TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Components: The hydrocracking catalyst in step (C) comprises a zeolite.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: The liquefaction step (A) in the presence of hydrogen is carried out in the presence of an ebullating-bed supported catalyst, in the presence of a catalyst dispersed in an entrained bed or without catalyst added. The liquefaction step (A) is carried out in at least two reactors arranged in series each containing an ebullating-bed supported catalyst. The liquefaction step (A) operates at 300-440 degrees C for the first reactor and at 350-470 degrees C for the second reactor, then at a pressure of 15-25 MPa, at a liquid hourly space velocity ((ton of feed/hour)/ton of catalyst) 0.1-5 hour-1 and at a hydrogen/feed ratio of 0.1-5 Nm3/kg in each reactor. The hydrocracking step (C) operates at 250-480 degrees C, at a pressure of 2-25 MPa, at a space velocity 0.1-20 hour-1 and the amount of hydrogen introduced is such that the volume ratio of hydrogen to hydrocarbons is 80-5000 Nm3/m3. The catalytic reforming step operates at a pressure of 0.1-4 MPa, at 400-700 degrees C, at a space velocity of 0.1-10 hour-1 and with a recycled hydrogen/hydrocarbons ratio (mol.) of 0.1-10. The hydrogen produced in the catalytic reforming step (E) is recycled to the liquefaction step (A) and/or to the hydrocracking step (C). The separation step (B) makes it possible to obtain a gas phase, at least one atmospheric distillate fraction containing naphtha, kerosene and/or diesel, a vacuum distillate fraction and a vacuum residue fraction. At least a proportion (preferably all of the atmospheric distillate fraction), optionally supplemented with at least a proportion of the vacuum distillate fraction and/or of other co-feeds, is sent to the hydrocracking step (C) and at least a proportion (preferably all of the vacuum distillate fraction) is recycled as solvent to the liquefaction step (A). The fraction containing naphtha from step (D) is separated into a light naphtha fraction and a heavy naphtha fraction, the light naphtha fraction is submitted at least partly to an isomerization process, and the heavy naphtha fraction is submitted at least partly to the catalytic reforming step (E). The heavier fraction that is heavier than the naphtha fraction obtained in step (D) is at least partly recycled to the hydrocracking step (C). The heavier fraction that is heavier than the naphtha fraction obtained in step (D) is at least partly sent to a steam cracker in order to obtain light olefins. The step of separating the aromatic compounds from the reformate, is carried out by liquid-liquid extraction, extractive distillation, adsorption and/or crystallization. The coal is co-processed with a feedstock selected from petroleum residues, vacuum distillates of petroleum origin, crude oils, synthetic crudes, topped crudes, deasphalted oils, resins from deasphalting, asphalts or tars from deasphalting, derivatives from petroleum conversion processes, aromatic extracts obtained from the production chains of bases for lubricants, bituminous sands or their derivatives, oil shales or their derivatives, waste hydrocarbon and/or industrial polymers, organic wastes or household plastics, vegetable or animal oils and fats, and tars and residues that cannot be upgraded or are difficult to upgrade obtained from gasification and/or Fischer-Tropsch synthesis of biomass. The coal or petroleum residues, lignocellulosic biomass or greater than or equal to 1 constituent of cellulosic biomass is selected from cellulose, hemicellulose and/or lignin, algae, charcoal, oil from pyrolysis of lignocellulosic biomass or of algae, pyrolytic lignin, products from hydrothermal conversion of lignocellulosic biomass or of algae, and/or activated sludge from water treatment works. EXAMPLE - No suitable example given.