Installation for the hydrotreatment and hydroconversion of hydrocarbon-containing feedstocks, with a common fractionation section, for the production of at least one of the following products: naphtha (light and/or heavy), diesel, kerosene, distillate and residue, comprising at least:
- a reaction section R-1 comprising at least one hydroconversion reactor,
• a hot high-pressure separator drum B-1, supplied with the effluent originating from the reaction section R-1, and the liquid effluent of which is a heavy fraction of the effluent from the reaction section R-1.
• a cold high-pressure separator drum B-2, supplied with the gaseous flow originating from the hot high-pressure separator drum B-1, and the liquid effluent of which is a light fraction of the effluent from the reactor R-1.
• optionally a hot medium-pressure separator drum B-3, supplied with the liquid effluent originating from the hot high-pressure separator drum B-1, and the liquid effluent of which supplies the drum B-5;
• optionally a cold medium-pressure separator drum B-4, supplied with the liquid effluent originating from the cold high-pressure separator drum B-2, and the gaseous fraction originating from the hot medium-pressure separator drum B-3 and the liquid effluent of which constitutes a feedstock of the common fractionation section;
• optionally a hot low-pressure separator drum B-5, supplied with the liquid flow originating from the hot medium-pressure separator drum B-3, and the liquid effluent of which constitutes a feedstock of the common fractionation section.
- a reaction section R10 comprising at least one hydrotreatment reactor
• optionally, a hot high-pressure separator drum B-10, supplied with the effluent originating from the reaction section R-10, and the liquid effluent of which is a heavy fraction of the effluent from the reaction section R-10;
• a cold high-pressure separator drum B-20, supplied with any gaseous flow originating from the hot high-pressure separator drum B-10, or directly with the effluent originating from the reaction section R-10, and the liquid effluent of which constitutes the light fraction or a mixture of the light fraction and the heavy fraction of the effluent from the reaction section R-10 which supplies either a cold medium- or low-pressure separator drum or, directly, the common fractionation section.
• optionally a hot medium-pressure separator drum B-30, the feedstock of which is the liquid flow originating from the hot high-pressure separator drum B-10, if it exists,
• optionally a cold medium-pressure separator drum B-40, supplied with the liquid flow originating from the cold high-pressure separator drum B-20, and the gaseous flow

originating from the hot medium-pressure separator drum B-30, if it exists, and the liquid effluent of which constitutes a feedstock of the common fractionation section • optionally a hot low-pressure separator drum B-50, supplied with the liquid flow originating from the hot medium-pressure separator drum B-30, and the liquid effluent and the vapour effluent of which constitute one or more feedstocks of the common fractionation section
a common fractionation section comprising at least one main fractionation column C-2, making it possible to separate a top fraction, an intermediate fraction and a heavy fraction, said fractions comprising the different products of the units,
the supply of the flow or flows originating from the first unit and the supply of the flow or flows originating from the second unit to said common fractionation unit being separate.
Installation according to claim 1, in which the common fractionation section comprises a separation column C-1, said separation column C-1 being separately supplied with:
- on the one hand, the liquid flow originating from the cold high-pressure separator drum B-2, and optionally the gaseous flow originating from the hot low-pressure separator drum B-5 of the first unit;
- on the other hand the liquid flow from the cold high-pressure separator drum B-20, and/or the liquid flow from the cold medium-pressure separator drum B-40, and/or the gaseous flow originating from the cold low-pressure separator drum B-50, of the second unit;
the main fractionation column C-2 being supplied with the liquid effluent from said separation column C-1, separately with the liquid flow originating from the hot low-pressure separator drum B-5 of the first unit, and with the liquid flow originating from the hot medium-pressure separator drum B-30 of the second unit.
Installation according to one of claims 1 or 2 in which the common fractionation section also comprises:
- at least one side-stripping column C-4, C-5 or C-6, supplied with one of the products of the intermediate fraction originating from the main fractionation column C-2: kerosene, diesel or residue, making it possible to separate a top gaseous fraction and a bottom liquid fraction,
- a pipe making it possible to send said top gaseous fraction to the main fractionation column C-2;
- an exchanger E4 for cooling said bottom liquid fraction of said side-stripping column;
- an outlet pipe for said cooled liquid fraction.
Installation according to one of claims 1 to 3, comprising a section for the treatment of acid gases C-7 comprising an amine absorber or a washing column operating at very low pressure, supplied

with at least a part of the top fraction originating from the main fractionation column C-2 containing the residual acid gases.
Installation according to claims 1 to 4 comprising a section for the recovery of liquefied petroleum gases comprising one or more fractionation columns, supplied with at least a part of the top fraction originating from the main fractionation column C-2 containing the residual acid gases, or with the flow originating from the section for the treatment of the acid gases C7.
Installation according to one of the preceding claims, in which one or other of the reaction sections comprises a hydroisomerization section including a catalytic dewaxing unit, comprising at least one catalytic bed of catalyst comprising a zeolite, a hydrogenating/dehydrogenating function, and an acid function.
Installation according to one of the preceding claims, in which the first unit is a hydrocracking unit and the second unit a diesel hydrodesulphurization unit.
Installation according to one of claims 1 to 6, in which the first unit is a unit for the hydroconversion of residue or distillate or deasphalted oil in an ebullating bed, and the second unit is a unit for the hydrodesulphurization of vacuum distillate, or diesel or kerosene.
Installation according to claim 8, in which the first unit is a unit for the hydroconversion of deasphalted oil in an ebullating bed, and the second unit is a unit for the hydrodesulphurization of vacuum distillate.
Integrated process for the hydrotreatment and hydroconversion of gasoils, vacuum distillates, atmospheric or vacuum residues, using the installation according to one of claims 1 to 9, in which the separation column C-1 operates under the following conditions: total pressure comprised between 0.4 MPa and 2.0 MPa, preferably between 0.6 and 2.0 MPa, very preferably between 0.7 and 1.8 MPa.
Integrated process for the hydrotreatment and hydroconversion of hydrocarbon-containing feedstocks according to claim 10, in which the fractionation column C-2 operates under the following pressure conditions: total pressure comprised between 0.1 MPa and 0.4 MPa, preferably comprised between 0.1 MPa and 0.3 MPa.
Integrated process for the hydrotreatment and hydroconversion of hydrocarbon-containing feedstocks according to claim 10 or 11, in which the side-stripping column(s) C-4, C-5 and C-6 operate under the following pressure conditions: total pressure comprised between 0.1 MPa and 0.4 MPa, preferably comprised between 0.1 MPa and 0.3 MPa.
Integrated process for the hydrotreatment and hydroconversion of hydrocarbon-containing feedstocks according to one of claims 10 to 12 in which the operating conditions of the catalytic

hydrotreatment, hydroconversion and hydoisomerization reactions are: a temperature of the fixed-bed reaction sections comprised between 200 and 460°C, an average temperature of the catalytic bed of the ebullating-bed reaction sections comprised between 300 and 600qC, preferably between 350°C and 510^, a total pressure comprised between 1.5 and 35 MPa, preferably between 2 and 25 MPa, an overall hourly space velocity of liquid feedstock for each catalytic step comprised between 0.1 and 20, preferably comprised between 0.15 and 15, a quantity of hydrogen relative to the liquid feedstock comprised between 50 and 2500 Nm3/m3.
14. Integrated process for the hydrotreatment and hydroconversion according to one of claims 10 to 13 in which the hydrocarbon-containing feedstock is selected from feedstocks of the atmospheric distillate type (naphtha, gasoline, kerosene and gasoils), vacuum distillate, for example gasoils, originating from the direct distillation of crude or conversion units such as FCC, coker or visbreaking, such as LCO (light cycle oil) light oil originating from a catalytic cracking unit, the feedstocks originating from aromatic extraction units, lubricating oil bases or bases originating from solvent dewaxing of lubricating oil bases, the distillates originating from fixed-bed or ebullating-bed desulphurization or hydroconversion processes of ATR (atmospheric residues) and/or of VR (vacuum residues) and/or deasphalted oils, the deasphalted oils, effluents from a Fischer-Tropsch unit, the vegetable oils, alone or in a mixture, or animal fats.
15. Integrated hydrotreatment and hydroconversion process according to claim 14 in which the hydrocarbon-containing feedstock is selected from the gasoils, the vacuum distillates, the atmospheric or vacuum residues or the effluents from a Fischer-Tropsch unit.