Abstract: The present invention relates to a process for selectively producing C3 olefins from a catalytically cracked or thermally cracked naphtha stream by fractionating the naphtha feed to obtain at least a C6 rich fraction and feeding the C6 rich fraction into a reaction stage at a point wherein the residence time of the C6 rich fraction is minimized.

Abstract: The present invention relates to a process for selectively producing C3 olefins from a catalytically cracked or thermally cracked naphtha stream by fractionating the naphtha feed to obtain a C6 fraction and feeding the C6 fraction either in the riser downstream of the injection point for the reminder of the naphtha feed, in the stripper, and/or in the dilute phase immediately downstream or above the stripper of a process unit.

Abstract: A process for the disproportionation and transalkylation of toluene and the heavy aromatics comprises: subjecting a first stream of toluene, and a stream enriched in aromatics of nine carbon atoms to toluene disproportionation and transalkylation reactions in the presence of hydrogen in a first reaction zone to produce a first product mixture comprising benzene, aromatics of eight carbon atoms and heavy aromatics of ten and more carbon atoms; subjecting a second stream of toluene, and a stream enriched in heavy aromatics of ten and more carbon atoms to transalkylation reaction in the presence of hydrogen in a second reaction zone to produce a second product mixture comprising benzene, aromatics of eight carbon atoms and aromatics of nine carbon atoms; and isolating and recovering benzene and aromatics of eight carbon atoms from the first and second product mixtures.

Abstract: An attrition resistant precipitated bulk iron catalyst is prepared from iron oxide precursor and a binder by spray drying. The catalysts are preferably used in carbon monoxide hydrogenation processes such as Fischer-Tropsch synthesis. These catalysts are suitable for use in fluidized-bed reactors, transport reactors, and, especially, slurry bubble column reactors.

Abstract: The present invention relates to a process for the selective disproportionation of toluene and the disproportionation and transalkylation of toluene and C9+ aromatics to mainly solve the problems in the prior arts of the great amount of recycle stream, high energy consumption or harsh requirement for the reaction feedstocks. The present invention has better solved these problems by the technical solution using a process for selective disproportionation of toluene to produce mixed xylenes containing a high concentration of p-xylene, and subsequent disproportionation and transalkylation of C9+ aromatics and toluene to produce benzene and the mixed xylenes which are in the thermodynamic equilibrium. The process is applicable to the industrial production.

Abstract: A process comprises separating a naphtha feed into a fraction comprising C7− hydrocarbons and a heavy C8+ fraction, separating the C8+ fraction into a light fraction comprising C8 and/or C8-C9 which then is reformed to produce gasoline and/or a desired distribution of aromatics.

Abstract: A slurry Fischer-Tropsch hydrocarbon synthesis process for synthesizing liquid hydrocarbons from synthesis gas in a hydrocarbon synthesis reactor also hydroisomerizes the synthesized hydrocarbon liquid, which comprises the slurry liquid, in one or more downcomer reactors immersed in the slurry body in the synthesis reactor. A monolithic catalyst is preferably used for the hydroisomerization, and slurry circulation down through the downcomer reactors from the surrounding slurry body, is achieved at least in part by density-difference driven hydraulics created by removing gas bubbles from the slurry passed into the downcomers. Preferably, catalyst particles are also removed before the slurry contacts the catalyst. Hydroisomerization occurs while the synthesis reactor is producing hydrocarbons, without interfering with the hydrocarbon synthesis reaction.

Abstract: This invention relates to a process to produce propylene from a hydrocarbon feed stream, preferably a naphtha feed stream, comprising C5 and C6 components wherein a light portion having a boiling point range of 120° C. or less is introduced into a reactor separately from the other components of the feed stream.

Abstract: An aliphatic alkylate with a high octane number is prepared from a C4 catalytic cracking or steam-cracking fraction that contains mainly isobutane, isobutene, butene-1 and butenes-2 by: (a) hydro-isomerizing said C4 fraction, obtaining a mixture that contains for the most part butenes-2, isobutene and isobutane; (b) separating, by distillation of the hydro-isomerized fraction, of a butene-2-rich effluent that is collected at the bottom and an isobutane- and isobutene-rich effluent that is collected at the top; (c) sending said isobutene- and isobutane-rich effluent into a hydrogenation zone that produces an effluent that for the most part contains isobutane; (d) sending of said butenes-2-rich effluent that is derived from (b) and of said effluent that for the most part contains the isobutane that is derived from (c) into an alkylation zone producing, by addition of isobutane to butenes-2, an isooctane mixture that contains excess isobutane; (e) separating by distillation of excess isobutane, which comes

Abstract: A process is provided for producing high purity benzene and high purity paraxylene from a hydrocarbon feed. In one aspect, the process comprises: (a) reforming a hydrocarbon feed using either a monofunctional catalyst or a bifunctional catalyst to provide one or more reformate streams; (b) fractionating the reformate stream to provide a toluene stream, a benzene stream, and a xylene stream; (c) subjecting the toluene stream to disproportionation; (d) purifying the benzene stream by extraction followed by distillation to provide a high purity benzene product; and (e) purifying the xylene stream by simulated moving bed countercurrent adsorption followed by crystallization to provide a high purity paraxylene product.

Abstract: The invention concerns a process for isomerising a feed containing essentially hydrocarbons, preferably paraffins containing principally 4 to 8, preferably princiapply to 6 and more principally 5 and/or 6 carbon atoms per molecule, comprising a fractionation zone and at least two isomersation reaction zones, said process comprising carrying out the following steps:(1) sending the feed to a fractionation zone;(2) drawing off at least a portion of the liquid circulating in said zone, via at least two draw-off levels; and(3) sending the major portion of the liquid drawn off in step (2) to at least two isomerisation zones, each isomerisation zone being associated with a draw-off level.

Abstract: Hydrocarbon feedstocks are hydroprocessed in parallel reactors, while hydrogen flows in series between the reactors. A first hydrocarbon feedstock and a hydrogen-rich recycle gas stream are introduced to a first reactor, where a first reactor effluent stream is produced and fed to a first separator, which separates the first reactor effluent stream into a first hydrogen-rich gas stream and a first hydroprocessed product stream. The first hydrogen-rich gas stream and a second hydrocarbon feedstock are fed to a second reactor, where a second reactor effluent stream is produced and fed to a second separator, which separates the second reactor effluent stream into a second hydrogen-rich gas stream and a second hydroprocessed product stream. A make-up hydrogen stream is added to the second hydrogen-rich gas to form the hydrogen-rich recycle gas stream that is compressed and fed to the first reactor.

Abstract: The invention concerns a process for isomerizing a feed containing essentially hydrocarbons, preferably paraffins containing principally 4 to 8, preferably principally 4 to 6 and more preferably principally 5 and/or 6 carbon atoms per molecule, comprising a fractionation zone and at least two isomerization reaction zones, said process comprising carrying out the following steps:(1) sending the feed to a fractionation zone;(2) drawing off at least a portion of the liquid circulating in said zone, via at least two draw-off levels;(3) sending the major portion of the liquid drawn off in step (2) to at least two isomerization zones, each isomerization zone being associated with a draw-off level;(4) sending the major portion of the effluents from step (3) to the fractionation zone, substantially adjacent to the draw-off levels;(5) recovering an effluent from the fractionation zone.

Abstract: A process is provided to react a feedstock comprising isobutane with pentenes in the presence of sulfuric acid catalyst to produce a high octane alkylate as well as a higher octane isopentane gasoline blending component. A method to reduce sulfuric acid consumption during alkylation is provided wherein a diolefinic contaminant of a pentene system feed is selectively hydrogenated before alkylation. An alkylation method is provided wherein the alkylation feed is separated into a fraction comprising substantially C.sub.4 and lower olefins and a fraction comprising substantially C.sub.5 olefins and the stream comprising C.sub.5 olefins is alkylated in a different reactor than the fraction comprising substantially C.sub.4 and lower olefins.

Abstract: A process is provided to react a feedstock comprising isobutane with pentenes in the presence of sulfuric acid catalyst to produce a high octane alkylate as well as a higher octane isopentane gasoline blending component. A method to reduce sulfuric acid consumption during alkylation is provided wherein a diolefinic contaminant of a pentene system feed is selectively hydrogenated before alkylation. An alkylation method is provided wherein the alkylation feed is separated into a fraction comprising substantially C.sub.4 and lower olefins and a fraction comprising substantially C.sub.5 olefins and the stream comprising C.sub.5 olefins is alkylated in a different reactor than the fraction comprising substantially C.sub.4 and lower olefins.

Abstract: A process is disclosed that provides a high conversion of n-butane to C.sub.5 + gasoline by integrating the medium pore metallosilicate catalyzed process for fresh n-butane conversion to C.sub.5 + gasoline with a medium pore metallosilicate catalyzed process for propane conversion in a manner which allows a portion of the propane by-product of n-butane conversion to be converted to C.sub.4 + alkanes, followed by recycle of the n-butane portion of the C.sub.4 + alkanes. It has been discovered that separation of the products from the separate propane and n-butane conversion steps can be carried out concurrently in a single fractionator to provide the C.sub.5 + gasoline product and the propane and butane recycle streams. Preferably, the fractionator butane cut is treated in a deisobutanizer to recover isobutane and n-butane recycle. A further discovery utilizes the common fractionator not only to separate the products from the conversion processes but to concurrently separate a mixed fresh C.sub.3 -C.sub.

Abstract: The invention is directed to method of making a thermally and oxidatively stable lubricating oil having a high viscosity index and a low pour point by the thermal polymerization of 1-olefins containing 8 to 10 carbon atoms, the preferred 1-olefins are 1-decanes. The polymerization is conducted at temperatures ranging from 280.degree. C. to 350.degree. C. and low pressures, of less than about 280 psig, in a reactor which is free of catalytic material. Thereafter, the polyalphaolefin is hydrotreated over a nickel catalyst, preferably nickel on Kieselguhr. In an improved process the polyalphaolefin is separated from a low molecular weight product by distillation. The low molecular product contains unreacted 1-olefins which are recycled to the thermal polymerization zone to produce more of the lubricant base stock.

Abstract: The present invention provides a process for decreasing the energy consumption of a catalytic cracking process product recovery section while improving gasoline yield by integrating multistage vapor compression and product recovery with deacidification and conversion of C.sub.2 -C.sub.4 aliphatics to C.sub.5 + normally liquid hydrocarbons.

Abstract: A process is disclosed for decreasing the emission of airborne pollutants from an oil refinery and for upgrading a paraffinic feedstream to olefins and/or aromatics. Flue gas from a fluid catalytic cracking process catalyst regenerator is cooled to supply the endothermic heat of reaction for a paraffin upgrading reaction, eliminating the need for an additional process furnace. The process further decreases airborne pollutant emissions by upgrading paraffinic fractions which would otherwise be burned as fuel.

Abstract: A continuous multistage process for preparing gasoline and/or distillate range hydrocarbons from lower molecular weight oxygenate feedstock wherein hydrocarbon yield is increased by recovering a vapor stream rich in ethene from an oxygenates conversion stage and reacting the ethene in a high severity reaction zone containing high activity zeolite catalyst.

Abstract: A process for reforming a hydrocarbon fraction having a limited proportion of C.sub.9 + hydrocarbons. A hydrocarbon fraction is separated into a light fraction and a heavy fraction, the light fraction containing less than 10% by volume of C.sub.9 + hydrocarbon. The light fraction is reformed in the presence of a monofunctional catalyst, and the heavy fraction is reformed in the presence of a bifunctional catalyst.

Abstract: Liquified Natural Gas (L.N.G.) is re-vaporized by heat exchange and pre-heated in a furnace at a temperature not exceeding 1100.degree. C. It is fed, together with an ionized hydrogen plasma stream, into a reactor containing a catalyst of the type described in the co-pending application No. 688,058. After heat exchange with the vaporizing L.N.G., the reactor effluent is separated into a condensed low-vapor-pressure liquid hydrocarbon product, rich in aromatics, into a hydrogen-rich gaseous by-product and into a recycle gas stream. The process is of particular interest where thermal or electrical energy is available at low cost. The Liquified Natural Gas Conversion Process may be considered as a method for storing such energy because the resulting liquid hydrocarbon product can be stored at low cost and may be sold during periods when such energy is in surplus.

Abstract: Natural gas hydrocarbon components, methane to butanes, are converted into low-vapor-pressure liquid hydrocarbons in a combination process which comprises successively passing the heavier fraction (C.sub.2 to C.sub.4) and the lighter fraction (C.sub.1, C.sub.2) with hydrogen over a non silica-based catalyst including crystals of basic mixed oxides and recovering C.sub.5 + hydrocarbons. First the heavier fraction of the feed (C.sub.2 +) is converted at temperatures below 600.degree. C. over a fluidized or moving catalytic bed. Condensible C.sub.3 + products are fractionated for C.sub.5 + recovery and for C.sub.3, C.sub.4 recycling. Gas by-products H.sub.2, C.sub.1, C.sub.2, are separated into an enriched hydrogen stream and into a C.sub.1, C.sub.2 by-product gas which is recycled into the lighter fraction C.sub.1, C.sub.2 of the feed.

Abstract: Vent gases containing propane and HF obtained from a hydrocarbon alkylation operation are treated together with an alkylate either before or after it has been debutanized thus to remove HF from said vent gases and/or the vent gases are combined with a normal butane stream before it is treated to remove HF therefrom thus to remove HF from said vent gases. In any event described, the propane in the vent gases is advantageously recovered in the normal butane containing stream.

Abstract: A process for treating a hydrocarbon composition containing both straight chain and non-straight chain hydrocarbons in which said hydrocarbon composition is separated into a straight chain hydrocarbon-rich fraction and a non-straight chain hydrocarbon-rich fraction, non-aromatics in said non-straight chain hydrocarbon-rich fraction are converted to aromatics, and at least a portion of the straight chain hydrocarbon-rich fraction is passed in combination with steam over a steam active catalyst comprising at least one Group VIII metal and a tin modified Group II metal aluminate under conditions such that aromatics are produced.