PROCESS FOR REINING CRUDE OIL

FIELD: oil, gas and coke-chemical industries.SUBSTANCE: invention relates to a process for refining crude oil which includes the use of a specific hydroconversion unit. In particular, the invention relates to a method that optimises the refinement of petroleum feedstock in an oil refinery equipped with a coking plant. Process for refining crude oil includes the following steps: feeding crude oil to one or more atmospheric distillation units to separate at least heavy residue(s); feeding the heavy residue(s) separated in the atmospheric distillation unit(s) to a sub-atmospheric distillation unit with the extraction of at least two liquid streams: vacuum residue and light separated fraction; feeding the vacuum residue separated in the sub-atmospheric distillation unit to a hydroprocessing unit comprising at least one hydroconversion reactor in a slurry phase into which is fed hydrogen or a mixture of hydrogen and HS in the presence of a suitable dispersed hydrogenation catalyst, the particle sizes of which range from 1 nm to 30 mcm, to produce a product in vapour phase and a by-product in slurry phase, where said product in vapour phase is treated and separated in a gas/liquid treatment and separation section, obtaining fractions both in the vapour phase and the liquid phase, and also; feeding a light separated fraction obtained in the sub-atmospheric distillation unit to hydrodesulphuration unit of light gasoils (HDS1); feeding the liquid fraction separated in the hydroconversion unit and having a boiling point above 350°C, to hydrodesulphuration and/or hydrocracking unit of heavy gasoils (HDS/HDC); feeding the liquid fraction separated in the hydroconversion unit and having a boiling point of 170 to 350°C, to hydrodesulphuration unit of medium gasoils (HDS2); feeding the liquid fraction separated in the hydroconversion unit and having a boiling point ranging from the boiling point of C5 products to 170°C, to desulphuration unit of naphtha (HDS3); feeding the liquid stream separated in the distillation unit at atmospheric pressure and having a boiling point ranging from the boiling point of C5 products to 170°C, to said desulphuration unit of naphtha (HDS3), wherein the hydroconversion unit, in addition to one or more slurry phase hydroconversion reactors, includes a first separator into which the residue is fed in slurry phase, followed by a second separator, a stripping unit at atmospheric pressure and a separation unit, and in addition to treatment in th