TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Catalyst: The acidic catalyst for dehydrating and the acidic catalyst for oligomerizing are selected from inorganic acids, and/or their metal salt(s).    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: The dehydrating is carried out in the presence of a dehydration catalyst, the oligomerizing is carried out in the presence of an oligomerization catalyst, and the hydrogenating is carried out in the presence of a hydrogenation catalyst; or the dehydrating and/or oligomerizing are carried out in the presence of an acidic catalyst, where the acidic catalyst for dehydrating and the acidic catalyst for oligomerizing is the same or different. Each of the dehydrating, oligomerizing, and hydrogenating are carried out in a different reaction zone, or greater than or equal to 2 of the dehydrating, oligomerizing, and hydrogenating are carried out in the same reaction zone. The process (P1) further involves removing the 2-6C alcohols from the feedstock before the dehydrating, where the removing involves carrying out the fermenting in step (b) below atmospheric pressure, so that aqueous 2-6C alcohol vapor is removed; and separating at least a portion of the product comprising at least one 12C and at least one 16C unsaturated oligomers produced in step (d), combining the separated portion with the dehydration product of step (c) prior to the oligomerization step, and adjusting the ratio of 12C and 16C saturated alkanes provided by step (e) by recycling at least a portion of the 8C unsaturated oligomers formed in step (d) back to the oligomerization step, to increase the amount of 16C unsaturated oligomers. The process (P1a) further involves combining the renewable jet fuel blendstock and the conventional jet fuel blendstock with at least one 10-14C aromatic hydrocarbon. Preferred Catalyst: At least one of the dehydration catalyst, oligomerization catalyst, or hydrogenation catalyst is heterogeneous catalysts, or homogeneous catalysts. The acidic catalyst for dehydrating and acidic catalyst for oligomerizing are selected from organic sulfonic acids, heteropolyacids, perfluoroalkyl sulfonic acids, and/or their metal salt(s) (preferably Amberlyst-35 (RTM: strongly acidic ion exchange resin for heterogeneous acid catalysis). The hydrogenating is carried out in the presence of a hydrogenation catalyst selected from iridium, platinum, palladium, rhodium, nickel, ruthenium, rhenium and cobalt, and/or their compounds. Preferred Composition: The renewable SPK blendstock produced by the process (P1) comprises 12C saturated alkanes (at least 60 mol%), and 16C saturated alkanes (at least 10 mol%). In the renewable SPK blendstock produced by the process (P1a), the ratio of the renewable jet fuel blendstock to the conventional jet fuel blendstock is (0:100 to 50:50, preferably 10:90 to 50:50, especially 30:70 to 50:50, particularly 40:60 to 50:50). EXAMPLE - Three surrogate blends were prepared using mixtures of 2,2,4,6,6-pentamethylheptane (12C) and 2,2,4,6,6,8,8-heptamethylnonane (16C). The mixtures were prepared at ratios of 90% 12C/10% 16C, 70% 12C /30% 16C, and 50% 12C/50% 16C. These ratios were chosen to simulate wide range of possible compositions of renewable synthesized paraffinic kerosene (SPK) jet blendstocks. The distillation curves for the three surrogate fuels were evaluated. A narrow boiling Jet A-1 petroleum-derived base fuel was chosen for blending with the SPK to demonstrate blending for the extreme case, where the boiling point range of conventional jet fuel had relatively high sensitivity to added SPK. This base jet fuel alone did not meet distillation slope requirements of T50 minus T10 of greater than 22 degrees C for a semi-synthetic jet fuel blend as specified by ASTM D7566 10a. The three surrogate mixtures were blended at 50% conventional Jet A-1 with 50% of the surrogate mixture. The resulting distillation curves and impact on distillation slope requirements were measured. For particular base fuel, all three surrogate compositions resulted in a fuel that met the T90 minus T10 distillation slope requirements of ASTM D7566 10a. However, only the 50/50 surrogate resulted in a final blend that met the T50 minus T10 distillation curve requirements of ASTM D7566 10a.