TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Catalyst: The catalyst is selected from alumina, silica-alumina, hafnia, titania and/or zirconia. The hydrotreating catalyst is selected from cobalt (Co), molybdenum (Mo), nickel (Ni), titanium (Ti), tungsten (W), zinc (Zn), antimony (Sb), bismuth (Bi), cerium (Ce), vanadium (V), niobium (Nb), tantalum (Ta), chromium (Cr), manganese (Mn), rhenium (Re), iron (Fe), platinum (Pt), iridium (Ir), palladium (Pd), osmium (Os), rhodium (Rh), ruthenium (Ru), nickel, copper impregnated zinc oxide (Cu/ZnO), copper impregnated chromium oxide (Cu/Cr), nickel aluminum oxide (Ni/Al2O3), palladium aluminum oxide (Pd/Al2O3), cobalt molybdenum (CoMo), nickel molybdenum (NiMo), nickel molybdenum tungsten (NiMoW), sulfided cobalt molybdenum (CoMo), sulfided nickel molybdenum (NiMo) and/or metal carbides.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: The product mixture of step (a) additionally comprises solid residue, and unreacted quantity of the alcohol species. The process further involves a step prior to step (a) for pyrolyzing a biomass to form the pyrolysis oil of step (a). The reacting of step (a) is performed at 150-500 (preferably 250-500) degrees C, a pressure of 500-4000 (preferably 1500-4000) psig, and for a duration of 2-240 (preferably 15-120) minutes. The reaction conditions of step (b) include a temperature of 120-450 (preferably 150-350) degrees C and a pressure of 500-3500 (preferably 800-1500) psig. The contacting of step (b) is first performed at 120-200 degrees C, followed by contacting at a higher temperature of 200-450 degrees C. The process further involves a separation step, where the solid residue is separated out from the product mixture using a separator. The separation step is performed by filtration, extraction, decantation and/or centrifugation, and where the separator is selected from gas-liquid, liquid-liquid, three-phase, horizontal, vertical, tubular, rotary, turbine and/or centrifugal. The process further involves a step for recovering the unreacted quantity of the alcohol species from the product mixture of step (a), and recycling at least a portion of the unreacted quantity as feed for step (a). The reacting of step (a) occurs in the presence of a catalyst (preferably solid catalyst). The feed is formed from biomass through fermentation processes, where the mass ratio of the pyrolysis oil to the feed is 0.05-10. The contacting of step (b) is performed in the presence of a high boiling point hydrocarbon solvent in addition to the hydrogen, to produce fuel range hydrocarbon products and excess hydrocarbon solvent. The excess hydrocarbon solvent is separated from the fuel range hydrocarbons product and recycled as at least a portion of the high boiling point hydrocarbon solvent used in step (b). Preferred Components: The feed comprises 1-30C alcohols (preferably methanol, ethanol, butanol, tetrahydrofurfuryl alcohol, ethylene glycol, propylene glycol, glycerol and/or fatty alcohols). The high boiling point hydrocarbon solvent is selected from diesel oil, atmospheric gas oil, vacuum gas oil, cracked stock gas oils such as light cycle oil, heavy cycle oil, fluid catalytic cracking decant oil, coker gas oil, thermal cracking distillate, visbreaking distillate and/or other refinery stream comprising predominantly 11-25C hydrocarbons. EXAMPLE - No suitable example given.