TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Components: The catalyst used in the second oligomerization step (e) comprises at least one zeolite comprising ZSM-5 zeolite, NU-10 and/or ZBM-30.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: The entire part of the effluent obtained from the first oligomerization step (d) is sent into the second step (e) of oligomerization. At least one separation step is implemented between the first oligomerization step (d) and the second step of oligomerization (e). The olefin effluent obtained from the first step of oligomerization (d) is separated into at least one olefin hydrocarbon effluent having greater than or equal to 4C and at least one 2-4C light olefin effluent. The entire 2-4C light olefin effluent is recycled in the first oligomerization step (d). In the process, entire olefin effluent having more than 4C resulting from the separation step, comprising 4-8C olefin compounds and olefin compound having more than 9C is fed into the second step of oligomerization (e). The olefin effluent having more than 4C obtained from the separation step is separated by at least a part of the olefin compound having more than 9C in a second separation step and at least a part of the olefin effluent having more than 9C is directly sent in step (f) of fractionating. The step (e) operates at a temperature of 50-400 degrees C, at a pressure of 2-15 MPa, and at weight hourly rate of 0.1-10 h-1. In the process, at least a part of the light effluent comprising 2-4C compounds derived from the fractionating step (f) is recycled in the first step of oligomerization; at least a part of the gasoline cut obtained from fractionating step (f) is recycled in the second step (e) of oligomerization; and at least a part of the middle distillate base obtained from the fractionating step (f) undergoes a hydrogenation step of produced olefin, in the presence of a catalyst comprising at least one Group VIII metal comprising palladium and/or nickel, and a support from alumina, silica or silica-alumina. The step of separating after hydrogenation step is carried out to allow fractionating into a kerosene cut, diesel oil and/or a cut having a boiling point of greater than 360 degrees C. EXAMPLE - Bioethanol charge composition comprising ethanol (99 wt.%), methanol (less than 0.05 wt.%), butanol (less than 0.1 wt.%), other alcohols (less than 0.05 wt.%), total content of alcohol other than ethanol (less than 0.2 wt.%), oxygenated compounds other than alcohols (less than 0.1 wt.%), water (less than 1 wt.%), total cationic impurities (less than 0.005 wt.%), and total anionic impurities (less than 0.005 wt.%) was purified. The purified charge was dehydrated into ethylene and water in the presence of a zeolite catalyst (ZSM-5) at a temperature of 400 degrees C, at a pressure of 0.1 MPa and a weight hourly rate of 5 h-1 to obtain a dehydration product predominantly ethylene hydrocarbon effluent comprising water. The effluent mainly ethylene was then subjected to a series of separation and purification by passage through a column of water washing, then by passage through a column of washing with sodium hydroxide in dryers to separate a portion of the water formed the ethylene effluent. The separated effluent was sent in first oligomerization step, in the presence of amorphous catalyst (silica-alumina support) and at a temperature of 240 degrees C and at a pressure of 4 MPa. The second oligomerization step was performed in the presence of the catalyst (powder of aluminum hydroxide mixed with a silica sol) and at a temperature of 150 degrees C, at an absolute pressure of 6 MPa and at a speed of 0.7 weight hourly rate of h-1. The effluent from the second oligomerization was subjected to fractionation to separate it into a light effluent comprising the 2-4C compounds, a gasoline cut and cut middle distillates (diesel and kerosene).