TECHNOLOGY FOCUS - INSTRUMENTATION AND TESTING - Preferred Components: The system further comprises at least one recycling connection for recycling a portion of the liquid hydrocarbon compounds from the separation unit and/or fractionation unit back to the hydroprocessing reactors. The system comprises: one hydroprocessing reactor comprising catalyst, which is catalysts containing metals from group VI and/or VIII of the periodic system, and the catalyst is capable of converting biological feed material to fuel components; and a first hydroprocessing reactor and a second hydroprocessing reactor. The first hydroprocessing reactor comprises a first catalyst which is any catalyst containing metals from group VIII and/or VIB of the periodic system on a suitable support capable of converting hydrocarbons to n-paraffins. The first catalyst in the first hydroprocessing reactor is platinum, palladium, nickel, nickel molybdenum or cobalt molybdenum supported by alumina and/or silica. The second hydroprocessing reactor comprises a second catalyst which is platinum, palladium or nickel tungsten supported by aluminum oxide, zeolite, zeolite-aluminum oxide or aluminum oxide-silicon dioxide. The evaporation unit comprises one, two, three or more evaporators. The evaporators are evaporators which uses thin film evaporation technology, preferably thin film evaporator, falling film evaporator, short path evaporator or plate molecular still.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: The process further comprises a step for recycling a portion of the liquid hydrocarbon compounds obtained from the separation or fractionation back to the hydroprocessing. The evaporating is accomplished in one, two, three or more evaporation steps. The evaporating is performed in an evaporator using thin film evaporation technology, preferably thin film evaporator, falling film evaporator, short path evaporator or plate molecular still. The hydroprocessing is accomplished in: a single step and the catalyst containing metals from group VI and/or VIII, is capable of converting biological feed material to fuel components, where the catalyst is nickel-tungsten or a mixture or combination of nickel-tungsten or nickel molybdenum catalysts on a support comprising aluminum oxide, zeolite, zeolite-aluminum oxide or aluminum oxide-silicon dioxide; or two steps and the catalyst in the first step is any catalyst containing metals from group VIII and/or VIB of the periodic system on a suitable support capable of converting hydrocarbons to n-paraffins and the catalyst in the second step is a catalyst which is platinum, palladium or nickel tungsten supported by aluminum oxide, zeolite, zeolite-aluminum oxide or aluminum oxide-silicon dioxide. The evaporating comprises more than one evaporation steps and that the light components are removed from the first evaporation step. The condensate of the first evaporation step is recovered and fed to a second evaporation step. Preferred Components: The material of biological origin is: (i) any kind of fats, any kind of waxes, plant fats, plant oils, plant waxes, animal fats, animal oils, animal waxes, fish fats, fish oils and fish waxes; (ii) fatty acids or free fatty acids obtained from plant fats, plant oils, plant waxes, animal fats, animal oils, animal waxes, fish fats, fish oils and/or fish waxes by hydrolysis, transesterification or pyrolysis; (iii) esters obtained from plant fats, plant oils, plant waxes, animal fats, animal oils, animal waxes, fish fats, fish oils and/or fish waxes by transesterification; (iv) metal salts of fatty acids obtained from plant fats, plant oils, plant waxes, animal fats, animal oils, animal waxes, fish fats, fish oils and/or fish waxes by saponification; (v) anhydrides of fatty acids from plant fats, plant oils, plant waxes, animal fats, animal oils, animal waxes, fish fats, fish oils and/or fish waxes; (vi) esters obtained by esterification of free fatty acids of plant, animal and fish origin with alcohols; (vii) fatty alcohols or aldehydes 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; (viii) recycled food grade fats and oils, and fats, oils and waxes obtained by genetic engineering; (ix) dicarboxylic acids or polyols including diols, hydroxyketones, hydroxyaldehydes, hydroxycarboxylic acids or corresponding di- or multifunctional sulfur or nitrogen compounds; (x) compounds derived from algae, molds, yeasts, fungi and/or other microorganisms capable of producing compounds mentioned in (i)-(ix) or compounds similar to those; or (xi) mixtures of the material of biological origin. The material of biological origin is: offish oils e.g. baltic herring oil, salmon oil, herring oil, tuna oil, anchovy oil, sardine oil and mackerel oil; plant oils e.g. rapeseed oil, colza oil, canola oil, tall oil, crude tall oil, sunflower seed oil, soybean oil, corn oil, hemp oil, linen seed oil, olive oil, cottonseed oil, mustard oil, palm oil, peanut oil, castor oil, Jatropha seed oil, Pongamia pinnata seed oil, palm kernel oil and coconut oil; animal fats e.g. lard, tallow, rendered lard and rendered tallow, and waste and recycled food grade fats and oils, as well as fats, waxes and oils produced by genetic engineering; animal waxes e.g. bee wax, Chinese wax, shellac wax, and lanoline (wool wax); or plant waxes e.g. carnauba palm wax, ouricouri palm wax, jojoba seed oil, candelilla wax, esparto wax, japan wax, rice bran oil, terpenes, terpineols and/or triglycerides. The gaseous compounds separated comprise hydrogen gas, hydrogen sulfide, light fuel gases, and mainly lighter than 5C hydrocarbons. The obtained fuel components are a fraction containing gasoline and/or naphtha and a fraction containing middle distillate. EXAMPLE - Crude tall oil was fed from storage at 60 degrees C to an evaporation unit containing a thin film evaporator and a short path evaporator. The feed rate of the crude tall oil to the evaporation unit was 30-80 kg/hour. The temperature of the first evaporation step was 137 degrees C and the pressure was 18 mbar. Water, turpentine and light fatty acids were removed from the feed of crude tall oil. The first evaporation step was performed on a thin film evaporator. In the first evaporator, all together 3% of the original amount of crude tall oil was evaporated, of which 2% was turpentine and light fatty acids and 1% was water. 97% of the amount of the original feed of crude tall oil was recovered as condensate from the first evaporator and fed further to a second evaporator. The second evaporation step was performed on a short path evaporator at 315 degrees C and 0.3 mbar. 5% of the amount of the original feed was removed from the second evaporation step as a heavy fraction comprising pitch. Distillate was recovered from the second evaporating step and the amount of it was 92% of the amount of the original feed of crude tall oil.