TECHNOLOGY FOCUS - CHEMICAL ENGINEERING - Preferred Process: The butane and hexane fractions are isomerized. Alkylate gasoline is formed from the butane fraction.The process is repeated with unreacted pentanes.At least a portion of the hexane paraffins is subjected to a reforming process.The reforming process is AROMAX(TM) process, or a platforming or rheniforming process.At least a portion of feedstock is obtained from natural gas, a cracked gas fed, the distillation of crude oil, hydrocracker, or an isomerization unit. It is treated to remove impurities from hydrogen, methane, ethane, olefins, or heteroatoms    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Component: Butane fraction can also be isobutane.    TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Component: The (de)hydrogenation catalyst includes at least one metal or a corresponding metal compound from iron, cobalt, nickel, ruthenium, rhodium, osmium, iridium, or preferably platinum and/or palladium or their compounds.The (de)hydrogenation catalyst also contains rhenium, tin, germanium, gallium, lead, tin, and/or their compounds.The (de)hydrogenation catalyst can be a mixture of platinum-on-alumina.The olefin metathesis catalyst comprises a metal or metal compound from tungsten (preferably), molybdenum, tin, or rhenium, preferably tungsten-on-silica.Preferred Composition: The volumetric ratio of the platinum component to the tungsten component is more than 1:50 and less than 50:1, preferably 1:10-10:1.The amount of platinum on alumina is 0.01-10, preferably 0.1-5 wt.%.The amount of tungsten on the silica is 0.01-50, preferably 0.1-20 wt.%. EXAMPLE - A molecular redistribution catalyst was prepared by mixing (de)hydrogenation catalyst component (3.1 cm3) and an olefin metathesis component (0.9 cm3). The mixture (4 cm3) was loaded into a stainless steel reactor and dried in nitrogen flow (100 cm3/min) from room temperature to 400 degreesF for 1 hour. It was reduced in hydrogen flow (100 cm3/min) at 400-900 degreesF for 1 hour and holding it at 900 degreesF for 12 hours. It was purged with a nitrogen flow for 1 hour and cooled to the reaction temperature. The reactor was pressurized at 2000 psig with nitrogen. The nitrogen was switched to a hydrocarbon feed comprising pentane or isopentane delivered at 2 or 4 cm3/hr. The results showed that the molecular redistribution reaction was able to convert the pentane and isopentane to butane and hexane products with small amounts of isomerization with a normal pentane feed and small amounts of normal products with an isopentane feed.