TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: The process further comprises: (e) forming renewable hydrogen by at least one of (e1) dehydrogenating at least a portion of the linear butene formed in step (b) and/or at least one renewable 4-16C olefin isolated from the renewable 3-16C olefins formed in step (d), thus forming renewable 4-16C diene and renewable hydrogen, (e2) dehydrocyclizing at least a portion of at least one renewable 6-16C olefin isolated from the renewable 3-16C olefins formed in step (d), thus forming renewable 6-16C aromatics and renewable hydrogen (both preferred), and/or (e3) dehydrocyclizing at least a portion of renewable 6-16C diene isolated from the renewable 4-16C dienes formed in step (e1) to form renewable 6-16C aromatics and renewable hydrogen; and (f) hydrogenating at least a portion of the renewable 3-16C olefins with the renewable hydrogen formed in step (e), thus forming a renewable saturated hydrocarbon fuel or fuel additive. The reacting step (d) comprises: at least one reactions including disproportionation, metathesis, oligomerization, isomerization, alkylation, dehydrodimerization and/or dehydrocyclization; dimerizing at least a portion of the renewable isobutene, thus forming a renewable isobutene dimer mixture containing at least one 8C hydrocarbon including 2,4,4-trimethylpentene, 2,5-dimethylhexene and/or 2,5-dimethylhexadienes; trimerizing at least a portion of the renewable isobutene, thus forming a renewable isobutene trimer mixture containing at least one pentamethylheptene including 2,2,4,6,6-pentamethylheptene; tetramerizing at least a portion of the renewable isobutene, thus forming a renewable isobutene tetramer mixture containing at least one heptamethylnonene including 2,2,4,6,6,8,8-heptamethylnonene; isomerizing at least a portion of the renewable isobutene of step (b) to form an isobutene isomerization mixture comprising renewable 2-butene; and disproportionating at least a portion of the renewable ethylene formed in step (c) and at least a portion of the renewable 2-butene formed in step (b), thus forming renewable propylene. The reacting step (d) further comprises: disproportionating at least a portion of the renewable ethylene formed in step (c), and at least a portion of the renewable 2-butene and/or the renewable 2-butene formed by isomerizing at least a portion of the renewable isobutene of step (b), thus forming renewable propylene; mixing the renewable butene mixture and/or renewable ethylene with at least a portion of a non-renewable butene, a butene mixture and/or non-renewable renewable ethylene to form 3-16C olefins, where at least a portion of the 3-16C olefins are renewable; and oligomerizing the renewable butenes mixture and the renewable ethylene and/or renewable propylene to form the 3-16C olefins. In the process: the amount of dehydrogenating and/or dehydrocyclizing in step (e), and/or the amount of hydrogenating in step (f) are controlled so that the amount of renewable hydrogen formed in step (e) is essentially completely consumed in step (f); the renewable isobutanol and renewable ethanol are provided by fermentation; dehydrating in step (b) and dehydrating in step (c) are carried out separately; at least one renewable 6-8C olefin is isolated from the renewable 3-16C olefins formed in step (d); at least one renewable 6-8C dienes are formed in step (e1); at least a portion of the renewable isobutene dimer mixture and the renewable isobutene dimer mixture are hydrogenated in step (f), where the renewable saturated hydrocarbon fuel or fuel additive comprises isooctane; at least a portion of the renewable isobutene trimer mixture and the renewable isobutene trimer mixture are hydrogenated in step (f), where the renewable saturated hydrocarbon fuel or fuel additive comprises pentamethylheptanes; and at least a portion of the renewable isobutene dimer mixture is dehydrocyclized in step (e2), thus forming a dehydrocyclization product containing renewable p-xylene and hydrogen. The process further comprises: dimerizing the renewable propylene; and dehydrocyclizing at least a portion of the renewable propylene dimer, thus forming renewable benzene. Preferred Components: The renewable 4-16C olefins isolated from the renewable 3-16C olefins formed in step (d) comprise renewable linear butenes including renewable 1-butene, renewable cis-2-butene and/or renewable trans-2-butene. The renewable 4-16C dienes formed in step (e1) comprise butadiene. The renewable 6-16C aromatics formed in step (e2) comprise renewable aromatics including renewable benzene, renewable toluene and/or renewable xylene, where the renewable xylene comprises renewable p-xylene. EXAMPLE - Renewable wet isobutanol (containing 15% water and ~4% ethanol) obtained from fermentation was fed through a preheater and to a fixed-bed tubular reactor packed with a commercial gamma -alumina dehydration catalyst. The internal reactor temperature was maintained at 400 degrees C and the reactor pressure was atmospheric. The products were separated in a gas-liquid separator at 20 degrees C, where relatively pure water was removed as the liquid product. The gas phase product was dried over a molecular sieve bed. Gas chromatography-flame ionization detector of the gas phase effluent from the dehydration reactor was isobutylene (82%), linear butenes (13%) (mixture of 1-butene, and cis- and trans-2-butene), ethylene (4.5%), and propylene (0.5%). The flow of the gas-phase stream was 120 seem. This stream was combined with 120 seem of nitrogen and was fed through a preheater and to a fixed-bed tubular reactor packed with commercial chromium oxide (15 g) on alumina dehydrogenation catalyst. The weight hourly space velocity of the mixed butene stream was 1/hour. The internal reactor temperature was maintained at 600 degrees C and the reactor pressure was atmospheric to obtain butadiene.