TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Catalyst: The hydrodeoxygenation catalyst and the catalyst in the pre-hydrogenation step is palladium (Pd), platinum (Pt), nickel (Ni), nickel-molybdenum (NiMo) or cobalt-molybdenum (CoMo) catalyst having an alumina and/or silica support. The decarboxylation/decarbonylation catalyst is Pd, Pt, Ni, NiMo or CoMo catalyst having alumina and/or silica support or activated carbon support. The isomerization catalyst is a supported catalyst containing a molecular sieve and a metal of the Group VIII of the Periodic Table of the elements.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Components: The feedstock comprises at least one component selected from 4-24C carboxylic acids, 12-24C carboxylic acids esters, 1-3C alcohols, 12-24C carboxylic acid anhydrides, and 12-24C alcohols. The feedstock comprises at least one starting material of biological origin selected from triglycerides, fatty acids, fatty acids esters, alcohols, fatty acid anhydrides, and fatty alcohols. The starting material is plant fats, plant oils, plant waxes, animal fats, animal oils, animal waxes, fish fats, fish oils and/or fish waxes; free fatty acids or fatty acids obtained by hydrolysis, acid transesterification or pyrolysis reactions from the plant fats, plant oils, plant waxes, animal fats, animal oils, animal waxes, fish fats, fish oils and/or fish waxes; esters obtained by transesterification from plant fats, plant oils, plant waxes, animal fats, animal oils, animal waxes, fish fats, fish oils and/or fish waxes; esters obtained by esterification of free fatty acids of plant, animal and/or fish origin with alcohols; fatty alcohols obtained as reduction products of fatty acids from plant fats, plant oils, plant waxes, animal fats, animal oils, animal waxes, fish fats, fish oils and/or fish waxes; and/or waste and recycled food grade fats and oils, and fats, oils and/or waxes obtained by genetic engineering. The feedstock contains unsaturated and/or polyunsaturated compounds (at least 80 wt.%). Preferred Process: The oligomerization is carried out under a pressure of 0 - 10 MPa and at 100 - 500degreesC in the presence of cationic clay catalyst (preferably zeolite catalyst). In the method, up to 10 (preferably 0.1 - 4) wt.% of water is added to the feedstock containing carboxylic acids in the oligomerization step. The deoxygenation is carried out as hydrodeoxygenation or as decarbonylation/decarboxylation, where the deoxygenation is carried out prior to, or following oligomerization. The hydrodeoxygenation is carried out in the presence of hydrogen at a temperature of 100 - 500degreesC, under a pressure of 0 - 20 MPa, the flow rate of weight hourly spaced viscosity (WHSV) of 0.1 - 10 l/hour in the presence of hydrodeoxygenation catalyst. Prior to hydrodeoxygenation, the product from the oligomerization step is subjected to pre-hydrogenation in the presence of a catalyst at 50 - 400degreesC under a hydrogen pressure of 0.1 - 20 MPa, and the flow rate WHSV of 0.1 - 10 l/hour. In the method, the feedstock of the process or the product of the oligomerization step is subjected to decarboxylation/decarbonylation in the presence of decarboxylation/decarbonylation catalyst at 200 - 400degreesC, pressure of 0 - 20 MPa, the flow rate WHSV of 0.1 - 10 l/hour. Following oligomerization and deoxygenation steps, the product is subjected to isomerization in the presence of hydrogen gas under a pressure of 0.1 - 20 MPa, at 100 - 500degreesC in the presence of isomerization catalyst. Preferred Oil: The base oil comprises (wt.%): saturated hydrocarbons (at least 95, preferably at least 97), mononaphthenes (20 - 80, preferably 20 - 60), linear paraffin (not greater than10, preferably not greater than5), where at least 75 (preferably at least 90) wt.% of the saturated hydrocarbons ar not greater than9C hydrocarbons. The base oil has up to 7C (preferably up to 3C). EXAMPLE - Feedstock containing soybean oil (200 ml), montmorillonite catalyst (6 g), and distilled water (5 ml), was loaded in reactor. The temperature was increased to 270degreesC. The oil was oligomerized while slowly mixing for 7 hours. In the hydrodeoxygenation step, the mixture oligomerized above was hydrogenated in the high-pressure reactor using dried and activated NiMo/Al2O3 catalyst to yield i-paraffin. Oligomerized soy oil mixture (200 ml) was hydrogenated at 325degreesC, under a hydrogen pressure of 5 MPa, until no acid groups were detected in the Fourier Transform Infra Red (FTIR) spectrum of the sample. The reaction mixture was mixed at 300 revolutions per minute. The final product was distilled, and was found to be branched and cyclic 36C paraffin having kinematic viscosity (KV100) of 5.2 mm2/second; viscosity index of 113; and pour point of -9degreesC.