Abstract: A process and a system for reforming and upgrading a heavy naphtha feedstock may include dehydrogenating naphthenes in the heavy naphtha feedstock to form a first effluent stream comprising aromatics and then separating the aromatics via extraction from the produced first effluent stream to produce a second effluent stream containing raffinate paraffins. The process may then include subjecting the second effluent stream to cyclization reactions to produce a third effluent stream comprising aromatics and then combining the first effluent stream and the third effluent stream prior to extraction.

Abstract: An apparatus for reforming a hydrocarbon stream is presented. The apparatus involves changing the design of reformers and associated equipment to allow for increasing the processing temperatures in the reformers and heaters. The reformers are operated under different conditions to utilize advantages in the equilibriums, but require modifications to prevent increasing thermal cracking and to prevent increases in coking.

Abstract: A process for converting a gaseous hydrocarbon feed comprising methane to an aromatic hydrocarbon is integrated with liquefied natural gas (LNG) and/or pipeline gas production. The gaseous hydrocarbon feed is supplied to a conversion zone comprising at least one dehydroaromatization catalyst and is contacted with the catalyst under conversion conditions to produce a gaseous effluent stream comprising at least one aromatic compound, unreacted methane and H2. The gaseous effluent stream is then separated into a first product stream comprising said at least one aromatic compound and a second product stream comprising unreacted methane and H2. The second product stream is further separated into a methane-rich stream and a hydrogen-rich stream and at least part of the methane-rich stream is passed to LNG and/or pipeline gas production.

Abstract: The present invention relates to a method and system for recovering aromatics from a naphtha feedstock obtained from a crude petroleum, natural gas condensate, or petrochemical feedstock. The method and system comprise the steps of recovering an aromatics fraction from the feedstock prior to reforming.

Abstract: Methods and processes for producing paraxylene from catalytic cracking hydrocarbons, particularly C4 and C5+ streams, are disclosed. Each of the processing steps may be tailored to the overall objective of high paraxylene yield from a relative inexpensive feedstock.

Abstract: A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and passing each feedstream to separation reformers. The reformers are operated under different conditions to utilize the differences in the reaction properties of the different hydrocarbon components. The process utilizes a common catalyst, and common downstream processes for recovering the desired aromatic compounds generated.

Abstract: A process for reforming a hydrocarbon stream is presented. The process involves increasing the processing temperatures in the reformers. The reformers are operated under different conditions to utilize advantages in the equilibriums, but require modifications to prevent increasing thermal cracking and to prevent increases in coking. The process utilizes a common catalyst, and common downstream processes for recovering the desired aromatic compounds generated.

Abstract: A hydrocarbon aromatization process comprising adding a nitrogenate, an oxygenate, or both to a hydrocarbon stream to produce an enhanced hydrocarbon stream, and contacting the enhanced hydrocarbon stream with an aromatization catalyst, thereby producing an aromatization reactor effluent comprising aromatic hydrocarbons, wherein the catalyst comprises a non-acidic zeolite support, a group VIII metal, and one or more halides. Also disclosed is a hydrocarbon aromatization process comprising monitoring the presence of an oxygenate, a nitrogenate, or both in an aromatization reactor, monitoring at least one process parameter that indicates the activity of the aromatization catalyst, modifying the amount of the oxygenate, the nitrogenate, or both in the aromatization reactor, thereby affecting the parameter.

Abstract: The present invention provides an integrated process for producing ethylene and aromatic hydrocarbons, specifically benzene, which comprises: (a) introducing a mixed lower alkane feed into a cracker to produce a product mixture which is comprised of ethylene and C3+ products and possibly unreacted ethane, (b) separating and recovering ethylene, (c) contacting the C3+ products and any unreacted ethane with an aromatic hydrocarbon conversion catalyst to produce a product mixture which is comprised of aromatic reaction products including benzene, and (d) recovering benzene and any other aromatic reaction products.

Abstract: The present invention provides an integrated process for producing ethylene and aromatic hydrocarbons, specifically benzene, which comprises: (a) contacting a mixed lower alkane feed with an aromatic hydrocarbon conversion catalyst to produce a product mixture which is comprised of aromatic reaction products including benzene, unreacted ethane and non-aromatic products, (b) separating and recovering the benzene and any other aromatic reaction products, (c) separating and recovering the ethane, and (d) introducing the ethane into a cracker to produce ethylene.

Abstract: A process for producing aromatic hydrocarbons which comprises a) contacting ethane or mixed lower alkanes with an aromatic hydrocarbon conversion catalyst to produce reaction products including benzene, b) separating methane, hydrogen, and C2-5 hydrocarbons from the reaction products of step a), and c) hydrodealkylating the remaining reaction products to produce benzene. In a preferred embodiment, the feed is split into two streams, one of which is catalytically or thermally cracked to produce ethylene which is then combined with the remaining ethane or lower alkanes and contacted with the aromatic hydrocarbon conversion catalyst.

Abstract: A process for producing an aromatic compound which can effectively decrease the contents of halogen elements in the aromatic compound and an aromatic compound which is produced in accordance with the process and useful as the material for obtaining an organic electroluminescence device having a long life are provided. The process for producing an aromatic compound comprises bringing an aromatic compound which is produced via an intermediate compound having halogen elements and has contents of halogen elements of 10 to 1,000 ppm by mass into reaction with a dehalogenating agent to decrease the contents of halogen elements to 10 ppm by mass or smaller, and an aromatic compound which is produced in accordance with the process.

Abstract: Disclosed is a system of making an olefin derivative from a dilute olefin feed. Dilute olefin is sent to an olefin reaction unit to form an olefin derivative product. The olefin derivative product is recovered from the reaction unit while a vent stream is also removed. Olefin is separated from the vent stream, and the olefin is sent to the olefin reaction unit for additional processing.

Abstract: There is provided with a process for separating normal paraffins from hydrocarbons of C5-10 using zeolite molecular sieve 5A, which comprises the steps of (a) selective adsorption (b) cocurrent purge (c) countercurrent desorption. The present process employs butane for purge and desorption step to achieve excellent desorption efficiency and recycles butane in liquid phase to reduce the investment cost. The optimum operating conditions for feedstock change and adsorption capacity reduction are determined by NIR system for on-line monitoring and control. The separated normal paraffins can be efficiently applied to raw material for ethylene production and the separated non-normal paraffins can be efficiently applied to raw material for aromatic hydrocarbons production.

Abstract: A process for the removal of hydrocarbon contaminants, such as dienes and olefins, from an aromatics reformate by contacting an aromatics reformate stream with a hydrotreating catalyst and/or a molecular sieve. The hydrotreating catalyst substantially converts all dienes to oligomers and partially converts olefins to alkylaromatics. The molecular sieve converts the olefins to alkylaromatics. The process provides an olefin depleted product which can be passed through a clay treater to substantially convert the remaining olefins to alkylaromatics. The hydrotreating catalyst has a metal component of nickel, cobalt, chromium, vanadium, molybdenum, tungsten, nickel-molybdenum, cobalt-nickel-molybdenum, nickel-tungsten, cobalt-molybdenum or nickel-tungsten-titanium, with a nickel molybdenum/alumina catalyst being preferred. The molecular sieve is an intermediate pore size zeolite, preferably MCM-22. The clay treatment can be carried out with any clay suitable for treating hydrocarbons.

Abstract: A process is disclosed for improving the yield in the production of high octane gasoline after naphtha reforming by utilizing a transalkylation step to upgrade the heavy and light fractions coming from the reforming step.

Abstract: A process for hydrotreating a hydrocarbon feedstock (1) involving the use of at least one hydrotreatment, particularly hydrodesulfurization, reactor (2) and a fractionation unit (3), which latter contains two distinct injection zones (4, 5) for the hydrocarbon feedstocks, a common zone (8) of vaporization of the light fractions and two distinct draw-off lines (6, 7) for the liquid bottoms; the hydrocarbon feedstock (1) being subjected to a preliminary treatment either in a first hydrodesulfurization reactor (20) the operating conditions of which (P, T, LHSV) may be different from those of the hydrotreatment reactor (2), or in a sweetening apparatus or else in a sulfur trap, the hydrocarbon feedstock being then injected into the first injection zone (4) of the fractionation unit (3), the liquid bottoms being removed through the draw-off line (6) of the injection zone (4) and passed into a hydrotreatment reactor (2), the effluents from said reactor (2) being injected into a second injection zone (5) of the

Abstract: In a process for the dehydrocyclization of a dehydrocyclizable hydrocarbon contained in a dehydrocyclization feed stream which comprises contacting said dehydrocyclizable hydrocarbon in a dehydrocyclization zone under dehydrocyclization conditions in the presence of a dehydrocyclization catalyst, the improvement comprises carrying out said dehydrocyclization process in the presence of a metal chloride additive in said dehydrocyclization feed stream, said metal chloride additive being present in an amount sufficient to inhibit deactivation of such dehydrocyclization catalyst.

Abstract: A method for optimizing the yield of aromatics and light olefins in a process for the conversion of cracked gasoline to aromatics and light olefins by separating the cracked gasoline into a light fraction and a heavy fraction and contacting the light fraction with a zeolite catalyst.

Abstract: Process for the removal of contaminant compounds containing one or more heteroatoms of sulfur, nitrogen and/or oxygen from hydrocarbon streams characterized in that it comprises:an adsorption step in which said compounds are adsorbed by means of an adsorber essentially consisting of silica gel, possibly modified with one or more metals selected from the elements of groups IVb, Vb, VIb, VIII, Ib, IIb or from tin, lead or bismuth, carried out at a temperature of between 0.degree. and 150.degree. C. and at a pressure of between 1 and 20 atm;an optional washing step with polar solvents or hydrocarbons;and a regeneration step for removing the substances adsorbed by means of thermal treatment in a flow of inert gas carried out at a temperature of between 100.degree. and 200.degree. C.

Abstract: A process for desulfurizing and enhancing the octane of cracked gasoline by first aromatizing the cracked gasoline and, second, hydrodesulfurizing the resulting intermediate product stream.

Abstract: A full boiling hydrocarbon feed is reformed to enhance para-xylene and benzene yields. First, the hydrocarbon feed is separated into a C.sub.5- cut, a C.sub.6 -C.sub.7 cut, and a C.sub.8+ cut. The C.sub.6 -C.sub.7 cut has less than 5 lv. % of C.sub.8+ hydrocarbon, and the C.sub.8+ cut has less than 10 lv. % of C.sub.7- hydrocarbon. The C.sub.6 -C.sub.7 cut is subjected to catalytic aromatization at elevated temperatures in a first reformer in the presence of hydrogen and using a non-acidic catalyst comprising at least one Group VIII metal and a non-acidic zeolite support to produce a first reformate stream; and the C.sub.8+ cut is subjected to catalytic aromatization at elevated temperatures in a second reformer in the presence of hydrogen and using an acidic catalyst comprising at least one Group VIII metal and a metallic oxide support to produce a second reformate stream. Less than 20 wt. % of the total amount of C.sub.

Abstract: The rate of coke formation during the aromatization of gasoline boiling range hydrocarbons in which the hydrocarbons are contacted with a zeolite catalyst is significantly reduced by providing a concentration of a silyating agent in the hydrocarbon feed.

Abstract: The feedstock to an aromatization process is processed by a selective adsorption step to remove hydrocarbon species, particularly indan, which have a severe adverse effect on aromatization catalyst stability. The feedstock preferably is a paraffinic raffinate from aromatics extraction. The intermediate from the adsorption step is particularly suitable for the selective conversion of paraffins to aromatics using a high-activity dehydrocyclization catalyst with high aromatics yields and long catalyst life.

Abstract: Disclosed is a method for producing aromatic hydrocarbons, which comprises contacting a light hydrocarbon feedstock comprising olefins and/or paraffins with a zeolite catalyst in a fixed-bed, adiabatic reactor containing a fixed catalyst bed comprised of the zeolite catalyst, to thereby effect a catalytic cyclization reaction of the light hydrocarbon feedstock, wherein the catalytic cyclization reaction is performed under conditions which satisfy the following requirements: (1) the zeolite catalyst has an initial stage-catalytic activity of 0.2 (sec.sup.-1) or more in terms of the initial stage, first-order reaction rate constant of the decomposition of n-hexane catalyzed by the zeolite catalyst; (2) the catalyst bed has a temperature of from 450.degree. C. to 650.degree. C.

Abstract: In the present invention, dimethylbutanes are removed from the raffinate component of the feed to a dehydrocyclization process. Thus, according to a preferred embodiment, a process is provided for producing aromatics by the following steps:(a) contacting fresh paraffins rich feed hydrocarbons, containing 0.1 to 20.0 wt. % dimethylbutanes with a highly selective dehydrocyclization catalyst in a reaction zone, under dehydrocyclization reaction conditions, to convert paraffins to aromatics and obtain an aromatics rich effluent;(b) separating aromatics from the effluent to obtain an aromatics lean raffinate;(c) removing dimethyl butanes from the raffinate to obtain a raffinate of reduced dimethylbutane content; and(d) recycling the raffinate of reduced dimethylbutane content to the reaction zone.Preferably, the dehydrocyclization catalyst used is a nonacidic, monofunctional catalyst. Platinum on L zeolite is a particularly preferred highly selective dehydrocyclization catalyst for use in the process.

Abstract: The rate of coke formation during the aromatization of gasoline boiling range hydrocarbons in which the hydrocarbons are contacted with a zeolite catalyst is significantly reduced by providing a concentration of a silylating agent in the hydrocarbon feed.

Abstract: An integrated three-column process for recovering hydrocarbon distillate products from a hydroprocessing or hydrocracking reactor effluent stream and a hydrocarbon distillate product recovery train are disclosed. According to the present recovery process, an effluent stream from the cracking reactor is cooled and separated into light and heavy phase streams. The heavy phase stream is depressurized and stripped of light end components in a steam stripping column. The light phase stream is further cooled to separate a liquid stream which is combined with the light ends from the stripper and fed to a debutanizer. A C.sub.4 -rich light end stream taken overhead from the debutanizer is condensed to produce LPG product stream(s). A C.sub.4 -lean heavy end stream removed from the bottoms of the debutanizer is combined with a heavy end bottoms stream from the stripper and fed to a fractionator for fractionation into product distillate streams such as light and heavy naphtha, jet fuel, diesel oil, and the like.

Abstract: This invention relates to a process for convening C.sub.5 /C.sub.6 hydrocarbons to aromatic products, e.g., benzene, toluene, etc. The process involves first flowing the C.sub.5 /C.sub.6 feedstream to a first reaction zone where the C.sub.5 /C.sub.6 feed is convened to aromatics and C.sub.3 /C.sub.4 products which are then flowed to a second reaction zone where the C.sub.3 --C.sub.4 compounds are convened to aromatic compound along with formation of hydrogen and fuel gas products. The product stream from the second reaction zone is combined with the products from the first conversion zone and the entire stream separated into the desired components.

Abstract: A process is disclosed for the conversion of light aliphatic hydrocarbons such as propane into aromatic hydrocarbons and especially high purity benzene. The feed hydrocarbon is converted to aromatic hydrocarbons in a dehydrocyclodimerization zone. The product stream from the dehydrocyclodimerization zone which contains benzene, toluene, xylenes and C.sub.6 -C.sub.10 non-aromatics are separated into an overhead stream which contains the non-aromatic hydrocarbons and a small fraction of the benzene and a bottoms stream which contains the remainder of the benzene and other aromatic components. The overhead stream is then flowed to a conversion zone where the C.sub.6 -C.sub.7 non-aromatic hydrocarbons are cracked and the benzene is combined with the bottoms stream and further separated to give a high purity benzene product stream and a toluene, xylenes and C.sub.9 + product stream. The toluene, xylenes and C.sub.9 + product stream may further be separated into a toluene and xylenes product and a C.sub.

Abstract: An improved aromatization apparatus is disclosed in which conversion is increased by recycling a highly purified C.sub.2 -C.sub.4 aliphatic stream. Loss of valuable ethane to fuel gas is substantially eliminated. In a preferred embodiment, a dephlegmator purifies the C.sub.2 -C.sub.4 recycle stream.

Abstract: An integrated process for the conversion of methanol feed to gasoline and distillate range liquid hydrocarbons comprising the steps of splitting the methanol feed into two portions, contacting the first portion of the methanol feed with a medium-pore shape selective zeolite catalyst in a first reaction zone at elevated temperature and moderate pressure to convert the first portion of the methanol feed to hydrocarbons comprising C.sub.2 + olefins; cooling and separating effluent from the first reaction zone to recover a C.sub.3 + olefin hydrocarbon stream and a C.sub.2 - light gas stream; pressurizing the C.sub.3 + olefin hydrocarbon stream and the second portion of the methanol feed and contacting the C.sub.3 + hydrocarbon stream and the methanol feed in a second reaction zone with a medium-pore shape selective oligomerization zeolite catalyst at substantially increased pressure and moderate temperature to convert at least a portion of the C.sub.

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: An improved aromatization process is disclosed in which conversion is increased by recycling a highly purified C.sub.2 -C.sub.4 aliphatic stream. Loss of valuable ethane to fuel gas is substantially eliminated. In a preferred embodiment, a dephlegmator purifies the C.sub.2 -C.sub.4 recycle stream.

Abstract: Aliphatic oxygenates are converted to high octane gasoline by an integrated reactor system wherein three reaction zones are utilized. In a first reaction zone the oxygenates are directly converted to gasoline and an isobutane by-product. In a second reaction zone oxygenates are dehydrated to an intermediate product comprising C.sub.3 -C.sub.4 olefins, which are then further reacted with the isobutane by-product in a third reaction zone to yield a gasoline alkylate. Ethylene-containing vapors may be separated from the second reaction zone and recycled to the first reaction zone for further processing.

Abstract: An integrated reforming/aromatization process is disclosed which improves the octane number and C.sub.5 + liquid yield of a catalytic reforming unit by integrating a catalytic aromatization zone into a catalytic reforming unit gas plant fractionator overhead condenser reflux circuit. The fractionator may be operated as a debutanizer to maximize C.sub.5+ gasoline product volume or a depentanizer to maximize C.sub.5+ gasoline product octane number.

Abstract: An improved fluid-bed reaction process and apparatus are disclosed in which feedstock is preheated and may be at least partially converted by contacting the feedstock with spent catalyst in a preheat zone. Additional benefits include a reduction in catalyst poisons and coke production in the reaction zone. By contacting the fresh feed with hot spent catalyst, at least a portion of the coke which would otherwise form in the reactor is deposited on the spent catalyst. Temporary catalyst poisons are also sorbed onto the spent catalyst. The spent catalyst is then withdrawn from the preheat zone, stripped of entrained hydrocarbon and regenerated.

Abstract: A heat balanced system for converting an olefinic feedstock comprising ethylene and C.sub.3.sup.+ olefins to heavier liquid hydrocarbon product in a catalytic exothermic process. Means are provided for prefractionating the olefinic feedstock to obtain a gaseous stream rich in ethylene and a liquid stream containing C.sub.3.sup.+ olefin, and a reactor for contacting an olefinic feedstock stream from the prefractionating step with ZSM-5 type oligomerization catalyst in a series of exothermic catalytic reactors to provide a heavier hydrocarbon effluent stream comprising distillate, gasoline and lighter hydrocarbons. In a preferred embodiment a catalytic system is provided for making gasoline or diesel fuel from an olefinic feedstock containing ethylene and C.sub.3.sup.+ lower olefins comprising a prefractionation system for separating and recovering ethylene and a liquid stream rich in C.sub.3.sup.

Abstract: A hydrocarbon conversion process is disclosed which extends the useful life of a regenerable zeolite-containing hydrocarbon conversion catalyst. In one aspect of this process, a hydrocarbon feed containing fluorides is passed through a fluoride removal system which reduces the fluoride concentration of the feed to below 100 ppb. The hydrocarbon feed containing less than 100 ppb fluorine is then converted over a regenerable zeolite-containing hydrocarbon conversion catalyst. The zeolite-containing hydrocarbon conversion catalyst is regenerated with an oxygen-containing gas stream as necessary to burn off carbonaceous deposits on the catalyst so as to return the zeolite catalyst to a high level of activity.

Abstract: Disclosed is a method and apparatus for producing gasoline and distillate grade products which employs integrating catalytic (or thermal) dehydrogenation of paraffins with MOGD to minimize interstage compression and gas plant separation cost. The process cascades the product from a low temperature propane or butane dehydrogenation zone into a first catalytic reactor zone which operates at low pressure and contains zeolite oligomerization catalysts, where the low molecular weight olefins are reacted to primarily gasoline range materials. These gasoline range materials can then be pressurized to the pressure required for reacting to distillate in a second catalytic reactor zone operating at high pressure and containing zeolite oligomerization catalyst. The first catalytic reactor zone also acts to remove the olefins from the dehydrogenation reactor effluent to allow recycle of the unreacted paraffins.

Abstract: Disclosed is a method and apparatus for conversion of LPG hydrocarbons into distillate fuels by integrating LPG dehydrogenation with catalytic oligomerization and recovering the distillates produced. The described method and apparatus may comprise an H.sub.2 separation zone, wherein a lean oil stream contacts a dehydrogenation effluent stream to produce a C.sub.3.sup.+ rich liquid stream to feed oligomerization. An energy efficient separation zone comprising dual debutanizers is disclosed. In addition, a method and apparatus is disclosed for a fluid bed dehydrogenation reactor zone using an FCC catalyst contaminated with a metal, such as nickel and/or vanadium.

Abstract: Aliphatic oxygenates are converted to high octane gasoline by an integrated process wherein three reaction zones are utilized. In a first reaction zone the oxygenates are directly converted to gasoline and an isobutane by-product. In a second reaction zone oxygenates are dehydrated to an intermediate product comprising C.sub.3 -C.sub.4 olefins, which are then further reacted with the isobutane by-product in a third reaction zone to yield a gasoline alkylate. Ethylene-containing vapors may be separated from the second reaction zone and recycled to the first reaction zone for further processing.

Abstract: A hydrocarbon conversion process for the production of C.sub.6 -C.sub.8 aromatic hydrocarbons from C.sub.3 and C.sub.4 aliphatic hydrocarbons is disclosed. This dehydrocyclodimerization process is characterized by the integrated product recovery steps employed to separate hydrogen and products from the reactor effluent. Following partial condensation of the reactor effluent stream, the resultant vapor is subjected to liquid absorption (scrubbing) followed by autorefrigeration to yield lighter gas streams. Liquids from the various steps are separated via fractionation.

Abstract: A multistage technique for converting olefins to heavier hydrocarbons including a sorption prefractionation unit for separating olefinic feedstock into a sorbate stream rich in liquified olefins and a vapor stream rich in light olefins; a first stage catalytic reactor unit for oligomerizing olefins from the sorbate stream including means for maintaining the first stage at elevated pressure and predetermined temperature for producing substantially linear aliphatic hydrocarbons; a second stage catalytic reactor unit for oligomerizing light olefin including means for maintaining the second stage under high severity conditions at substantially higher temperature than the first stage; and a product fractionation unit for separating effluent from the first and second stages to separate and recover heavy hydrocarbon product and a sorbent recycle fraction. The sorbent fraction is recycled to the sorption prefractionation unit for contacting olefinic feedstock with the recycled sorbent.

Abstract: An improved continuous process for converting lower olefinic hydrocarbon feedstock to C.sub.5.sup.+ liquid hydrocarbons by contacting vapor phase olefinic feedstream with acid zeolite catalyst in the presence of recycled diluent stream rich in C.sub.3 -C.sub.4 hydrocarbons in an enclosed reactor at elevated temperature and pressure. The improved technique comprises a system for cooling reactor effluent to recover a heavier hydrocarbon stream containing a mixture of C.sub.3 -C.sub.4 hydrocarbons and C.sub.5.sup.+ hydrocarbons and debutanizing the heavier hydrocarbons below reactor pressure to obtain a C.sub.5.sup.+ product stream and a condensed C.sub.3 -C.sub.4 hydrocarbon stream. Operating efficiencies are realized in the heat exchange system by reboiling the debutanized C.sub.5.sup.+ hydrocarbon product stream with hot reactor effluent, and by recycling and combining at least a portion of the condensed C.sub.3 -C.sub.4 hydrocarbon stream to dilute liquid olefin hydrocarbon feedstock.

Abstract: A heat balanced technique for converting an olefinic feedstock comprising ethylene and C.sub.3.sup.+ olefins to heavier liquid hydrocarbon product in a catalytic exothermic process. Methods and means are provided for prefractionating the olefinic feedstock to obtain a gaseous stream rich in ethylene and a liquid stream containing C.sub.3.sup.+ olefin, and contacting an olefinic feedstock stream from the prefractionating step with ZSM-5 type oligomerization catalyst in a series of exothermic catalytic reactors to provide a heavier hydrocarbon effluent stream comprising distillate, gasoline and lighter hydrocarbons. In a preferred embodiment a catalytic system is provided for making gasoline or diesel fuel from an olefinic feestock containing ethylene and C.sub.3.sup.+ lower olefins comprising a prefractionation system for separating and recovering ethylene and a liquid stream rich in C.sub.3.sup.

Abstract: A hydrocarbon feed for use in a catalytic conversion process that utilizes a zeolite catalyst, and that contains a catalytically deleterious impurity, is refined by contact with a zeolitic sorbent. The invention is applicable to dewaxing, with an example illustrating reduction by 100.degree. F. of the initial equilibrium (lineout) temperature by the method of this invention. Other reactions include conversions of aromatic hydrocarbons such as alkylation, isomerization and disproportionation.

Abstract: A process for the dimerization and cyclization of isobutene to form, as preferred product, paraxylene in which the whole of the product of isobutene dimerization (including unreacted feedstock) is contacted with a catalyst for the cyclization of the isobutene dimer. The process is operable in a single dimerization/cyclization stage or in separate dimerization and cyclization stages with no intermediate separation of products. Optionally, the isobutene feedstock is provided by dehydrogenation of isobutane, unreacted isobutane in the resulting feedstock being carried through the dimerization/cyclization and eventually recycled.

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.

Abstract: A continuous process for the selective production of ethylene by the diacritic cracking of heavy hydrocarbon feeds such as residual oils, heavy vacuum gas oils, atmospheric gas oils, crude oils and coal-derived liquids. The diacritic cracking takes place in a non-tubular multi-zone reactor at elevated pressures (e.g. 70-1000 p.s.i.a.) A fuel is combusted with oxygen in the first section of the multi-zone reactor. The high temperature products of combustion of the first zone pass into a second section of the reactor where the feed is atomized and cracked to yield products including ethylene, acetylene and synthesis gas. The reaction products of the second zone then pass into a third section in which they are quenched. In each stage of the reactor the present process seeks to prevent the build-up of coke deposits on the walls of the reactor. In the first two stages, a film of gas such as CO.sub.2 or N.sub.2 is injected along the inner walls to prevent build-up of coke.