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. The process provides increased yields of upgraded hydrocarbon products that possess the characteristics of a liquid transportation fuel or a blend component thereof.

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 oligomerization catalyst to provide enhanced yields of aliphatic hydrocarbons that possess the characteristics of a blend component of a liquid transportation fuel or other value-added chemical products.

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 oligomerization catalyst to provide enhanced yields of aliphatic hydrocarbons that possess the characteristics of a blend component of a liquid transportation fuel or other value-added chemical products.

A diamondoid fuel comprising a cage structure including 10, 14, 18, or 22 carbons. The diamondoid fuel also includes one of one to four cyclopropyl groups bonded to the cage structure or two to four functional groups bonded to the cage structure where the functional groups are an alkyl group, an allyl group, a cyclopropyl group, or combinations thereof. Additionally, at least one functional group is an allyl group and at least one functional group is a cyclopropyl group.

A diamondoid fuel comprising a cage structure including 10, 14, 18, or 22 carbons. The diamondoid fuel also includes one of one to four cyclopropyl groups bonded to the cage structure or two to four functional groups bonded to the cage structure where the functional groups are an alkyl group, an allyl group, a cyclopropyl group, or combinations thereof. Additionally, at least one functional group is an allyl group and at least one functional group is a cyclopropyl group.

Processes for producing neopentane are disclosed herein. Processes comprise demethylating a C.sub.6-C.sub.8 alkane within a shell and tube reactor to produce a demethylation product including at least 10 wt % neopentane based on the weight of the demethylation product.

Processes for producing neopentane are disclosed herein. Processes comprise demethylating a C.sub.6-C.sub.8 alkane within a shell and tube reactor to produce a demethylation product including at least 10 wt % neopentane based on the weight of the demethylation product.

Processes for co-production of methyl tertiary-butyl ether (MTBE) and alkylate is disclosed. The process includes comprising passing a hydrocarbon feed stream comprising C.sub.4 hydrocarbons to a dehydrogenation unit to generate a dehydrogenation effluent comprising C.sub.4 olefins. The dehydrogenation effluent is passed to a MTBE unit to provide a mixed stream comprising C.sub.4 olefins and MTBE. The mixed stream is separated to provide an MTBE product stream and a fractionator overhead stream comprising olefins. The fractionator overhead stream is passed to an alkylation unit to produce an alkylation product stream comprising an alkylate.

An alkylation process including an upfront isomerization zone is described. 100% n-butane or field butanes can be converted into a blend of approximately 60 wt % isobutane and 40 wt % n-butane in the isomerization zone. This blend can be used as the feed to all types of alkylation zones. It stabilizes the feed composition so that the dehydrogenation zone and alkylation zone always operate with the same feed.

An alkylation process including an upfront isomerization zone is described. 100% n-butane or field butanes can be converted into a blend of approximately 60 wt % isobutane and 40 wt % n-butane in the isomerization zone. This blend can be used as the feed to all types of alkylation zones. It stabilizes the feed composition so that the dehydrogenation zone and alkylation zone always operate with the same feed.