NOVELTY - Continuous hydrogenation of triglyceride containing raw materials like vegetable oils, comprises: (a) dividing raw material feed stream into a number of different partial stream F1 to Fn identical to the number of catalyst beds (n) in the reactor system; (b) adjusting the temperature at the reactor inlet at the first catalyst bed (after start up phase); (c) adding added diluting agent only to the streams of raw material feed F1 and hydrogen containing gas H1 entering at the reactor inlet; and (d) using hydrogen in excess of the theoretical hydrogen consumption.    USE - The process is useful for continuous hydrogenation of triglyceride containing raw materials like vegetable oils to produce diesel and/or kerosene fraction in fixed bed reactor system having several catalyst beds comprising hydrogenation catalyst (claimed).    ADVANTAGE - The invention provides improved process for continuous hydrogenation of triglyceride containing raw materials like vegetable oils in a fixed bed reactor system having several catalyst beds comprising specific hydrogenation catalysts. The process uses less recycle, requires less revamp of existing units, minimizes corrosion caused by free fatty acids and/or essentially avoids losses of valuable paraffinic product.    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, where 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, comprises: (a) dividing raw material feed stream into a number of different partial stream F1 to Fn identical to the number of catalyst beds (n) in the reactor system at a temperature of less than 80 degrees C, the stream of hydrogen containing gas is also divided into the same number of different partial stream H1 to Hn at a temperature of less than 110 degrees C, then partial raw material feed stream and partial stream of hydrogen containing gas H1 are passed to the first catalyst bed, 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 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 comprising 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; (b) adjusting the temperature at the reactor inlet at the first catalyst bed (after start up phase) 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; (c) adding added diluting agent only 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) using hydrogen in excess of the theoretical hydrogen consumption, where a hydrogenation supported or unsupported catalyst comprising an active phase constituted by a sulfur-containing group VIB element, the group VIB element being molybdenum, is used in at least the first catalyst bed of the fixed bed reactor system.