Abstract: A process for denitrogenation of high nitrogen content hydrocarbon feeds comprising contacting the feed with hydrogen under denitrogenation conditions in the presence of a catalyst comprising an active metallic component comprising at least one metal having hydrogenation activity and at least one oxygenated phosphorus component and a support component comprising at least one non-zeolitic, porous refractory inorganic oxide matrix component and at least one crystalline molecular sieve zeolite component.

Abstract: A process is provided to dedust oil derived from solid hydrocarbon-containing material, such as oil shale, coal or tar sand in multi-stage desalters. In the process, water is dispersed into the oil before entering each desalter to form an emulsion. The desalter separates the emulsion into a stream of oil having a substantially lower concentration of dust and a dusty stream of water containing most of the dust. In one embodiment, the sludge-like dusty stream from the first desalter is combusted in a lift pipe and used as heat carrier material in the retort. In other embodiments, the dusty stream from the first desalter is centrifuged or filtered and thereafter heated in a dryer to remove residual oil and water from the stream before the stream is combusted in the lift pipe and used as heat carrier material in the retort and dryer. Effluent water from the second and third desalters as well as from the centrifuge or filter are recycled upstream and dispersed in the oil.

Abstract: Hydrodenitrogenation of high nitrogen content hydrocarbon feeds comprises contacting the feed with hydrogen under hydrodenitrogenation conditions in the presence of a multiple catalyst system comprising an initial catalyst of apparent higher order reaction kinetics and lower rate constant for hydrodenitrogenation followed by at least one subsequent catalyst of apparent lower order reaction kinetics and higher rate constant for hydrodenitrogenation.

Abstract: Shaped catalyst which can be prepared by use of steam.

Abstract: A catalyst support is prepared from a composite comprising alumina and one or more oxides of phosphorous by forming the composite into a shaped support material having at least 0.8 cc/gm of its pore volume in pores having diameters of 0 nm (0 A) to 120 nm (1,200 A) and at least 0.1 cc/gm of its pore volume in pores having diameters of 120 nm (1,200 A) to 5,000 nm (50,000 A) and heating said shaped support material in the presence of steam at sufficient elevated temperature, steam pressure, and time period to increase the average pore diameter of said shaped support in the absence of any appreciable reduction in pore volume.A catalyst is prepared by impregnating the steam-treated support with at least one hydrogenating metal.The catalyst can be used suitably in hydrocarbon conversion processes, such as a process for the hydrodemetallization of a hydrocarbon stream containing asphaltenes and a substantial amount of metals.

Abstract: A process for hydrotreating a hydrocarbon stream such as petroleum distillate and similar hydrocarbon materials by contacting said stream with hydrogen and a catalyst comprising a porous refractory inorganic oxide support and deposited thereon hydrogenation components comprising chromium, molybdenum and at least one Group VIII metal. This process enables improved removal of nitrogen and sulfur, particularly from gas oils.

Abstract: Disclosed is a two-stage catalytic process for hydrodemetallation and hydrodesulfurization of heavy hydrocarbon streams containing asphaltenes and a substantial amount of metals. The first stage of this process comprises contacting the feedstock in a first reaction zone with hydrogen and a demetallation catalyst comprising hydrogenation metal selected from Group VIB and/or Group VIII deposed on a large-pore, high surface area inorganic oxide support; the second stage of the process comprises contacting the effluent from the first reaction zone with a catalyst consisting essentially of hydrogenation metal selected from Group VIB deposed on a smaller-pore, catalytically active support comprising alumina, said second-stage catalyst having a surface area within the range of about 150 m.sup.2 /gm to about 300 m.sup.2 /gm, having a majority of its pore volume in pore diameters within the range of about 80 A to about 130 A, and the catalyst has a pore volume within the range of about 0.4 cc/gm to about 0.9 cc/gm.

Abstract: A process for hydrotreating a hydrocarbon stream to remove nitrogen and sulfur which process comprises contacting a hydrocarbon stream comprising a stream selected from petroleum distillate, tar sands distillate, and shale oil, with hydrogen and a catalyst comprising a porous refractory inorganic oxide and deposited thereon hydrogenation components comprising chromium, molybdenum and at least one Group VIII metal, said catalyst having a pore volume distribution comprising 20-50% of pore volume in pores with diameters of 0-50 Angstrom units, 30-70% of pore volume in pores with diameters of 50-100 Angstrom units, 0-20% of pore volume in pores with diameters of 100-150 Angstrom units, and 0-10% of pore volume in pores with diameters greater than 150 Angstrom units.

Abstract: A process for hydrodemetallation and hydrodesulfurization of hydrocarbon feedstock containing asphaltenes and metals by contacting said feedstock with hydrogen and a bimodal catalyst consisting essentially of at least one active original hydrogenation metal selected from Group VIB deposited on a support comprising alumina wherein said catalyst has a surface area within the range of about 140 to about 300 m.sup.2 /gm, a total pore volume based upon measurement by mercury penetration within the range of about 0.4 cc/gm to about 1.0 cc/gm, and comprising about 60% to about 95% of its micropore volume in micropores having diameters within the range of about 50 A to about 200 A, 0% to about 15% of its micropore volume in pores having diameters within the range of about 200 A to about 600 A and about 3% to about 30% of said total pore volume based upon measurements by mercury penetration in macropores having diameters of 600 A or greater.

Abstract: A process for hydrotreating a hydrocarbon stream such as petroleum distillate and similar hydrocarbon materials by contacting said stream with hydrogen and a catalyst comprising a porous refractory inorganic oxide support and deposited thereon hydrogenation components comprising chromium, molybdenum and at least one Group VIII metal. This process enables improved removal of nitrogen and sulfur, particularly from gas oils.

Abstract: Disclosed is a two-stage catalytic process for hydrodemetallation and hydrodesulfurization of heavy hydrocarbon streams containing asphaltenes and a substantial amount of metals. The first stage of this process comprises contacting the feedstock in a first reaction zone with hydrogen and a demetallation catalyst comprising hydrogenation metal selected from Group VIB and/or Group VIII deposed on a large-pore, high surface area inorganic oxide support; the second stage of the process comprises contacting the effluent from the first reaction zone with a catalyst consisting essentially of hydrogenation metal selected from Group VIB deposed on a smaller pore, catalytically active support comprising alumina, said second stage catalyst having a surface area within the range of about 150 m.sup.2 /gm to about 300 m.sup.2 /gm, having a majority of its pore volume in pore diameters within the range of about 80 A to about 130 A, and the catalyst has a pore volume within the range of about 0.4 cc/gm to about 0.9 cc/gm.

Abstract: A heavy hydrocarbon stream containing metals, asphaltenes, nitrogen compounds, and sulfur compounds is (a) contacted with hydrogen and a hydrotreating catalyst containing molybdenum and chromium, either as metals, as oxides, as sulfides, or mixtures thereof, deposed on a large-pore, catalytically active alumina to reduce the metals content in said stream, to convert the asphaltenes, nitrogen compounds, and sulphur compounds in said stream, the catalyst has a pore volume within the range of about 0.4 cc/gm to about 0.8 cc/gm, a surface area within the range of about 150 m.sup.2 /gm to about 300 m.sup.2 /gm, and an average pore diameter within the range of about 100 A (10 nm) to about 200 A (20 nm); and (b) at least a portion of the hydrotreated stream is cracked with a cracking catalyst to produce gasoline and distillates in improved yields. The catalyst in step (a) may also contain cobalt.

Abstract: The process comprises contacting a heavy hydrocarbon stream containing metals and asphaltenes to reduce the contents of nitrogen compounds, sulfur compounds, metals and asphaltenes in the hydrocarbon stream under suitable conditions and in the presence of hydrogen with a catalyst comprising a hydrogenating component consisting essentially of molybdenum and chromium, their oxides, their sulfides, or mixtures thereof on a large-pore, catalytically active alumina. The catalyst has a pore volume within the range of about 0.4 cc/gm to about 0.8 cc/gm, a surface area within the range of about 150 m.sup.2 /gm to about 300 m.sup.2 /gm, and an average pore diameter within the range of about 100 A to about 200 A.

Abstract: The process comprises contacting a heavy hydrocarbon stream under suitable conditions and in the presence of hydrogen with a catalyst comprising a hydrogenating component selected from the group consisting of (1) molybdenum, chromium, and a small amount of cobalt, (2) their oxides, (3) their sulfides, and (4) mixtures thereof deposed on a large-pore, catalytically active alumina. The molybdenum is present in an amount within the range of about 5 wt.% to about 15 wt.%, calculated as MoO.sub.3 and based upon total catalyst weight, the chromium is present in an amount within the range of about 5 wt.% to about 20 wt.%, calculated as Cr.sub.2 O.sub.3 and based upon the total catalyst weight, and the cobalt is present in an amount within the range of about 0.1 wt.% to about 5 wt.%, calculated as CoO and based upon the total catalyst weight. The catalyst possesses a pore volume within the range of about 0.4 cc/gm to about 0.8 cc/gm, a surface area within the range of about 150 m.sup.2 /gm to about 300 m.sup.

Abstract: There is disclosed a catalyst for the hydrodemetallization of petroleum hydrocarbon streams containing asphaltenes and large quantities of metals. This catalyst consists essentially of a small amount of a single hydrogenation metal selected from the group consisting of metals from Group VIB of the Periodic Table of Elements and metals from Group VIII of the Periodic Table deposed on a large-pore alumina. The hydrogenation metal may be present in the elemental form, as an oxide, as a sulfide, or mixtures thereof. The catalyst is characterized by a surface area of at least 120 square meters per gram, a pore volume of at least 0.7 cc per gram, and an average pore diameter of at least 125 Angstrom units. Suitable examples of a hydrogenation metal are nickel and molybdenum.

Abstract: There is disclosed a process for the demetalation of a heavy petroleum hydrocarbon stream containing metals and asphaltenes. This process comprises contacting in a reaction zone the heavy petroleum hydrocarbon stream under suitable operating conditions and in the presence of hydrogen with a catalyst comprising a hydrogenation component deposed on a large-pore, high-surface area silica gel to produce an effluent that contains less metals and less asphaltenes than the hydrocarbon stream charged to the reaction zone.

Abstract: The catalyst comprises the oxides of cobalt and molybdenum deposited on a co-catalytic acidic cracking support comprising ultrastable, large-pore crystalline aluminosilicate material and a silica-alumina cracking catalyst. This catalyst may be used in a hydrocracking process or a combination process for converting petroleum hydrocarbons to gasoline blending stock having an unleaded research octane number greater than about 105. The hydrocracking process comprises contacting the catalyst in a hydrocracking reaction zone under hydrocracking conditions with a feedstock having an initial boiling point of at least 350.degree. F. The combination process comprises treating the hydrocarbons in the hydrocracking process, selectively solvent-extracting the aromatics from the resultant hydrocracked product to obtain an aromatic extract and a non-aromatic raffinate, catalytically reforming the non-aromatic raffinate, and blending the resultant catalytic reformate with aromatic extract.