A method of producing a fuel additive includes passing a feed stream comprising C4 hydrocarbons through a methyl tertiary butyl ether unit producing a first process stream; passing the first process stream through a selective hydrogenation unit producing a second process stream; passing the second process stream through an isomerization unit producing a third process stream; and passing the third process stream through a hydration unit producing the fuel additive and a recycle stream.

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.

Provided herein is a unique process that prepares a saturated hydrocarbon mixture with well-controlled structural characteristics that address the performance requirements driven by the stricter environmental and fuel economy regulations for automotive engine oils. The process allows for the branching characteristics of the hydrocarbon molecules to be controlled so as to consistently provide a composition that has a surprising CCS viscosity at 35 C. (ASTM D5329) and Noack volatility (ASTM D5800) relationship. The process comprises providing a specific olefinic feedstock, oligomerizing in the presence of a BF.sub.3 catalyst, and hydroisomerizing in the presence of a noble-metal impregnated, 10-member ring zeolite catalyst.

The invention provides a process for preparing a fluid having a boiling point in the range of from 150 to 260 C. and comprising more than 80% by weight of isoparaffins and less than 50 ppm of aromatics, comprising the step of catalytically hydrogenating a feed comprising more than 85% by weight of oligomerized olefins, at a temperature from 115 to 195 C. and at a pressure from 30 to 70 bars. The invention also provides the fluid obtainable by the process of the invention and the use of said fluid.

Processes for producing olefins include passing a hydrocarbon feed to a hydrocarbon cracking unit that cracks the hydrocarbon feed to produce a cracker effluent, passing the cracker effluent to a cracker effluent separation system that separates the cracker effluent to produce at least a cracking C4 effluent including 1-butene, 1,3-butadiene, and isobutene, passing the cracking C4 effluent to an SHIU that contacts the cracking C4 effluent with hydrogen in the presence of a selective hydrogenation catalyst to produce a hydrogenation effluent having a 2-butenes concentration greater than or equal to the sum of the concentrations of 1-butene and isobutene. The processes include passing the hydrogenation effluent to a metathesis unit that contacts the hydrogenation effluent with a metathesis catalyst and a cracking catalyst downstream of the metathesis catalyst to produce a metathesis reaction effluent comprising at least propene.

Processes for producing olefins include passing a hydrocarbon feed to a hydrocarbon cracking unit that cracks the hydrocarbon feed to produce a cracker effluent, passing the cracker effluent to a cracker effluent separation system that separates the cracker effluent to produce at least a cracking C4 effluent including 1-butene, 1,3-butadiene, and isobutene, passing the cracking C4 effluent to an SHIU that contacts the cracking C4 effluent with hydrogen in the presence of a selective hydrogenation catalyst to produce a hydrogenation effluent having a 2-butenes concentration greater than or equal to the sum of the concentrations of 1-butene and isobutene. The processes include passing the hydrogenation effluent to a metathesis unit that contacts the hydrogenation effluent with a metathesis catalyst and a cracking catalyst downstream of the metathesis catalyst to produce a metathesis reaction effluent comprising at least propene.

The invention relates to an efficient, high-throughput method of converting monoterpenes to high performance aviation fuel blendstocks. The method is a one pot, two-step process that includes a dehydration step followed by a hydrogenation step. Both steps can proceed without the use of solvents. Use of biosynthetically generated monoterpenes by this method produces sustainable aviation fuel blendstocks having applications that include use as a full-performance or an ultra-performance jet fuel blendstock.

The invention relates to an efficient, high-throughput method of converting monoterpenes to high performance aviation fuel blendstocks. The method is a one pot, two-step process that includes a dehydration step followed by a hydrogenation step. Both steps can proceed without the use of solvents. Use of biosynthetically generated monoterpenes by this method produces sustainable aviation fuel blendstocks having applications that include use as a full-performance or an ultra-performance jet fuel blendstock.

The invention relates to a process for producing benzene comprising the steps of: (a) providing a hydrocracking feed stream comprising C.sub.5-C.sub.12 hydrocarbons, (b) contacting the hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst under process conditions including a temperature of 425-580 C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 3-30 h.sup.1 to produce a hydrocracking product stream comprising BTX and (c) separating the BTX from the hydrocracking product stream, wherein the hydrocracking catalyst comprises a shaped body comprising a zeolite and a binder and a hydrogenation metal deposited on the shaped body, wherein the amount of the hydrogenation metal is 0.010-0.30 wt-% with respect to the total catalyst and wherein the zeolite is ZSM-5 having a silica (SiO.sub.2) to alumina (Al.sub.2O.sub.3) molar ratio of 25-75.