Abstract: There is disclosed a method for preparing a metal-cation-deficient crystalline borosilicate, which method comprises: (1) preparing a mixture containing an oxide of silicon that is substantially free of metal cations, an oxide of boron, ammonium hydroxide, alkylammonium cation or a precursor of an alkylammonium cation, and water; and (2) maintaining the mixture at suitable reaction conditions to effect formation of the borosilicate.There are also disclosed the crystalline borosilicate that results from the above-described method of preparation and uses of that borosilicate.

Abstract: A new crystalline borosilicate comprises a molecular sieve material having the following composition in terms of mole ratios of oxides:0.9.+-.0.2M.sub.2/n O:B.sub.2 O.sub.3 :YSiO.sub.2 :ZH.sub.2 Owherein M is at least one cation, n is the valence of the cation, Y is a value within the range of 4 to about 600, and Z is a value within the range of 0 to about 160, and providing a specific X-ray diffraction pattern. The borosilicate is used to catalyze various processes, such as isomerization, disproportionation, and transalkylation.

Abstract: A new catalytic composition and its method of preparation are presented. The catalytic composition comprises a crystalline borosilicate and a porous refractory inorganic oxide, said borosilicate and said inorganic oxide having been intimately admixed with one another, said borosilicate comprising a molecular sieve material having the following composition in terms of mole ratios of oxides:0.9.+-.0.2 M.sub.2/n O:B.sub.2 O.sub.3 :YSiO.sub.2 :ZH.sub.2 O,wherein M is at least one cation having a valence of n, Y is between 4 and about 600, and Z is between 0 and about 160.The catalytic composition can be used for the conversion of hydrocarbon streams, e.g., the isomerization of xylene feedstocks.

Abstract: An improved process for the reforming of a hydrocarbon stream, which process comprises contacting said hydrocarbon stream under reforming conditions and in the presence of hydrogen with a catalyst which comprises platinum, rhenium, a small amount of palladium, and combined halogen on a refractory inorganic oxide, such as an alumina, and which has not been presulfided. The improvement comprises a rhenium-containing catalyst which has not been presulfided and which contains a small amount of palladium, i.e., about 0.05 wt. % to about 1 wt. % palladium. The feedstock being reformed can contain up to about 50 ppm sulfur.

Abstract: There is disclosed a catalyst for the reforming of hydrocarbon streams. This catalyst comprises iridium as a hydrogenation component on a support of zirconia and alumina. The support comprises zirconia in an amount of about 3 wt. % to about 15 wt. % zirconia or at least 60 wt. % zirconia. The iridium is present in an amount of about 0.05 wt. % to about 1.5 wt. %, calculated as the metal and based upon the total weight of the catalyst.Also disclosed is a reforming process, which process comprises contacting a hydrocarbon stream in a reaction zone under reforming conditions and in the presence of hydrogen with the above-described catalyst.

Abstract: The process comprises contacting a hydrocarbon feedstock containing a substantial amount of organic nitrogen-containing compounds in a first reaction zone under hydrocracking conditions and in the presence of hydrogen with a first catalyst comprising nickel and molybdenum or nickel and tungsten, their oxides, and/or their sulfides on a co-catalytic acidic cracking support comprising ultrastable, large-pore crystalline alumino-silicate material and a silica-alumina matrix to produce a first hydrocracked effluent and contacting said first hydrocracked effluent in a second reaction zone under hydrocracking conditions and in the presence of hydrogen with a second catalyst comprising cobalt and molybdenum, their oxides, and/or their sulfides on a co-catalytic acidic cracking support comprising ultrastable, large-pore crystalline aluminosilicate material and a silica-alumina matrix to produce a second hydrocracked effluent.

Abstract: The process comprises passing a hydrocarbon stream under reforming conditions through each of the reactors of the unit; when the catalyst in all of the reactors in the unit except the lead reactor has become deactivated to such an extent that the catalyst in all of the reactors other than the lead reactor must be regenerated, discontinuing the flow of the hydrocarbon stream through all of the reactors in said unit other than the lead reactor while continuing to pass the hydrocarbon stream through the lead reactor; regenerating the beds of catalyst in each of the reactors of said unit other than the lead reactor to remove the carbonaceous deposits from the catalyst in such beds and to restore at least partially the activity of the catalyst while continuing to pass the hydrocarbon stream through the lead reactor under reforming conditions; resuming the flow of the hydrocarbon stream through all of the reactors in the unit; and repeating all of the aforesaid steps until the catalyst in the lead reactor has becom

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: A process for recovering and upgrading hydrocarbons from oil shale by contacting the oil shale solids in the presence of an acidic or oxidative catalytic substance with a water-containing fluid at a temperature in the range of from at least 705.degree. F., the critical temperature of water, to about 900.degree. F., in the absence of externally supplied hydrogen, wherein the water has a density of at least 0.15 gram per milliliter. Examples of such acidic or oxidative catalytic substance are molecular oxygen, sodium bisulfate, sodium bisulfite, and carbon dioxide.

Abstract: The process comprises contacting a cracked naphtha in a reaction zone under hydrodesulfurization conditions and in the presence of hydrogen with a catalyst comprising a hydrogenation component comprising a Group VIB metal and a Group VIII metal deposited on a solid support comprising magnesium oxide. The catalyst support may also comprise a refractory inorganic oxide, such as alumina. In the latter case, the catalyst support should contain at least 70 wt.% magnesium oxide to furnish a satisfactory embodiment of the catalyst.

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: The process comprises the step of passing the nitrogen oxides through a zone maintained at conditions at which said nitrogen oxides will be reduced, said zone including a substantially rigid catalytic member of a metal support or substrate plated with one or more members selected from the group consisting of copper, nickel, iron, and chromium and having, at least in part, an oxidized surface that catalytically promotes the reduction of the oxides of nitrogen as they pass through said zone.

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 a hydrogenation component comprising a member selected from the group consisting of a metal of Group VIA, compounds of a metal of Group VIA, and mixtures thereof supported on a co-catalytic solid support comprising mordenite and a porous refractory inorganic oxide. The hydrogenation component may be characterized further by a member selected from the group consisting of rhenium, compounds of rhenium, a non-noble metal of Group VIII, compounds of a non-noble metal of Group VIII, and mixtures thereof. The preferred Group VIA metal is molybdenum.The catalyst preparation may comprise blending finely-divided mordenite into a sol or gel of the refractory inorganic oxide to form a blend, gelling the blend, if a sol is present, to form a gel by adding a solution of a suitable inorganic ammonium-affording compound, and drying and calcining the gel to form a calcined material.

Abstract: The apparatus comprises a distributing means for distributing solid particles into a vessel, a particle entry duct having an inlet end at its top and an outlet end at its bottom, and a flexible connecting means for connecting the particle entry duct to the distributing means. The top of the connecting means is attached to the particle entry duct at a point along the axis of the particle entry duct and the bottom of the connecting means is attached to the distributing means at a point where the center of gravity of the distributing means is located. The length of the connecting means is such that the bottom of the particle entry duct is on the same level as the top of the distributing means or below the top of the distributing means and the elements of the apparatus are positioned such that the periphery of the particle entry duct falls within the periphery of the top of the distributing means. Any suitable particle distributing means may be employed.

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.

Abstract: There are disclosed a method for sulfiding a multi-metallic catalyst or a bi-metallic catalyst and a method for initiating the reforming of a petroleum hydrocarbon feedstock in a reforming reaction zone containing a multi-metallic catalyst or a bi-metallic catalyst.The method for sulfiding is employed when a hydrogen-rich gas containing light hydrocarbons is used in the sulfiding of the catalyst. The method comprises passing a stream of said gas over said catalyst at a temperature of about 350.degree. F. to about 470.degree. F., injecting a sulfur-containing compound into the stream of gas up-stream from said catalyst in order to provide a sulfur-carrying gas, and contacting said catalyst with said sulfur-carrying gas at said temperature for a time that is sufficient to provide a sulfur concentration on said catalyst of about 0.1 to about 2.5 moles of sulfur per mole of total active metal. A typical sulfur-containing compound is dimethyl sulfide.

Abstract: The catalyst comprises a catalytic surface of one or more metallic oxides formed on a substantially rigid, reticulated support or substrate of a tough, strong metal or metal alloy having a melting point in excess of about 2,000.degree. F. The oxides are those of one or more members selected from the group consisting of copper, nickel, iron and chromium.The catalyst is prepared by the method comprising the steps of: (a) plating the surface of the support or substrate with one or more layers of one or more of the members to form a plated support or substrate, (b) heating in an inert atmosphere the plated support or substrate so that the atoms on the surfaces of the members interdiffuse with themselves and with surface atoms of the support or substrate, and (c) exposing the plated support or substrate to oxidizing conditions to oxidize, at least in part, the atoms at or near the surface of the plated support or substrate to form thereat oxides of the members.