Abstract: Indigenous metal impurities in an oil are removed by contacting the oil with a novel solid consisting essentially of porous alumina containing a minor amount of phosphorus. The contacting is carried out under oil demetallizing conditions.

Abstract: Suspended mineral solids are separated from a coal-derived liquid containing the solids by a process comprising the steps of: (a) contacting said coal-derived liquid containing solids with a molten additive having a melting point of 100.degree.-500.degree. C. in an amount of up to 50 wt.

Abstract: Unsaturated C.sub.4 hydrocarbons are converted into normal butane by introducing an unsaturated C.sub.4 hydrocarbon stream into a hydrogenation zone to convert it into a stream of normal butane and isobutane. Normal butane is recovered from a separation zone while isobutane is directed to an isomerization zone wherein a portion of the isobutane is converted into normal butane. The stream from the isomerization zone is returned to the separation zone to recover the normal butane produced in the isomerization reaction. The normal butane produced by the process is subsequently utilized in a cracking zone to produce ethylene.

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: In a fractionation system wherein a stream of heat-containing fluid is taken from a zone effecting at least a partial control of at least one operating condition in said zone by withdrawing said fluid at a rate responsive to and correlated with a change in said condition and utilizing the heat in said withdrawn fluid.

Abstract: In a process for the production of olefins in two stages wherein, in the first stage, heavy petroleum fractions are hydrogenated in the presence of hydrogen and a hydrogenation catalyst and, in the second stage, the thus-hydrogenated fractions are subjected to thermal cracking the presence of steam, the improvement which comprises employing as the hydrogenation catalyst a zeolite of the faujasite structure combined with elements from Groups VIB, VIIB and VIII of the periodic table of the elements, wherein the alkali component of the zeolite is exchanged at least partially for ammonium, hydronium, alkaline earth and/or rare earth ions, and the elements are present in a metallic, ionic, oxidic and/or sulfidic form.

Abstract: Purity of hydrocarbon streams is increased by contacting with stable oxides of calcium, titanium, zinc, or zirconium prior to passage to a catalytic conversion process. In one embodiment, the stable metal oxides are preactivated by heating with vaporous hydrocarbon at an elevated temperature which is effective in extending the temperature at which metal oxides are subsequently effective for purification of hydrocarbon streams.

Abstract: Thiophenes are selectively removed from gasoline by contact thereof with a silver-exchanged faujasite-type zeolite.

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 invention provides a titania-zirconia or a titania-zirconia-alumina catalyst base containing a system of metals, metal oxides or metal sulfides from Groups VIB, VIIB and VIII of the Periodic Table. Such catalyst are useful in the hydrodesulfurization and denitrogenation of hydrocarbon feed stocks and the saturation of aromatics contained therein.

Abstract: A method for reducing the nitrogen content of a feed stream derived from oil shale and/or coal comprising hydrodenitrogenating the feed stream, subjecting the hydrodenitrogenated feed stream to first flashing conditions to remove hydrogen, hydrogen sulfide, and ammonia, dehydrogenating the remainder of the feed stream, and subjecting the dehydrogenated feed stream to second flashing conditions to separate hydrogen from the process product.

Abstract: An HF alkylation-fractionation system for the separation of the hydrocarbon phase separated from the HF alkylation effluent by passing the hydrocarbon phase first to a prefractionation zone operated at low pressure, followed by fractionation of both overhead and bottoms from the prefractionation zone at higher pressures and temperatures, and utilization of the high temperature streams obtained from the higher pressure fractionations as sources of heat for indirect heat exchange of the prefractionation zone and feed to at least one of the subsequent fractionations.

Abstract: In the recovery of ethane and propane from an alkylation of an isoparaffin with an olefin to prevent buildup of ethane and propane in the system, the ethane and propane are taken as a side draw from the conventional HF stripper instead of being vented from the depropanizer or the fractionator overhead accumulator. Considerable ethane, propane and HF are thus saved and equipment costs reduced, especially because fractionator wall thickness can be reduced and because of the elimination of the equipment attendant the venting of the accumulator.

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: Isomeric mixtures of non-polar disubstituted aromatic compounds are brought into contact with a shape selective crystalline zeolite catalyst, under cracking or transalkylation conditions, to undergo selective reaction of the 1,4-isomer, thereby leaving the 1,2-isomer and/or 1,3-isomer in excess of equilibrium. The shape selective zeolite catalyst employed herein comprises a crystalline zeolite having a silica to alumina ratio of at least 12 and a constraint index, as herein defined, within the approximate range of 1 to 12.

Abstract: An olefin and isoparaffin are contacted in the presence of an acid alkylation catalyst to form an alkylate-containing alkylation effluent. The effluent is separated with the hydrocarbon phase passing to a prefractionation zone. A side stream from the prefractionation zone is passed in indirect heat exchange relationship with an interheater of an isostripper thereby providing a majority of the heat necessary to reboil the isostripper.

Abstract: A fresh charge containing aromatic hydrocarbons is hydrotreated in admixture with a recycle fraction, in the presence of a bifunctional catalyst, a portion of the effluent is subjected to steam-cracking, thereby recovering a gas oil fraction which is subjected to hydrogenation and forms said recycle fraction. The mixture of recycle fraction and charge is advantageously treated with hydrogen in the presence of a monofunctional catalyst to hydrogenate olefins, at a lower temperature than the hydrotreatment, and then passed to the hydrotreatment zone.

Abstract: A feed slurry containing fine solids, polar liquids and premium liquid oil and produced by high temperature hydrogenation of a solid fuel, such as coal, is separated into a first fraction comprising the premium liquid oil and a second fraction comprising the fine solids and polar liquids by (a) contacting the feed slurry with a solvent, such as (1) C.sub.5 -C.sub.9 aliphatic hydrocarbon (2) C.sub.5 -C.sub.9 alicyclic hydrocarbon or (3) naphthenic or paraffinic fraction of a coal liquefaction product containing less than 10 wt. % aromatics at a temperature of 100.degree.-250.degree. C. and pressure sufficient to maintain the feed slurry and solvent in the liquid state but less than 450 psi. The feed slurry is introduced at or near the top of a contacting zone of a vertical column, which also has an upper settling zone and a lower collection zone, and the solvent is introduced at or near the bottom of the contacting zone of said column at a solvent; slurry wt ratio of at least 0.

Abstract: Process and apparatus for the desalting and dehydration of crude oil wherein, the crude oil is washed in one or several stages using fresh or recirculated hot water containing a demulsifier. The crude oil is also passed through a coalescence stage, and a settling stage aimed at obtaining a salt content to meet crude oil specifications. Subsequently the crude oil is led into a lower stripping compartment of a column, in which dehydration is carried out to the desired level by using fuel or combustion gas, the stripping temperature being reached by heating the crude or the gas or both, the gas-vapor mixture being cooled in the upper compartment of the column by a cooling fluid such as the untreated crude oil or recirculated or fresh water, depending upon the nature and salt content of the crude. The cooled gas is recirculated within the column or led to a pipeline for consumption, while the cooling fluid, in the case of water, is recirculated in the unit.

Abstract: A process and catalyst for the alkylation of isoparafffins is disclosed. The catalyst is an unsupported solid perfluorinated polymer containing pendent sulfonic acid groups.