Abstract: An isomerization zone process is disclosed that combines a deisohexanizer with a PSA separation section to provide a product stream comprising methylbutane and dimethylbutane. The process combines a methylpentane and normal hexane recycle stream, a normal pentane recycle stream and a fresh feedstream to provide a combined feedstream that is charged to an isomerization zone. The effluent from the isomerization zone is stabilized and passed to a deisohexanizer. A sidecut stream carries the methylpentane and normal hexane recycle stream from the deisohexanizer. Hydrocarbons having a higher boiling point than the sidecut stream are withdrawn as a bottoms stream from the deisohexanizer. An overhead carries normal pentane, methylbutane and dimethylbutanes to the PSA separation section. An extract stream is recovered as the normal pentane recycle stream. The raffinate from the PSA provides a high octane isomerate stream comprising mainly methylpentane and dimethylbutanes.

Abstract: Catalytic hydrodealkylation by means of a catalyst which comprises microporous particles having a catalytic species carried thereon. Particulars of the microporous particles are disclosed.

Abstract: A process using zeolites, or molecular sieves, for separating an alpha-olefin having five or more carbons and the corresponding internal olefin or olefins. A mixture containing the alpha-olefin and one or more of the corresponding internal olefins is contacted with a zeolite which had previously undergone cation exchange. The selectivity of the zeolite, or molecular sieve, changes and eventually reverses as the carbon number increases. The selectivity is also related to the identity of the cation introduced during the cation exchange.

Abstract: Raffinate yield from solvent extraction is improved when the extract phase recovered from the solvent extraction process is subjected to a membrane separation step wherein a saturates/1-ring aromatics rich retentate is produced and a 2+ ring aromatics rich permeate are produced and the saturates/1-ring aromatic rich retentate phase is recycled to the solvent extraction process.

Abstract: A process for removing vinylidene olefin from an olefin mixture containing about 1 to 55 mole percent vinylidene olefin, 0 to 20 mole percent internal olefin and the balance vinyl olefin, said process comprising:(a) reacting said olefin mixture in the presence of a BF.sub.3 /phosphorus acid catalyst system so as to selectively dimerize vinylidene olefins, and(b) separating said vinyl olefin and internal olefin from the dimerized vinylidene olefin to produce an olefin product having a reduced vinylidene olefin content and an increased vinyl olefin content compared to said starting olefin mixture.

Abstract: The present invention provides a highly selective catalytic cracking process for the conversion of feedstocks containing a predominant content of C.sub.10 and higher mixed olefins into C.sub.9 and lower olefin products at efficiencies of greater than 20%. said products further characterized in that the content C.sub.6 to C.sub.9 olefins is maximized while the content of C.sub.2 to C.sub.4 olefins is minimized. The process involves contacting an olefin feedstock mixture containing at least about 50 weight %, more preferably at least about 70 weight %, of C.sub.10 and higher olefins under cracking conditions with a catalyst selected from the group consisting of amorphous precipitated silica, selected crystalline silicates and aluminosilicates, namely beta, mordenite and ZSM-5 types, as well as ion exchanged or acid variants thereof. Cracking conditions include a temperature within the range of from about 250.degree. up to about 450.degree. C.

Abstract: A method for preparing one or more diemthylnaphthalenes from one or more dimethyltetralins, and optionally for preparing one or more other specific dimethylnaphthalenes by isomerization of the aforesaid dimethylnaphthalene(s) is disclosed.

Abstract: The present invention is directed to a process for treating hydrotreated naphtha which involves treating the naphtha over massive nickel catalyst followed by treating the naphtha over a metal oxide under conditions effective for removing impurities from said naphtha to result in substantially purified naphtha, wherein the metal oxide is selected from the group of metal oxides having a free energy of formation of sulfide which exceeds said free energy of formation of platinum sulfide, such as manganous oxide. In so doing, naphtha in the gas phase in the presence of hydrogen is passed over the manganous oxide at a temperature within the range of about 800.degree. F. and 1100.degree. F., a hydrogen to oil molar ratio between about 1:1 and 6:1, a whsv between about 2 and 8, and pressure between about 50 and 300 psig; and the naphtha in the liquid phase at a temperature between about 300.degree. F. and about 350.degree. F., and whsv less than about 5 is passed over the massive nickel.

Abstract: The process relates to converting normal paraffins and/or mono-methyl branched paraffins, which are generally of low octane value, to more highly branched isoparaffins which are generally superior to normal paraffins in octane.

Abstract: Naphthenic hydrocarbons are separated from aliphatic rich hydrocarbon feeds comprising mixtures of naphthenes with paraffinic hydrocarbons by a membrane extraction process whereby the hydrocarbon feed is contacted with one face of a porous, non-selective partition barrier membrane while simultaneously contacting the other side of said membrane with a polar solvent such as ethylenediamine. The naphthenic hydrocarbon preferentially migrates through the porous membrane partition barrier in response to the polar solvent present on the permeate side of the barrier.

Abstract: Non-normal, branched paraffins (isoparaffins) are separated from hydrocarbon feeds comprising mixtures of isoparaffins and normal paraffins by the procedure involving the steps of contacting the hydrocarbon feed with one face of a non-selective, microporous partition barrier membrane while simultaneously contacting the opposite face of said membrane, preferably in countercurrent flow, with a polar solvent. The isoparaffins in the feed selectively permeate across the porous partition barrier membrane in response to the polar solvent to the solvent side of the membrane whereby a permeate enriched in isoparaffins and a retentate of decreased isoparaffin content as compared to the feed are obtained.

Abstract: The present invention relates to the improved skeletal isomerization of olefins over molecular sieve catalysts, the improvement comprising carrying out the skeletal isomerization at a temperature above 900.degree. F.

Abstract: The invention relates to the production of high octane fuels including a process for separating the high octane components for the gasoline pool from lower octane components, which are recycled to an isomerization reaction by adsorptively separating dimethyl paraffins from an isomerate with an aluminophosphate zeolite and SSZ-24, an all-silica zeolite adsorbent isostructural with AIPO.sub.4 -5, and a C.sub.6-10 normal paraffin desorbent. The lower octane components of the isomerate, normal paraffins and mono-branched paraffins, are recycled to the isomerization reaction zone for further conversion to multi-branched paraffins. The useful aluminophosphates are SAPO-5, AIPO.sub.4 -5 MgAPO-5 and MAPSO-5.

Abstract: A simultaneous recovery of pure benzene and pure toluene is performed by extractive distillation with N-formylmorpholine and/or other N-substituted morpholines whose substituents contain not more than seven C-atoms as a solvent. From the entry product by predistillation, a benzene fraction boiling in the region between 75.degree. and 85.degree. C. and a toluene fraction boiling in the region between 99.degree. and 111.degree. C. is separated. The benzene fraction is supplied in the lower part, and the toluene fraction is supplied in the upper part of the extractive distillation column separated by a chimney plate into two parts.

Abstract: An improved process for regeneration of catalyst used in fluidized catalytic cracking of hydrocarbons using a cross-flow or swirl type catalyst regenerator is disclosed. Instead of a single catalyst withdrawal outlet for regenerated catalyst, multiple catalyst withdrawal points are provided. Use of multiple catalyst outlets, or a continuous radial catalyst outlet, greatly reduces stagnant regions in the bed. The process is useful in FCC units having inventories of from 10 to 100 tons of catalyst.

Abstract: A liquid catalyst composition for the oxidative coupling of methane and other hydrocarbon compounds to produce higher hydrocarbons and for the oxidative dehydrogenation of aliphatic and alicyclic hydrocarbon compounds, aliphatic and alicyclic substituted aromatic hydrocarbons, and mixtures thereof is disclosed.

Abstract: Toothed-wheel shaped particles are used as catalysts in the dehydrogenation of hydrocarbons, particularly ethylbenzene to styrene.

Abstract: The fluidity at low temperatures of compositions based on liquid hydrocarbons from refining is improved by the addition, preferably in solution, of ethylene/propylene/(conjugated diene) copolymers or terpolymers, containing 20-55% of propylene, optionally degraded by thermo-oxidation, and structurally characterized by values of at least one of X.sub.2 and X.sub.4 parameters, which are equal to, or lower than, about 0.02, indicative of the absence in the polymeric chain of propylene linking inversions.

Abstract: Disclosed is a method for catalytically hydropyrolyzing carbonaceous material to produce liquid products boiling under about 550.degree. C. with reduced amounts of methane being formed. The process comprises (a) treating the carbonaceous material with as hydrogenation catalyst; (b) contacting the so-treated carbonaceous material with an effective amount of hydrogen, at an effective residence time, at a temperature below the critical temperature of rapid methane formation; (c) recovering the resulting liquids, gases, and char; and (d) recycling the char.

Abstract: The yield, raffinate product quality, and throughput of the selective solvent extraction of hydrocarbon feeds is improved by subjecting the hydrocarbon feeds from which aromatic hydrocarbons are to be selectively solvent extracted to a membrane separation process which selectively permeates aromatics through the membranes to produce a permeate rich in aromatics and a retentate rich in saturates and 1-ring aromatics and subjecting this retentate to the selective solvent extraction process.