Abstract: Disclosed is a catalyst comprising a porous alumina support bearing 2.5-6 wt % of a non-cobalt Group VIII metal oxide, 14.5-25 wt % of a Group VI-B metal oxide, and 0-4 wt % of a phosphorus oxide, said catalyst having a Total Surface Area of 240-320 M.sup.2 /g, Pore Volume of 0.65-0.90 cc/g, and a Pore Diameter Distribution whereby 50-62.8% of the Total Pore Volume is present as micropores of diameter 55-115 .ANG., 27.5-37% of the Total Pore Volume is present in large pores of a diameter greater than 160 .ANG. and 20-30.5% of the Total Pore Volume is present as macropores of diameter greater than 250 .ANG..

Abstract: Heavy hydrocarbons are hydrotreated to increase content of components boiling below 1000.degree. F. by contact with Group VIII non-noble metal oxide and Group VI-B metal oxide on alumina having a Total Surface Area of 150-240 m.sup.2 /g, a Total Pore Volume, (TPV) of 0.7-0.98, and a Pore Diameter Distribution whereby .ltoreq.20% of the TPV is present as primary micropores of diameter .ltoreq.100 .ANG., at least about 34% of TPV is present as secondary micropores of diameter of about 100 .ANG.-200 .ANG., and about 26%-46% of the TPV is present as mesopores of diameter .gtoreq.200 .ANG..

Abstract: A novel zeolite characterized by a large number of secondary pores, a substantially decreased Lattice Constant of below about 24.19 .ANG., and a substantially decreased Acid Site Density is attained by hydrothermal and acid-treating of an ultrastable Y-zeolite.

Abstract: Heavy oils may be hydrotreated in the presence of a porous alumina support bearing metals of Group VIII, excluding cobalt, and VI-B and optionally phosphorus, the catalyst having a Total Surface Area of 240-320 m.sup.2 /g, a Total Pore Volume of 0.65-0.9 cc/g, and a Pore Diameter Distribution whereby 50-62.8% of the Total Pore Volume is present as micropores of diameter 55-115 .ANG. and 20-30.5% of the Total Pore Volume is present as macropores of diameter greater than 250 .ANG..The heavy oils and hydrogen are contacted with the catalyst such that the catalyst is maintained at isothermal conditions and is exposed to a uniform quality of feed. The process is particularly effective in achieving desired levels of hydroconversion of feedstock components having a boiling point greater than 1000.degree. F. to products having a boiling point less than 1000.degree. F.

Abstract: Disclosed is a hydrotreating catalyst which comprises a porous alumina support bearing metals of Group VIII and VI-B and optionally phosphorus, the catalyst having a Total Surface Area of 240-310 m.sup.2 /g, a Total Pore Volume of 0.5-0.75 cc/g, and a Pore Diameter Distribution whereby 63-78% of the Total Pore Volume is present as micropores of diameter 55-115 .ANG. and 11-18% of the Total Pore Volume is present as macropores of diameter greater than 250 .ANG., said catalyst being particularly effective in achieving desired levels of hydroconversion of feedstock components having a boiling point greater than 1000.degree. F. to products having a boiling point less than 1000.degree. F.

Abstract: Hydrodesulfurization of a cracked naphtha is effected in the presence of, as catalyst, an alkali metal, a metal of Group VIII, and a metal of Group VI-B on an alumina support containing a hydrotalcite-like composition.

Abstract: Spent or inactive alumina-supported catalysts removed from a catalytic hydrotreating process and having carbonaceous and metallic deposits thereon are reactivated. After a solvent wash to remove process oils, the spent catalyst is contacted with steam at a temperature of 1000.degree. to about 1250.degree. F. for a period of about 2 to about 5 hours to form a reactivated catalyst suitable for reuse in a catalytic hydrotreating process. Optionally, the steam-treated catalyst can be regenerated by contact with an oxygen-containing gas at a temperature of about 700.degree. to about 900.degree. F. to remove carbon deposits from the catalyst, or, alternatively, the steam-treated catalyst can be acid-leached to remove undesired metals and then contacted with an oxygen-containing gas at an elevated temperature to remove carbon deposits.

Abstract: Hydrodesulfurization of a cracked naphtha is effected in the presence of, as catalyst, a non-noble metal of Group VIII and a metal of Group VI-B on an alumina support containing a hydrotalcite-like composition. The process of the instant invention gives high levels of hydrodesulfurization compared to prior art magnesia-containing catalysts and lower levels of olefin saturation, and less octane reduction in the desulfurized gasoline.

Abstract: A mild hydrocracking process for the hydrodemetallation (HDM), hydrodesulfurization (HDS) and hydroconversion (HC) of hydrocarbon feedstocks such as residuum feedstocks which provides increased conversion and increased yields of middle distillates is disclosed. The process utilizes a catalyst comprising about 1.0 to about 6.0 wt. % of an oxide of a Group VIII metal, about 12.0 to about 25.0 wt. % of an oxide of molybdenum and 0 to about 5.0 wt. % of an oxide of phosphorus supported on a porous alumina support containing about 0.1 to about 10.0 wt. % of lithium oxide.

Abstract: Heavy hydrocarbons are hydrotreated to increase content of components boiling below 1000.degree. F. by contact with Group VIII non-noble metal oxide and Group VI-B metal oxide on alumina having a Total Surface Area of 150-240 m.sup.2 /g, a Total Pore Volume, (TPV) of 0.7-0.98, and a Pore Diameter Distribution whereby .ltoreq.20% of the TPV is present as primary micropores of diameter .ltoreq.100 .ANG., at least about 34% of TPV is present as secondary micropores of diameter of about 100 .ANG.-200 .ANG., and about 26%-46% of the TPV is present as mesopores of diameter >200 .ANG..

Abstract: Heavy oils may be hydrotreated in the presence of a porous alumina support bearing metals of Group VIII and VI-B and optionally phosphorus, the catalyst having a Total Surface Area of 165-230 m.sup.2 /g, a Total Pore Volume of 0.5-0.8 cc.g, and a Pore Diameter Distribution whereby less than about 5% the Total Pore Volume is present as primary micropores of diameter less than 80 .ANG., and secondary micropores of diameter of +20 .ANG. of a Pore Mode of 100-135 .ANG. are present in amount of at least about 65% of the micropore volume having pores with diameter less than 250 .ANG., and 22-29% of the Total Pore Volume is present as macropores of diameter >250 .ANG..The process of the instant invention is particularly effective in achieving desired levels of hydrodemetallation, hydrodesulfurization, and hydrocracking of asphaltenes in the fraction of hydrotreated/hydrocracked petroleum resid product having a boiling point greater than 1000.degree. F.

Abstract: Heavy oils may be hydrotreated in the presence of a porous alumina support bearing metals of Group VIII and VI-B and optionally phosphorus, the catalyst having a Total Surface Area of 165-230 m.sup.2 /g, a Total Pore Volume of 0.5-0.8 cc.g, and a Pore Diameter Distribution whereby less than about 5% of the Total Pore Volume is present as primary micropores of diameter less than 80.ANG., and secondary micropores of diameter of .+-.20.ANG. of a Pore Mode of 100-135.ANG. are present in amount of at least about 65% of the micropore volume having pores with diameter less than 250.ANG., and 22-29% of the Total Pore Volume is present as macropores of diameter >250.ANG.. The process of the instant invention is particularly effective in achieving desired levels of hydrodemetallation, hydrodesulfurization, and hydrocracking of asphaltenes in the fraction of hydrotreated/hydrocracked petroleum resid product having a boiling point greater than 1000.degree. F.

Abstract: Heavy oils may be hydrotreated in the presence of a porous alumina support bearing metals of Group VIII and VI-B and optionally phosphorus, the catalyst having a Total Surface Area of 240-310 m.sup.2 /g, a Total Pore Volume of 0.5-0.75 cc/g, and a Pore Diameter Distribution whereby 63-78% of the Total Pore Volume is present as micropores of diameter 55-115A and 11-18% of the Total Pore Volume is present as macropores of diameter greater than 250A. The heavy oils and hydrogen are contacted with the catalyst such that the catalyst is maintained at isothermal conditions and is exposed to a uniform quality of feed. The process is particularly effective in achieving desired levels of hydroconversion of feedstock components having a boiling point greater than 1000.degree. F. to products having a boiling point less than 1000.degree. F.

Abstract: Hydrodesulfurization of a cracked naphtha is effected in the presence of a transition alumina support bearing a Group VIII non-noble metal oxide and a Group VI-B metal oxide, the atom ratio of Group VIII metal to Group VI-B metal being 1-8. The process of the instant invention gives high levels of hydrodesulfurization compared to prior art magnesia-containing catalysts and lower levels of olefin saturation, and less octane reduction in the desulfurized gasoline.

Abstract: A novel zeolite characterized by a large number of secondary pores, a substantially decreased lattice constant, and a substantially decreased acid site density is attained by hydrothermal and acid-treating of an ultrastable Y-zeolite or a superultrastable Y-zeolite.

Abstract: A mild hydrocracking process for the hydrodemetallation (HDM), hydrodesulfurization (HDS) and hydroconversion (HC) of hydrocarbon feedstocks such as residuum feedstocks which provides increased conversion of heavy hydrocarbons boiling above 1000.degree. F. into products boiling below 1000.degree. F. as well as increased yields of middle distillates is disclosed. The process utilizes a catalyst comprising about 1.0 to about 6.0 wt. % of an oxide of a Group VIII metal, about 12.0 to about 25.0 wt. % of an oxide of molybdenum and 0 to about 5.0 wt. % of an oxide of phosphorus supported on a porous support comprising precipitated alumina or silica-containing alumina and dealuminated Y-zeolite.

Abstract: Hydrodesulfurization of a cracked naphtha is effected in the presence of, as catalyst, an alkali metal, a metal of Group VIII, and a metal of Group VI-B on an alumina support containing a hydrotalcite-like composition.

Abstract: A mild hydrocracking process for the hydrodemetallation (HDM), hydrodesulfurization (HDS) and hydroconversion (HC) of hydrocarbon feedstocks such as residuum feedstocks which provides increased conversion and increased yields of middle distillates is disclosed. The process utilizes a catalyst comprising about 1.0 to about 6.0 wt. % of an oxide of a Group VIII metal, about 12.0 to about 25.0 wt. % of an oxide of molybdenum and about 0 to about 5.0 wt. % of an oxide of phosphorus supported on a porous alumina support containing about 0.1 to about 10.0 wt. % of lithium oxide.

Abstract: A mild hydrocracking process for the hydrodemetallation (HDM), hydrodesulfurization (HDS) and hydroconversion (HC) of hydrocarbon feedstocks such as residuum feedstocks which provides increased conversion of heavy hydrocarbons boiling above 1000.degree. F. into products boiling below 1000.degree. F. as well as increased yields of middle distillates is disclosed. The process utilizes a catalyst comprising about 1.0 to about 6.0 wt. % of an oxide of a Group VIII metal, about 12.0 to about 25.0 wt. % of an oxide of molybdenum and 0.1 to about 5.0 wt. % of an oxide of phosphorus supported on a porous support comprising precipitated alumina or silica-containing alumina and hydrogen form, acidified, dealuminated Y-zeolite.

Abstract: Spent or inactive alumina-supported catalysts removed from a catalytic hydrotreating process and having carbonaceous and metallic deposits thereon are reactivated. After a solvent wash to remove process oils, the spent catalyst is contacted with steam at a temperature of 1000.degree. to about 1250.degree. F. for a period of about 2 to about 5 hours to form a reactivated catalyst suitable for reuse in a catalytic hydrotreating process. Optionally, the steam-treated catalyst can be regenerated by contact with an oxygen-containing gas at a temperature of about 700.degree. to about 900.degree. F. to remove carbon deposits from the catalyst, or, alternatively, the steam-treated catalyst can be acid-leached to remove undesired metals and then contacted with an oxygen-containing gas at an elevated temperature to remove carbon deposits.