Abstract: A method for converting heavy olefins present in a product stream exiting a first reaction zone into light olefins and carbonaceous deposits on a catalyst without separation of the heavy olefins from the product stream exiting the first reaction zone. The method comprises creating the product stream exiting the first reaction zone, the product stream exiting the first reaction zone comprising the heavy olefins, moving the product stream exiting the first reaction zone to a second reaction zone without separation of the heavy olefins from the product stream exiting the first reaction zone, and contacting the product stream exiting the first reaction zone with the catalyst under conditions effective to form the light olefins, the contacting causing the carbonaceous deposits to form on at least a portion of the catalyst.

Abstract: A process for producing alkyl aromatics using a transalkylation reaction zone and an alkylation reaction zone is disclosed. One portion of the transalkylation reaction zone effluent passes to an alkylation reaction zone where an aromatic substrate is alkylated to the desired alkyl aromatic. At least a portion of the alkylation reaction zone effluent and another portion of the transalkylation reaction zone effluent pass to a product recovery zone. This process decreases the capital and operating costs of recycling aromatic substrate to the transalkylation and/or alkylation reaction zone while maintaining operational flexibility. This process is well suited for solid transalkylation and alkylation catalysts. Ethylbenzene and cumene may be produced by this process.

Abstract: A process is set forth for reacting impure toluene to obtain benzene, toluene and a para-rich xylene stream, which are substantially free of close-boiling non-aromatics. The impure toluene comprises at least 70 wt % toluene and between about 0.2 wt % and about 5 wt % close-boiling non-aromatics. The process may also comprise aromatizing a naphtha over a non-acidic catalyst. The impure toluene from the aromatization step is passed over an acidic intermediate pore zeolite to produce a para-rich xylene stream and chemically pure benzene.

Abstract: The present invention relates to a process for the production of light olefins comprising olefins having from 2 to 4 carbon atoms per molecule from an oxygenate feedstock. The process comprises passing the oxygenate feedstock to an oxygenate conversion zone containing a metal aluminophosphate catalyst to produce a light olefin stream. A propylene stream and/or mixed butylene is fractionated from said light olefin stream and cracked to enhance the yield of ethylene and propylene products. This combination of light olefin product and propylene and butylene cracking in a riser cracking zone or a separate cracking zone provides flexibility to the process which overcomes the equilibrium limitations of the aluminophosphate catalyst. In addition, the invention provides the advantage of extended catalyst life and greater catalyst stability in the oxygenate conversion zone.

Abstract: Disclosed are various embodiments for alkylating olefins and isoparaffins in the presence of an acid to reduce and/or control acid consumption or maximize and/or control the octane number of the produced alkylate product. One embodiment includes alkylation by controlling the C3/iso-C5 olefin ratio to reduce acid consumption. Another embodiment includes alkylation of C3 and C5 olefins in separate alkylation zones to maximize alkylate octane number. Even another embodiment includes propylene alkylation followed by C4 and/or C5 olefin alkylation, with the spent propylene acid used in the C4 and/or C5 olefin alkylation. Still another embodiment includes alkylation of C3, C4 and C5 olefins in separate alkylation zones, with the spent propylene acid used in the C4 alkylation, and the spent butylene acid used in the C5 alkylation. Yet another embodiment includes alkylation by controlling the C3/C4 olefin ratio to maximize the octane number of the produced alkylate.

Abstract: The preparation of olefins from steam cracker or refinery C.sub.4 streams is carried out by selective hydrogenation of butadienes and acetylenic impurities in the steam cracker or refinery C.sub.4 stream, with simultaneous or subsequent, at least partial isomerization of 1-butene to 2-butene, followed by removal of i-butene from the C.sub.4 stream by reaction with an alcohol to form an ether, followed by removal of oxygen-containing impurities from the C.sub.4 stream using adsorber materials, followed by two-stage metathesis of the butenes in the C.sub.4 stream by conversion of 1-butene and 2-butene present in the C.sub.4 stream into propene and 2-pentene and subsequent reaction of the 2-pentene with ethene in the presence of a metathesis catalyst to form propene and 1-butene. Optionally, butadiene may be removed from the C.sub.4 stream by extractive distillation in a preliminary step.

Abstract: A process for producing 2,6-dialkylnaphthalene from a hydrocarbon feedstock that contains at least one component selected from the group consisting of dialkylnaphthalene isomers, monoalkylnaphthalene isomers, polyalkylnaphthalenes, and naphthalene, is provided that includes the following steps:I. separating the hydrocarbon feedstock and/or a dealkylation product fed from step III into a naphthalene fraction, a monoalkylnaphthalene fraction, a dialkylnaphthalene fraction and a remaining products fraction;II. separating and purifying 2,6-dialkylnaphthalene from the dialkylnaphthalene fraction of step I;III. dealkylating the hydrocarbon feedstock and/or the remaining products fraction of step I and feeding the dealkylation product to step I; andIV. alkylating the naphthalene and monoalkylnaphthalene fractions of step I;wherein the hydrocarbon feedstock is fed to step I or step III.

Abstract: A process for producing alkyl aromatics using a transalkylation reaction zone and an alkylation reaction zone is disclosed. The transalkylation reaction zone effluent passes to the alkylation reaction zone where aromatics in the transalkylation reaction zone effluent are alkylated to the desired alkyl aromatics. This process decreases the capital and operating costs of recycling the aromatics in the transalkylation reaction zone effluent. This process is well suited for solid transalkylation and alkylation catalysts. Ethylbenzene and cumene may be produced by this process.

Abstract: A separation arrangement for a cumene process that operates with a relatively wet feed to an alkylation zone and relatively dry feed to a transalkylation zone reduces utilities and capital expenses for the separation and recycle of distinct wet and dry components by using an arrangement that first separates effluent from the trans alkylation and alkylation reaction zone in a benzene column before performing light ends and drying in a downstream depropanizer column. The arrangement uses a portion of the net overhead stream from the benzene column as a wet recycle stream for return to the alkylation reaction zone and sends another portion of the benzene net overhead to the depropanizer to supply a dry benzene recycle for the trans alkylation reaction zone.

Abstract: The present invention relates to a process for the production of light olefins comprising olefins having from 2 to 4 carbon atoms per molecule from an oxygenate feedstock. The process comprises passing the oxygenate feedstock to an oxygenate conversion zone containing a metal aluminophosphate catalyst to produce a light olefin stream. A propylene stream and/or mixed butylene is fractionated from said light olefin stream and cracked to enhance the yield of ethylene and propylene products. This combination of light olefin product and propylene and butylene cracking in a riser cracking zone or a separate cracking zone provides flexibility to the process which overcomes the equilibrium limitations of the aluminophosphate catalyst. In addition, the invention provides the advantage of extended catalyst life and greater catalyst stability in the oxygenate conversion zone.

Abstract: A process for the production of alkylaromatic hydrocarbons that operates with a high water content in an alkylation zone and a low water content in a transalkylation zone is disclosed. An aromatic feed and an acyclic feed are first passed through the alkylation reaction zone that operates at a high water content. A stripping column receives the effluent of the alkylation reaction zone, removes water and unreacted aromatic feed and produces a bottom stream containing unreacted aromatic feed and alkylated aromatics. A recycle column receives the bottom stream and produces an overhead stream of unreacted aromatic feed having a low water content. The overhead stream and a stream of polyalkylated aromatics are contacted in the transalkylation zone.

Abstract: Disclosed are various embodiments for alkylating olefins and isoparaffins in the presence of an acid to reduce and/or control acid consumption or maximize and/or control the octane number of the produced alkylate product. One embodiment includes alkylation by controlling the C.sub.3 /C.sub.5 olefin ratio to reduce acid consumption. Another embodiment includes alkylation of C.sub.3 and C.sub.5 olefins in separate alkylation zones to maximize alkylate octane number. Even another embodiment includes propylene alkylation followed by C.sub.4 and/or C.sub.5 olefin alkylation, with the spent propylene acid used in the C.sub.4 and/or C.sub.5 olefin alkylation. Still another embodiment includes alkylation of C.sub.3, C.sub.4 and C.sub.5 olefins in separate alkylation zones, with the spent propylene acid used in the C.sub.4 alkylation, and the spent butylene acid used in the C.sub.5 alkylation. Yet another embodiment includes alkylation by controlling the C.sub.3 /C.sub.

Abstract: The following steps are conducted for producing a hydrocarbon having a carbon number of at least 2: a coupling step, in which a coupling feed gas containing methane and a gas containing oxygen are supplied to a conveying catalyst bed which is formed by an ascending stream which contains a catalyst, and then methane and oxygen are allowed to react so as to produce a coupling product gas; a catalyst separation step for separating the catalyst from the coupling product gas; and a catalyst feedback step for feeding back the thus-separated catalyst to the coupling step. Accordingly, the reaction system does not accumulate excessive heat, the combustion reaction as a side reaction is hindered, and the selectivity of the coupling reaction is enhanced. In addition, the yield of the hydrocarbon having a carbon number of at least 2 is improved.

Abstract: A process for producing alkylnaphthalene from a feedstock comprising isomers of dialkylnaphthalene and naphthalene by contacting the feedstock with a catalyst composition, in which the process comprising transalkylation between isomers of dialkylnaphthalene and naphthalene to produce monoalkylnaphthalene, and isomerization of dialkylnaphthalene, wherein the catalyst composition comprising a synthetic zeolite characterized by an X-ray diffraction pattern including interplanar d-spacing as set forth in Table A of the specification.

Abstract: A process for the conversion of a halogenated organic stream containing trace quantities of organic nitrates to produce a stream comprising hydrogenated hydrocarbonaceous compounds free from organic nitrates and halogenated organic compounds by means of contacting the feed stream and hydrogen with a selective hydrogenation catalyst in a first hydrogenation zone at hydrogenation conditions to convert the organic nitrates into water-soluble nitrogen compounds while effectively minimizing the production of hydrogen halide compounds. The resulting effluent from the first hydrogenation zone is contacted with an aqueous scrubbing solution to recover at least a portion of the water-soluble nitrogen compounds in order to produce a stream containing halogenated organic compounds and essentially free of nitrogen compounds which is then introduced into a second hydrogenation zone operated at selected hydrogenation conditions to produce water-soluble hydrogen halide compounds and hydrogenated hydrocarbonaceous compounds.

Abstract: A synthetic oil is made by a process comprising the steps of (a) reacting a vinylidene olefin in the presence of a catalyst to form an intermediate mixture which contains at least about 50 weight percent dimer of said vinylidene olefin, and (b) adding a vinyl olefin to said intermediate mixture and reacting said intermediate mixture and said vinyl olefin in the presence of a catalyst so as to form a product mixture which contains said dimer of said vinylidene olefin and a codimer of said added vinyl olefin with said vinylidene olefin.

Abstract: Aliphatic feeds are converted to olefins and/or aromatics in a multi pressure reactor system. A high pressure first stage reactor generates much or all of the hydrogen needed to reduce catalyst coking in lower pressure downstream reactors. High pressure operation protects catalyst stability in the first reactor, while produced hydrogen helps protect downstream catalyst. Low pressure downstream operation improves yields.

Abstract: This invention provides a process for upgrading hydrocarbon feedstock comprising the steps of:(i) recovering a C.sub.4 -rich aliphatic stream from a catalytic cracking process;(ii contacting said C.sub.4 -rich aliphatic stream with an isomerization catalyst comprising a zeolite sorbing 30 to 55 mg n-hexane at 90.degree. C., 83 torr, and 15 to 40 mg 3-methylpentane at 90.degree. C., 90 torr, per g dry zeolite in the hydrogen form in a first reaction stage to selectively isomerize C.sub.4 n-olefins to C.sub.4 isoolefins; and(iii) contacting the product stream from said first reaction stage with a solid acid alkylation catalyst selected from the group consisting of MCM-36 and MCM-49, as described herein and zeolites having a Constraint Index of less than or equal to about 2, to produce isoparaffinic alkylate gasoline.

Abstract: Disclosed is a method which combines catalytic cracking and olefin production using a coked catalytic cracking catalyst as a dehydrogenation catalyst to dehydrogenate an alkane feed stream and form an olefin rich product stream. The method uses a staged backmixed regeneration system to form the dehydrogenation catalyst and to fully reactivate deactivated cracking catalyst for reuse in the cracking reaction. The catalyst preferably comprises a crystalline tetrahedral framework oxide component.

Abstract: A process for upgrading low octane naphthas to produce gasoline products with low levels of benzene and aromatics while retaining a high pool octane uses a paraffinic naphtha reformer feed which is dehexanized to provide a C.sub.7 + fraction which is fed to the reformer and a C.sub.6 fraction which is fed together with the C.sub.6 fraction from the reformer effluent to a catalytic upgrading step where the low octane components from the naphtha and the benzene from the reformate are converted to a low benzene, high octane gasoline by alkylation of the benzene and other aromatics present in the reformate. The process has the advantage that benzene make in the reformer is reduced by the partial by-passing of the C.sub.6 benzene precursors around the reformer; in addition, improved benzene alkylation results from the presence of additional light olefins generated by the cracking of paraffins from the paraffinic naphtha. the reaction is preferably carried out in a turbulent fluidized bed reaction zone.

Abstract: An alkane-containing feedstream is passed through one or more tubes, which may contain alkane-dehydrogenation catalyst, immersed in a bed of fluidized particles. The bed is at an elevated temperature which maintains the temperature within the tube(s) at an alkane-dehydrogenation temperature. The particles may be inert, chemically active and/or catalytically active. In one embodiment, cracking catalyst particles are circulated between a reaction zone wherein they contact a cracker feedstock which is converted to cracked hydrocarbon products and a regenerator (22) wherein carbonaceous deposits on the catalyst particles are exothermically removed by contact with an oxygen-containing gas (24). Hot regenerated particles from the regenerator (22) are recirculated (27) to the reaction zone for re-use therein.

Abstract: This invention is a process of converting n-pentane to cyclopentane. In accordance with a preferred embodiment of the invention, n-pentane feed is converted in dual temperature stage process without interstage processing of the first stage product mixture.

Abstract: An ethylene oligomerization process comprising: (a) contacting, in a reaction solution, an organonickel compound and a phosphine compound to form a first reaction mixture; and thereafter (b) contacting said first reaction mixture with ethylene to form a second reaction mixture; and concurrently with step (b) or thereafter, contacting said second reaction mixture with a fluorinated organoacid; while maintaining a reaction temperature from about 0.degree. C. to about 200.degree. C., and a reaction pressure of about 1 to about 10,000 psig.

Abstract: An improvement in iso-olefin etherification is obtained in an integrated process combining a fluidized catalytic cracking reaction and a fluidized catalyst etherification reaction wherein zeolite catalyst particles are withdrawn in partially deactivated form from the ether reaction stage and added as part of the catalyst in the FCC reaction.

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: An integrated process comprising the steps of pressurizing a C.sub.3.sup.+ olefin hydrocarbon stream and a methanol feed and contacting the C.sub.3.sup.+ hydrocarbon stream and methanol feed in a first reaction zone with a medium-pore shape selective oligomerization zeolite catalyst at elevated pressure and moderate temperature to convert at least a portion of the C.sub.3.sup.+ hydrocarbons and methanol feed to heavier liquid hydrocarbon product stream comprising olefinic gasoline and distillate range liquids. An ethene stream and a stream containing unreacted methanol and water are recovered from the first reaction zone effluent and the methanol is separated from the water.The ethene and the separated unreacted methanol are contacted with a medium-pore shape selective zeolite catalyst in a second reaction zone at elevated temperature and moderate pressure to convert the methanol feed to hydrocarbons comprising C.sub.3.sup.+ olefins and cooling effluent from the second reaction zone to recover a C.sub.3.sup.

Abstract: A reactor system for increased production of olefinic gasoline incorporating the integration of olefins to gasoline conversion under moderate severity conditions in contact with medium pore catalyst with oxygenates to olefin conversion. The effluent product of the olefins to olefin conversion is passed to an olefins to gasoline and/or distillate (MOGD) conversion zone for olefin upgrading. Liquid recycle requirements, feed throughput and/or the number of MOGD fixed bed stages are reduced for the MOGD process and overall process costs are lowered. The process includes the use of common catalyst handling and regeneration steps for the integrated processes.

Abstract: Compositions and methods of preparation for a lubricant mixture having enhanced viscosity index comprising:(a) a low viscosity C.sub.20 -C.sub.60 lubricant range liquid comprising substantially linear hydrocarbons prepared by shape selective catalysis of lower olefin with medium pore acid zeolite catalyst to provide substantially linear liquid olefinic intermediates or C.sub.20.sup.+ hydrogenated lubricants, said lubricant range liquid having a kinematic viscosity of about 2-10 cS at 100.degree. C.; and(b) at least one poly(alpha-olefin) having viscosity greater than 20 cS and viscosity index improvement properties.

Abstract: A process is disclosed for converting a feedstock containing ethylene to produce heavier hydrocarbons in the gasoline or distillate boiling range including the steps of contacting the olefins feedstock with a first siliceous crystalline molecular sieve at an elevated temperature and relatively low pressure under conditions which maximize the conversion of ethylene to C.sub.3 -C.sub.4 olefins and C.sub.5 + hydrocarbons, separating C.sub.3 -C.sub.4 olefins from the C.sub.5 + hydrocarbons, and contacting the separated C.sub.3 -C.sub.4 olefins with a second siliceous crystalline molecular sieve at moderate temperatures under conditions favorable for conversion of the C.sub.3 -C.sub.4 olefins to heavier hydrocarbons in the gasoline or distillate boiling range.

Abstract: A process is provided for upgrading the olefinic gasoline by-product of low-severity medium-pore zeolite catalyzed hydrocarbon conversion processes including catalytic dewaxing and olefin oligomerization. The olefinic gasoline stream is upgraded in a high-severity catalytic conversion process which may be carried out in a catalytic cracking unit primary or secondary riser reactor or in a second medium-pore zeolite-catalyzed reaction zone. The olefinic gasoline stream may be mixed with a C.sub.2 -C.sub.7 aliphatic stream before upgrading the mixture in the high-severity catalytic conversion process. Examples of such low-severity medium-pore zeolite catalyzed hydrocarbon conversion processes include distillate and lubricant dewaxing as well as olefin oligomerization.

Abstract: A process for the increased production of olefinic gasoline is described incorporating the integration of olefins to gasoline conversion under moderate severity conditions in contact with zeolite type catalyst with oxygenates to olefins conversion. The product of the olefins to gasoline conversion is passed to an olefins to gasoline and distillate (MOGD) conversion zone for distillate production. Liquid recycle requirements, feed throughput and/or the number of MOGD fixed bed stages are reduced for the MOGD process and overall process costs are lowered. The process includes the use of common catalyst handling and regeneration steps for the integrated processes.

Abstract: An integrated process is provided for converting methanol, dimethylether or the like to heavy hydrocarbon products, especially distillate range hydrocarbons. In a first stage catalytic process oxygenate feedstock is converted to lower olefins. C.sub.3.sup.+ olefins are selectively sorbed in an interstage sorption fractionator and passed along with gasoline sorbent to a second stage oligomerization reactor. Distillate range hydrocarbons are useful as diesel fuel or the like.

Abstract: A staged reactor technique for converting ethene-rich olefinic feedstock to heavier hydrocarbons, particularly gasoline and distillate range products. By employing low temperature and high temperature separators, an economic recycle is provided for each stage.

Abstract: A two-stage catalytic conversion process for converting an olefins-containing feed is disclosed which comprises contacting the feed in a first stage under substantially non-oligomerizing conditions with a catalyst comprising at least one metal (X) selected from the group consisting of metals from Groups 1a, 1b, 2a, 2b, 4b, 5b, 6b and 8 of the Periodic Table of the Elements and contacting the effluent from the first stage in the second stage under olefin oligomerization conditions at a temperature which is at least 50.degree. C. above the operating temperature of the first stage with a catalyst comprising at least one metal (Z) selected from the group consisting of metals from Groups 1b, 2a, 2b, 4b, 5b, 6b, and 8 on a mordenite-type of crystalline trivalent metal (Q) silicate.

Abstract: An integrated process for the conversion of methanol to high octane gasoline and distillate. Methanol is converted to olefins in the presence of zeolite type catalyst. C.sub.4 and C.sub.5 olefin fraction is converted to MTBE and TAME in the presence of excess methanol and acid etherification catalyst. Unreacted methanol and hydrocarbons are passed to an olefins to gasoline and distillate oligomerization unit in conjunction with C.sub.3, C.sub.6 and C.sub.7 olefins from the methanol to olefins unit whereby distillate and LPG products are produced. Gasoline products from the oligomerization unit are passed to the etherification unit whereby an ether-rich gasoline fraction is separated.

Abstract: An improved two-step process for the conversion of lower molecular weight paraffins, the process comprising contacting in a first step a C.sub.2 -C.sub.10 alkane-rich feedstock with a siliceous zeolite catalyst in a primary fluidized bed reaction zone under high temperature dehydrogenation conditions to obtain an intermediate product comprising oligomerizable olefinic hydrocarbons and aromatics; and then contacting in a second step the intermediate product with a siliceous zeolite catalyst in a secondary fluidized bed reaction zone under low temperature oligomerization conditions to obtain a final product comprising gasoline boiling range aliphatic and aromatic hydrocarbons.

Abstract: A multi-stage catalytic olefin upgrading technique for converting lower olefinic feedstock to heavier liquid hydrocarbon product.

Abstract: This invention relates to a process for producing liquid products e.g. gasoline blending components by conversion of a mixed paraffin/olefin gaseous feedstock over two types of catalysts. In a first stage, the mixed feedstock is brought into contact with a partially deactivated catalyst which converts olefins in the feed into liquid products. Gaseous products now rich in paraffins are separated and brought into contact in a second stage with another catalyst which is more active than that used in the first stage. The liquid products emerging from the second stage are thereafter separated and recovered. The catalyst is preferably a gallium oxide loaded MFI type zeolite.

Abstract: Alkylate is produced by catalytically converting oxygenate feedstock, such as methanol, to lower olefins comprising C.sub.2 -C.sub.4 olefins. Ethene is separated by interstage sorption of C.sub.3 + components and an isoparaffin is alkylated with C.sub.3 -C.sub.4 olefins derived from sorbate. The system comprises means for fractionating an olefinic feedstream containing ethene and C.sub.3 + olefinic components by contacting the olefinic feedstream in a sorption zone with a liquid hydrocarbon sorbent to selectively sorb C.sub.3.sup.+ components; means for reacting C.sub.3.sup.+ olefins with excess isoparaffin in a catalytic alkylation reactor to produce C.sub.7 + alkylate hydrocarbons; fractionating the alkylation reactor effluent to provide a liquid hydrocarbon fraction rich in C.sub.7.sup.+ alkylate. Liquid recycle or C.sub.5.sup.+ liquid coproduced with the lower olefin may be passed to the sorption zone as lean sorbent. C.sub.7.sup.+ alkylate product and C.sub.5.sup.

Abstract: An apparatus for converting oxygenated feedstock, such as methanol, dimethyl ether or the like, to liquid hydrocarbons. In the primary catalyst stage the feedstock is contacted with a fluidized zeolite catalyst to produce C.sub.2 -C.sub.4 olefins and C.sub.5.sup.+ hydrocarbons. In a secondary catalytic stage with oligomerization catalyst comprising medium-pore shape selective acidic zeolite at increased pressure converts C.sub.3.sup.+ olefins to gasoline and/or distillate liquids. A portion of the recovered gasoline stream is recycled to the fluidized bed at a point above the bed stratum corresponding to substantially complete oxygenate conversion.

Abstract: Disclosed is a multistage process for converting lower aliphatic oxygeanated hydrocarbon feedstock to hydrocarbon product rich in benzene, toluene and/or xylene which comprises:contacting said oxygenated hydrocarbons in a primary stage with a medium pore shape selective acidic zeolite to an intermediate hydrocarbon product comprising predominantly aliphatic hydrocarbons;contacting at least a portion of the aliphatic hydrocarbons from the primary stage with a secondary stage catalyst comprising gallium-promoted medium pore shape selective zeolite characterized by a constraint index within the approximate range of 1 to 12 and a silica to alumina ratio of about 20 to 100:1; thereby producing benzene, toluene and/or xylene.

Abstract: This invention relates to a two-stage conversion of olefins into aromatic hydrocarbon mixtures by contacting them in the first stage with a crystalline metal silicate and in the second stage with a crystalline gallium silicate.

Abstract: A process for converting oxygenated feedstock, such as methanol, dimethyl ether or the like, to liquid hydrocarbons.In the primary catalyst stage the feedstock is contacted with zeolite catalyst to produce C.sub.2 -C.sub.4 olefins and C.sub.5.sup.+ hydrocarbons.In a secondary catalytic stage with oligomerization catalyst comprising medium-pore shape selective acidic zeolite at increased pressure converts C.sub.3.sup.+ olefins to gasoline and/or distillate liquids.The improvement is a technique for recovering lower alkene for recycle to the primary catalytic stage.

Abstract: MTBE can be dissociated with high selectivity to isobutene and methanol over acid action exchange resin catalysts using very high LHSV, e.g. of 7 to 35 at pressure drops of 0.5 to 50 psig through the fixed bed at reaction pressure of 0.5 to 4 atmospheres and bed temperatures in a fixed bed tubular-reactor in the range of 90.degree. C. to 160.degree. C. Good conversions are obtained and undissociated MTBE and by-products of the dissociation may be recycled to a liquid phase MTBE synthesis.

Abstract: A process for converting oxygenated feedstock comprising methanol, dimethyl ether or the like to liquid hydrocarbons comprising the steps ofcontacting the feedstock with zeolite catalyst in a primary catalyst stage at elevated temperature and moderate pressure to convert feedstock to hydrocarbons comprising C.sub.2 -C.sub.4 olefins and C.sub.5.sup.+ hydrocarbons;cooling and separating effluent from the primary stage to recover a liquid hydrocarbon stream and a light hydrocarbon vapor stream rich in C.sub.2 -C.sub.4 olefins;compressing the olefinic light hydrocarbon stream to condense a liquid olefinic hydrocarbon stream rich in C.sub.3.sup.

Abstract: The invention relates to a process for the pretreatment of a light olefin fraction, or of a mixture of such fractions, for the purpose of selectively removing the isobutene and butadiene present.In accordance with the invention, the olefin fraction is contacted with boron trifluoride in the gas phase, under such conditions and for such a length of time that the isobutene and the butadiene will polymerize selectively, and the boron trifluoride and the isobutene and butadiene polymers obtained are then conventionally separated from the effluent.

Abstract: An integrated process is provided for converting methanol, dimethylether or the like to heavy hydrocarbon products, especially distillate range hydrocarbons. In a first stage catalytic process oxygenate feedstock is converted to lower olefins. C.sub.3.sup.+ olefins are selectively sorbed in an interstage sorption fractionator and passed along with gasoline sorbent to a second stage oligomerization reactor. Distillate range hydrocarbons are useful as diesel fuel or the like.

Abstract: A process to convert a substantially linear alkene, such as n-butene, to isomerized products comprises contacting such alkene under conversion conditions comprising a temperature of above 300.degree. C. to about 650.degree. C. and an alkene reactant partial pressure of less than about 0.4 atmospheres with an AMS-1B borosilicate catalyst composition containing at least 50 wt. % hydrogen from AMS-1B incorporated in an inert binder.

Abstract: A process to convert an alkene to oligomerized, aromatized and isomerized products comprises contacting such alkene under conversion conditions with an AMS-1B borosilicate catalyst composition.

Abstract: An improved two-step process for the conversion of lower molecular weight paraffins, the process comprising contacting in a first step a C.sub.2 -C.sub.10 alkane-rich feedstock with a siliceous zeolite catalyst in a primary fluidized bed reaction zone under high temperature dehydrogenation conditions to obtain an intermediate product comprising oligomerizble olefinic hydrocarbons and aromatics; and then contacting in a second step the intermediate product with a siliceous zeolite catalyst in a secondary fluidized bed reaction zone under low temperature oligomerization conditions to obtain a final product comprising gasoline boiling range aliphatic and aromatic hydrocarbons.