| 摘要 |
<p>A catalyst support has a mean pore diameter of 20-140 Angstrom and a total pore volume of 0.1-0.1ml/g measured by porosity to mercury. The ratio between the volume of pores with a diameter between Dmean-30 Angstrom and Dmean+30 Angstrom to the total pore volume is greater than 0.6; the volume in pores with a diameter greater than Dmean+30 Angstrom is less than 0.1ml/g. A catalyst contains at least one hydro-desulfurization element from group VIB and VIII of the periodic table; a non zeolitic support based on silica-alumina containing 10-80 wt.% silica (SiO2); a BET specific surface of 150-500 m2/g; a porous volume held in the pores with a diameter greater than 140 Angstrom, 160 Angstrom and 200 Angstrom of less than 0.1ml/g measured by porosity to mercury and with less than 0.01 ml/g held in the pores with a diameter greater than 500 Angstrom. The pore distribution is such that the ratio between the volume V2 measured by porosity to mercury held in pores between Dmean - 30 Angstrom and Dmean + 30 Angstrom over the total mercury volume is greater than 0.6; the volume V3 held in pores with a diameter greater than Dmean + 30 Angstrom is less than 0.1 ml/g and the volume V6 held in pores with diameter greater than Dmean + 15 Angstrom is less than 0.2 ml/g. The catalyst's diffraction diagram X contains at least the principal characteristic rays of at least one of the transition aluminas from the group including the alpha, rho, chi, eta, gamma, kappa, theta and delta aluminas. The proportion of octanhedric ALVI determined by the NMR MAS analysis of the solid of 27Al is greater than 50%. The base of the catalyst is nickel and tungsten or platinum and palladium. The catalyst has at least one doping element which is phosphorus, boron or silicon, deposited on the catalyst. The catalyst includes at least one element from group VIIB and/or VB and the filled compressed density is greater than 0.84 g/cm3. An Independent claim is included for a catalyst support as described above, with less than 0.1 wt.% cationic impurities and less than 0.5% by weight anionic impurities. An Independent claim is included for a hydrocracking process using such a catalyst, in one or two stages with a first hydrorefining zone in which the charge is placed in contact with a hydrorefining catalyst with a methylcyclohexane conversion rate of less than 10% and a second hydrocracking zone in which at least part of the effluent from the first zone is placed in contact with a non zeolitic hydrocracking catalyst with a methylcyclohexane conversion rate above 10%. The catalytic volume of the hydrorefining catalyst is 20 to 45% of the total catalytic volume.</p> |
