NOVELTY - Continuous (P1) hydrogenation of triglyceride containing raw materials of vegetable oils in fixed bed reactor system having several catalyst beds (3,4) comprising hydrogenation catalyst, involves a) dividing the raw material feed stream into a number of different partial streams F1 to Fn identical to the number of catalyst beds n in the reactor system at less than 80 degrees C; b) the temperature at the reactor inlet at the first catalyst bed (after a start-up phase) is adjusted with added diluting agent; and c) diluting agent is added to the streams of raw material feed F1 and hydrogen.    USE - For continuous hydrogenation of triglyceride containing raw materials like vegetable oils in a fixed bed reactor system having several catalyst beds (claimed).    ADVANTAGE - The process is improved process conducted at low temperatures and allows the utilization of existing units due to the low recycle ratio; provide a process using less recycle, requiring less revamp of existing units, minimizing corrosion caused by free fatty acids and/or avoiding losses of valuable paraffinic product and the other above-mentioned disadvantages due to deoxygenation of triglycerides through decarb-reactions; allows the use of existing units without considerable revamp; provides an extremely mild conversion of the triglyceride containing raw material without side reactions impairing the quality of the liquid product and without catalyst damage.    DETAILED DESCRIPTION - Continuous (P1) hydrogenation of triglyceride containing raw materials like vegetable oils in a fixed bed reactor system having several catalyst beds comprising hydrogenation catalyst, which beds are arranged in series, where the raw material feed, hydrogen containing gas and diluting agent are passed together through the catalyst beds of the reactor system at hydrogenation conditions, involves a) dividing the raw material feed stream into a number of different partial streams F1 to Fn identical to the number of catalyst beds n in the reactor system at less than 80 degrees C, the stream of hydrogen containing gas is also divided into the same number of different partial streams H1 to Hn at less than 110 degrees C, then partial raw material feed stream F1 and partial stream of hydrogen containing gas H1 are passed to the first catalyst bed, partial raw material feed stream F2 and partial stream of hydrogen containing gas H2 are passed to the second catalyst bed and so on, if n is greater than 2, each partial stream of raw material feed following in downstream direction being that much larger than the preceding one that the weight ratio of diluting agent to raw material feed is the same at the entrance of all catalyst beds and does not exceed 4:1, the term diluting agent comprising hydrogenation product formed in every catalyst bed and added diluting agent as defined below in b), b) the temperature at the reactor inlet at the first catalyst bed (after a start-up phase) is adjusted with added diluting agent, which is a specific fraction of the hydrogenation product obtained by the present process, which is recovered from the reactor exit product mixture by separation in two steps without controlled pressure reduction at 145-280 degrees C and 15-60 degrees C, c) diluting agent is only added to the streams of raw material feed F1 and hydrogen containing gas H1 entering at the reactor inlet and passing through the first catalyst bed, and d) hydrogen is used in excess of the theoretical hydrogen consumption.    DESCRIPTION OF DRAWING(S) - The figure shows the process for the continuous hydrogenation of triglyceride containing raw materials like vegetable oils.    First catalyst bed (3)    Second catalyst bed (4)    High temperature separator (8)    Low temperature separator (9)    Degassing vessel (12)