producing catalysts for neopentane production are provided herein. A process includes reducing a catalyst precursor comprising a transition metal and an inorganic support at a temperature less than 500° C. to produce a catalyst. Also provided herein are processes to produce neopentane using the catalysts described herein and neopentane compositions produced therefrom.

A catalyst comprising Y.sub.2O.sub.3 nanorods and gold nanoparticles dispersed on a surface of the nanorods is provided. The gold is present at a concentration of 0.5-2 wt %. A method of forming olefins by oxidative cracking is also provided. The method includes reacting an alkane with a reactant gas mixture in the presence of a catalyst under conditions suitable for forming light olefins (ethtylene and propylene).

A catalyst comprising Y.sub.2O.sub.3 nanorods and gold nanoparticles dispersed on a surface of the nanorods is provided. The gold is present at a concentration of 0.5-2 wt %. A method of forming olefins by oxidative cracking is also provided. The method includes reacting an alkane with a reactant gas mixture in the presence of a catalyst under conditions suitable for forming light olefins (ethtylene and propylene).

Disclosed herein are processes for producing neopentane. The processes generally relate to demethylating isooctane to produce neopentane. The isooctane may be provided by the alkylation of isobutane with butylenes.

Disclosed herein are processes for producing neopentane. The processes generally relate to demethylating isooctane to produce neopentane. The isooctane may be provided by the alkylation of isobutane with butylenes.

Disclosed herein are processes for producing neopentane. The processes generally relate to demethylating isooctane to produce neopentane. The isooctane may be provided by the alkylation of isobutane with butylenes.

The present disclosure relates generally to processes and systems for producing liquid transportation fuels by converting a feed stream that comprises both isopentane and n-pentane, and optionally, some C6+ hydrocarbons. Isopentane and smaller hydrocarbons are separated to form a first fraction while n-pentane and larger components of the feed stock form a second fraction. Each fraction is then catalytically-activated in a separate reaction zone with a separate catalyst, where the conditions maintained in each zone maximize the conversion of each fraction to olefins and aromatics, while minimizing the production of C1-C4 light paraffins. In certain embodiments, the first fraction is activated at a lower temperature than the second fraction. Certain embodiments additionally comprise mixing at least a portion of the two effluents and contacting with an alkylation catalyst to provide enhanced yields of mono-alkylated aromatics that are suitable for use as a blend component of liquid transportation fuels or other value-added chemical products.