NOVELTY - Production of hydrocarbon based middle distillates from a feed comprising butanol and pentanol, comprises dehydration isomerization of the feed to produce an olefinic effluent, separation of water from the effluent, purification of the organic liquid effluent, first and second oligomerization of the effluent, fractionation of the effluent into a light product including 2-5C compounds, an intermediate product including 6-9C compounds and a middle distillate product including 10C+ compounds, third oligomerization of the intermediate product and hydrogenation of the middle distillate product.    USE - The process is useful for the production of hydrocarbon based middle distillates from a feed comprising butanol and pentanol (claimed). The process is useful for the conversion of 4-5C bio-alcohols in fuel base such as kerosene.    ADVANTAGE - The process ensures better control of the products obtained by separation of the two steps of oligomerization, thus controls the temperature increase in the reactor due to the exothermic reactions in each steps. The process allows adding aromatics to the fuel base obtained according to the limits prescribed by ASTM D7566-11a while respecting the density specification of the standard.    DETAILED DESCRIPTION - Production of hydrocarbon based middle distillates from a feed comprising butanol and pentanol, comprises: (a) dehydration isomerization of the feed in the presence of an amorphous acid or zeolite catalyst in a reactor at an absolute pressure of 0.5-2 MPa and at an inlet temperature of 350-450 degrees C to produce a predominantly olefinic effluent; (b) separation of water present in the olefinic effluent at a pressure of 0.5-1.2 MPa and a temperature of 35-60 degrees C to produce an organic liquid effluent; (c) purification of the organic liquid effluent to produce a purified organic effluent; (d) first selective oligomerization of isobutylenes and isopentenes of the feed including at least part of the purified organic effluent output from the step (c) in the presence of an amorphous catalyst in a reactor at an absolute pressure of 0.5-10 MPa, an inlet temperature 40-95 degrees C and at a feed rate of 0.1-10 per hour to produce a first oligomerization effluent including at least 20 wt.% of olefin having a number of carbon atoms equal to or higher than 6, based on the total mass of olefins contained in the effluent; (e) second oligomerization of the effluent of first oligomerization, and the total effluent obtained from step (g) and at least part of the light product obtained from step (f), in the presence of an amorphous catalyst in a reactor at an absolute pressure of 2-15 MPa, an inlet temperature of 100-200 degrees C and at a feed rate of 0.1-10 per hour to produce an effluent of second oligomerization; (f) fractionation of the effluent of second oligomerization into at least 3 products comprising a light product mainly including 2-5C compounds, an intermediate product mainly including 6-9C compounds, and a middle distillate product mainly including 10C+ compounds; (g) third oligomerization of at least the intermediate product in the presence of an amorphous catalyst in a reactor at an absolute pressure of 2-15 MPa, a temperature of 100-200 degrees C and at a feed rate of 0.1-5 per hour; (h) hydrogenation of at least a part of the middle distillate product in the presence of a catalyst including at least a group VIII metal in a reactor operating at an absolute pressure of 2-4 MPa, a temperature of 100-350 degrees C and a feed rate of 1-5 per hour with a hydrogen-hydrocarbons molar ratio of 10-450.