Abstract: A process is disclosed to extract metal values selected from the group consisting of cobalt, molybdenum, nickel, tungsten, and vanadium from metal-containing particles, such as spent hydroprocessing catalyst particles containing carbon residue. In this process, the spent catalyst particles are roasted in an oxygen-containing gas at a temperature of from 400.degree. C. to 600.degree. C., and then the roasted catalyst particles are contacted with an aqueous solution of ammonia, ammonium salt, and hydrogen peroxide. That aqueous solution has an initial pH of at least 9.5 and an initial hydrogen peroxide concentration of from 0.02 to 0.2 M. That aqueous solution is maintained at a pH of greater than 9.5.

Abstract: The present invention is a bacteria and its use in a Microbial Enhanced Oil Recovery (MEOR) process. Any one of two newly isolated strains of bacteria are injected downhole in a petroleum reservoir to modify its profile. This bacteria has the capability to plug the zones of higher permeability within the reservoir so that a subsequent waterflood may selectively enter the oil bearing less permeable zones. The injected water is used to drive this oil to an area where it may then be recovered.

Abstract: The present invention is a process for in situ biodegradation of spilled hydrocarbons. The process involves drawing oxygen into a hydrocarbon contaminated zone. A borehole is drilled into the contaminated zone and gas is evacuated at high rates out of the borehole to thereby draw oxygen into the contaminated zone. Surprisingly, the carbon dioxide concentration in the evacuated gas remains high even at the high flow rates.

Abstract: A process for removing residual sulfur from a hydrotreated naphtha feedstock is disclosed. The feedstock is contacted with molecular hydrogen under reforming conditions in the presence of a less sulfur sensitive reforming catalyst, thereby converting trace sulfur compounds to H.sub.2 S, and forming a first effluent. The first effluent is contacted with a solid sulfur sorbent, removing the H.sub.2 S and forming a second effluent. The second effluent is contacted with a highly selective reforming catalyst under severe reforming conditions.

Abstract: Isobutene is produced by contacting isobutane with a sulfided, type L zeolitic catalyst containing platinum, tin, barium, and an inorganic binder. The isobutane is contacted with the catalyst in the presence of a sulfur-containing gas at a temperature of from 850.degree. F. to 1250.degree. F., a pressure of less than 20 psig, a liquid hourly space velocity of below 40, and an H.sub.2 /HC of less than 10. Preferably, the catalyst comprises: (1) a sulfided, type L zeolite containing from 8% to 10% by weight barium, from 0.6% to 1.0% by weight platinum, and tin at an atom ratio with the platinum of about 1:1; and (2) an inorganic binder of either silica, alumina, or aluminosilicates.

Abstract: A new catalyst is disclosed which is useful for dehydrocyclizing alkanes. This catalyst contains a type L zeolite, a Group VIII metal, and an alkaline earth metal. Preferably, this catalyst contains a type L zeolite, from 0.1% to 5% by weight platinum and from 1% to 20% by weight barium.

Abstract: A new catalyst is disclosed which is useful for dehydrocyclizing alkanes. This catalyst contains a zeolite of the L family, a Group VIII metal, and an alkaline earth metal.

Abstract: A highly selective zeolitic reforming catalyst is disclosed that contains a promoter selected from the group consisting of iron, cobalt, and titanium; and that has a platinum to promoter weight ratio of less than 10:1. In one embodiment a type L zeolite is formed by combining an aqueous solution of potassium hydroxide, aluminum hydroxide, and ferric nitrate with an aqueous solution of silica to form a thickening gel in a mother liquor; heating the thickening gel to form a type L zeolite; cooling the solution containing the type L zeolite; decanting the mother liquor from the solution; filtering the type L zeolite from the solution; washing the filtered type L zeolite so that the pH of the wash is about 101/2; and drying the washed type L zeolite. The catalyst is formed by adding platinum to the dried type L zeolite by pore fill impregnation with an aqueous solution of Pt(NH.sub.3).sub.4 (NO.sub.3).sub.2 to form a catalyst; drying the catalyst and calcining the catalyst.

Abstract: A highly selective zeolitic reforming catalyst is disclosed that contains a promoter selected from the group consisting of iron, cobalt, and titanium; and that has a platinum to promoter weight ratio of less than 10:1. In one embodiment a type L zeolite is formed by combining an aqueous solution of potassium hydroxide, aluminum hydroxide, and ferric nitrate with an aqueous solution of silica to form a thickening gel in a mother liquor; heating the thickening gel to form a type L zeolite; cooling the solution containing the type L zeolite; decanting the mother liquor from the solution; filtering the type L zeolite from the solution; washing the filtered type L zeolite so that the pH of the wash is about 101/2; and drying the washed type L zeolite. The catalyst is formed by adding platinum to the dried type L zeolite by pore fill impregnation with an aqueous solution of Pt(NH.sub.3).sub.4 (NO.sub.3).sub.2 to form a catalyst; drying the catalyst and calcining the catalyst.

Abstract: A method of dehydrocyclizing alkanes is disclosed wherein the alkanes are contacted with a catalyst containing a large-pore zeolite, a Group VIII metal, and an alkaline earth metal wherein the Selectivity Index is greater than 60%.

Abstract: A process is disclosed wherein a naphtha feed is contacted in a reaction vessel with a dehydrocyclization catalyst comprising a large-pore zeolite containing at least one Group VIII metal to produce an aromatics product and a gaseous stream, the aromatics product is separated from the gaseous stream and is passed through a molecular sieve which adsorbs paraffins present in the aromatics product, then the gaseous stream is used to strip the paraffins from the molecular sieve, and the gaseous stream and the paraffins are recycled to the reaction vessel. Preferably, the dehydrocyclization catalyst comprises a type L zeolite containing from 8% to 15% by weight barium and from 0.6% to 1.0% by weight platinum, wherein at least 80% of the crystals of the type L zeolite are larger than 1000 Angstroms, and an inorganic binder selected from the group consisting of silica, alumina, and aluminosilicates.

Abstract: A naphtha feed is contacted in a reaction vessel with a dehydrocyclization catalyst comprising a large-pore zeolite containing at least one Group VIII metal to produce an aromatics product and a gaseous stream, the aromatics product is separated from the gaseous stream and is passed through a molecular sieve which adsorbs paraffins present in the aromatics product, then the gaseous stream is used to strip the paraffins from the molecular sieve, and the gaseous stream and the paraffins are recycled to the reaction vessel.

Abstract: Process and composition for removing H.sub.2 S and like sulfides from gas streams by contact with a substituted aromatic nitrile having an electron-attracting substituent on the aromatic ring at least as strong as halogen (e.g., isophthalonitrile) and an organic tertiary amine in an inert organic solvent such as N-methyl-2-pyrrolidone.

Abstract: A reforming process is disclosed wherein a hydrocarbon feed is contacted with two reforming catalysts at conditions which favor reforming. The first reforming catalyst comprises a metallic oxide support having disposed therein a Group VIII metal. This first reforming catalyst may contain Group VIII metal promoters, such as rhenium, tin, germanium, cobalt, nickel, iridium, rhodium, ruthenium and combinations thereof. The second reforming catalyst is a non-acidic catalyst comprising a large-pore zeolite containing at least one Group VIII metal. A preferred first reforming catalyst comprises alumina having disposed therein in intimate admixture platinum and rhenium. A preferred second reforming catalyst is a non-acidic catalyst comprising a type L zeolite containing platinum.

Abstract: A new catalyst is disclosed which is useful for dehydrocyclizing alkanes. This catalyst contains a zeolite of the L family, a Group VIII metal, and an alkaline earth metal.

Abstract: A hydrocarbon conversion process is disclosed wherein the alkanes are contacted with a catalyst containing a metallic oxide support and a Group VIII metal, and with a catalyst containing a large-pore zeolite, a Group VIII metal, and an alkaline earth metal.

Abstract: A new catalyst is disclosed which is useful for dehydrocyclizing alkanes. This catalyst contains a type L zeolite, a Group VIII metal, and an alkaline earth metal. Preferably, this catalyst contains a type L zeolite, from 0.1% to 5% by weight platinum and from 1% to 20% by weight barium.

Abstract: A method of dehydrocyclizing alkanes is disclosed wherein the alkanes are contacted with a catalyst containing a large-pore zeolite, a Group VIII metal, and an alkaline earth metal wherein the Selectivity Index is greater than 60%.

Abstract: A hydrocarbon conversion process is disclosed wherein a hydrocarbon feed is contacted with a reforming catalyst in the presence of a halogen at conditions which favor dehydrocyclization, isomerization, and dehydroisomerization of the hydrocarbon feed. The degree of the isomerization and dehydroisomerization is controlled by adjusting the amount of halogen present. The amount of halogen present can be adjusted on stream by the addition of halogen-containing gas or water. The reforming catalyst comprises a large-pore zeolite, containing at least one Group VIII metal. In one embodiment, the reforming catalyst comprises: (a) a large-pore zeolite containing barium and platinum; and (b) an acidic or acidifiable inorganic binder selected from the group consisting of silica-alumina, zirconia-silica and alumina.

Abstract: A hydrocarbon feed is contacted with a reforming catalyst in a reaction vessel to produce a reformate, hydrogen, methane, and ethane are stripped from the reformate in a first separator, C.sub.3 -C.sub.5 hydrocarbons are stripped from the stripped reformate in a second separator, and then a portion of the hydrogen, methane, and ethane; and substantially all of the C.sub.3 -C.sub.5 hydrocarbons are recycled to the reaction vessel as heat carrier.