NOVELTY - Continuous hydrogenation of triglyceride containing raw materials like vegetable oils to produce diesel and/or kerosene fraction in a fixed bed reactor system having several catalyst beds comprising hydrogenation catalyst, which beds are arranged in series, comprises passing raw material feed, hydrogen containing gas and diluting agent together through the catalyst beds of the reactor system at hydrogenation conditions.    USE - The process is useful for continuous hydrogenation of triglyceride containing raw materials like vegetable oils to produce diesel and/or kerosene fraction in a fixed bed reactor system.    ADVANTAGE - The process requires less recycle and less revamp of existing units, and minimizes corrosion caused by free fatty acids and/or essentially avoiding losses of valuable paraffinic product. The process maximize the base gas oil and/or kerosene yield and to promote the hydrodeoxygenation mechanism.    DETAILED DESCRIPTION - Continuous hydrogenation of triglyceride containing raw materials like vegetable oils to produce diesel and/or kerosene fraction in a fixed bed reactor system having several catalyst beds comprising hydrogenation catalyst, which beds are arranged in series, comprises passing raw material feed, hydrogen containing gas and diluting agent together through the catalyst beds of the reactor system at hydrogenation conditions, where the raw material feed stream is divided into a number of different partial stream 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 (H) containing gas is also divided into the same number of different partial stream H1 to Hn at less than 110 degrees C, then partial raw material feed stream and partial stream of hydrogen containing gas H1 are passed to first catalyst bed (3), and before the first partial mixed stream (F1+H1) enters the first catalyst bed, it is mixed with added diluting agent which is a specific fraction of the hydrogenation product obtained by the present process, partial raw material feed stream F2 and partial stream of hydrogen containing gas H2 are passed to the second catalyst bed (4) 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 essentially the same at the entrance of all catalyst beds and does not exceed 4:1, the diluting agent comprises the hydrogenation product formed in every catalyst bed as well as the specific fraction recycled to the reactor inlet at the first catalyst bed and is referred to as added diluting agent, the temperature at the reactor inlet at the first catalyst bed (after start up phase) is adjusted by adding diluting agent called added diluting agent, which is recovered from the reactor exit product mixture by separation in one or two steps without controlled pressure reduction, added 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, hydrogen is used in excess of the theoretical hydrogen consumption, and a hydrogenation bulk or supported catalyst comprising an active phase constituted by at least one element from group VIB and at least one element from group VIII, the elements are in the sulfide form, and the atomic ratio of the metal (or metals) from group VIII to the metal (or metals) from group VIB being strictly more than 0 and less than 0.095, is used in at least the first catalyst bed of the fixed bed reactor system.    DESCRIPTION OF DRAWING(S) - The figure shows a schematic representation of a process.    First catalyst bed (3)    Second catalyst bed (4)    Third catalyst bed (5)    High temperature separator (8)    Low temperature separator. (9)