TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Components: The hydrogen-rich gas is hydrogen-recycle gas stream and/or hydrogen make-up. The hydrodeoxygenation catalyst is Mo supported on alumina. The hydrotreating catalyst comprises metal component i.e. group VIII and/or VI of Periodic System and is supported on carrier containing alumina, silica and/or titania. The hydroisomerization treatment catalyst comprises metal component i.e. group VIII and/or VI of Periodic System and is supported on carrier containing alumina, silica, titania, silica-alumina, ZSM-5 and/or zeolite beta .    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Components: The renewable organic material comprises triglycerides, fatty acids, resin acids and/or fatty acid esters. Preferred Method: The method further comprises passing effluent stream from second step to hydrotreating stage by contacting stream with hydrotreating catalyst; and passing effluent streams to hydroisomerization stage by contacting stream with hydroisomerization catalyst. The hydrodeoxygenation step is carried out at 50-350 degrees C under hydrogen pressure of 1-200 bar and liquid hourly space velocity of 0.1-10/hour. The effluent is separated into liquid effluent stream and gaseous effluent stream. The liquid effluent stream is mixed with fresh hydrogen-rich gas. A purified hydrogen-containing gas stream is formed by removing hydrogen sulfide, ammonia, carbon monoxide, carbon dioxide and light hydrocarbons from gaseous effluent. The purified hydrogen-containing gas recycled. The steps are carried out in the same or in separate hydroprocessing reactors. The hydrotreating step and hydroisomerization step are carried out at 50-450/oC under hydrogen pressure of 1-200 bar and at liquid hourly space velocity of 0.1-10/hour. EXAMPLE - An amorphous alumina powder (1000 g) was mixed with water (850 g) for 10 minutes and extruded in 1/16 inches trilobe shape. The extrudates were dried and calcined for 2 hours at 600 degrees C. The carrier was impregnated with basic solution of ammonium dimolybdate (ADM), dried, and calcined at 400 degrees C for 2 hours. The amount of ADM was adjusted to produce catalyst with 3 wt.% molybdenum content. The catalyst (100 ml) was loaded in isothermal pilot plant reactor. A straight-run fossil diesel spiked with tert-butyl disulfide was used for sulfiding catalyst. As feedstock, rapeseed oil (15 vol.%) mixed with straight run fossil light gas oil (LGO, 85 vol.%) was mixed with hydrogen gas and passed over catalyst. The complete conversion of rapeseed oil was evidenced by removal of all material (triglycerides) boiling above 405 degrees C. The yield of propane was 0.65 wt.% based on fresh feed. The catalyst has the ability to achieve 100% conversion of triglycerides at typical hydrotreating conditions with very little reduction in sulfur, nitrogen and aromatics content.