Abstract: The present invention relates to a continuous or non-continuous ionic liquid alkylation process comprising a step for solids removal, the process further comprising the steps (a) measuring the solids content in the ionic liquid alkylation process stream by on line (in situ) or off line sampling; (b) in response to the solids measurement signal, regulating the flow of the ionic liquid side stream to be sent to the solids removal device; (c) regulating the flow of the fresh ionic liquid inlet stream, for controlling the solids content in the ionic liquid alkylation process to a pre-defined level. The process of the invention provides a means to more efficiently run an ionic liquid alkylation process.

Abstract: Disclosed herein are processes in which precipitation permits removal of metal halides (e.g. AlCl3) from ionic liquids. After precipitation, the precipitated metal halides can be physically separated from the bulk ionic liquid. More effective precipitation can be achieved through cooling or the combination of cooling and the provision of metal halide seed crystals. The ionic liquids can be regenerated ionic liquid catalysts, which contain excess metal halides after regeneration. Upon removal of the excess metal halides, they can be reused in processes using ionic liquid catalysts, such as alkylation processes.

Abstract: The present invention relates to a process for nonoxidatively dehydroaromatizing a reactant stream comprising C1-C4-aliphatics, comprising the steps of I. feeding reactant stream E into a reaction zone 1, converting reactant stream E under nonoxidative conditions in the presence of a particulate catalyst to a product stream P comprising aromatic hydrocarbons and discharging product stream P from reaction zone 1, II. transferring the catalyst with reduced activity as a result of deposited coke into a reaction zone 2, III. at least partly regenerating the catalyst with supply of a hydrogen-comprising gas stream H in a reaction zone 2, at least some of the coke deposited being converted to methane to form a methane-comprising gas stream M which is fed at least partly to reaction zone 1, IV. discharging the catalyst from reaction zone 2 and V.

Abstract: A process is disclosed for the conversion of a hydrocarbonaceous assets into gasoline. The hydrocarbonaceous assets are converted at a first methanol production facility into methanol by processes comprising gasification and methanol synthesis. At least a portion of the methanol is shipped to a second gasoline production facility that is at least 10 miles in distance from the first location. At the second gasoline production facility, at least a portion of the methanol is converted by a MTG process to produce a gasoline and LPG components and steam. At least a portion of the methanol may also be used in a methanol to olefin process to produce olefins and steam. The olefins may be alkylated with olefins to produce alkylates which may mixed with the gasoline.

Abstract: A system and/or process for decreasing the level of at least one organic fluoride present in a hydrocarbon phase contained in an alkylation settler by contacting the hydrocarbon phase with an HF containing stream, containing greater than about 80 wt. % and less than about 94 wt. % HF, in the intermediate portion of the settler which contains at least one tray system, with each tray system comprising a perforated tray defining a plurality of perforations and a layer of packing below the perforated tray, are disclosed.

Abstract: A staged fluidized catalytic cracker and method for cracking a hydrocarbonaceous material includes a plurality of staged reactors that have catalyst particles flowing in series from one reactor to the next and hydrocarbon feed that is delivered in parallel to the reactors. Between each reactor the partially spent catalyst is actively stripped to partially reactivate the catalyst. Once the catalyst is fully spent in the final reactor the catalyst can be oxidatively regenerated.

Abstract: Disclosed herein are processes in which precipitation permits removal of metal halides (e.g. AlCl3) from ionic liquids. After precipitation, the precipitated metal halides can be physically separated from the bulk ionic liquid. More effective precipitation can be achieved through cooling or the combination of cooling and the provision of metal halide seed crystals. The ionic liquids can be regenerated ionic liquid catalysts, which contain excess metal halides after regeneration. Upon removal of the excess metal halides, they can be reused in processes using ionic liquid catalysts, such as alkylation processes.

Abstract: The benzene content in a gasoline pool is reduced by a process that hydrogenates a benzene-containing isomerization zone feedstream. The additional cyclic hydrocarbons produced by the saturation of benzene can be processed in the isomerization zone for ring opening to increase the available paraffinic feedstock or the isomerization zone can be operated to pass the cyclic hydrocarbons through to a product recovery section. The isomerization zone feedstream is treated to remove contaminants and dried before entering the hydrogenation zone.

Abstract: Systems and methods for producing and using one or more doped catalysts are provided. One or more coked-catalyst particles can be fluidized in the presence of one or more oxidants to provide a fluidized mixture. The coke from the one or more coked-catalyst particles can be removed to provide regenerated catalyst particles within the fluidized mixture. One or more doping agents can be distributed to the fluidized mixture, and the one or more doping agents can be deposited onto the surface of the regenerated catalyst particles to provide a regenerated, doped catalyst particle.

Abstract: Alkylation processes are described herein. The alkylation process generally includes contacting an input stream including benzene with an alkylation catalyst and an alkylating agent to form an alkylation output stream including ethylbenzene. The alkylation process further includes contacting at least a portion of the alkylation output stream with a transalkylation catalyst and a benzene source to form a transalkylation output stream, wherein the benzene source is selected to minimize the amount of alkylation catalyst poisons contacting the alkylation catalyst.

Abstract: A process for preparing a gas oil cut comprises the following steps in succession: 1) oligomerizing an olefinic C2-C12 hydrocarbon cut, preferably C3-C7 and more preferably C3-C5; 2) separating the mixture of products obtained in step 1) into three cuts: a light cut containing unreacted C4 and/or C5 olefinic hydrocarbons, an intermediate cut having a T95 in the range 200-220° C. and a heavy cut comprising the complement; T95 being the temperature at which 95% by weight of product has evaporated, as determined in accordance with standard method ASTM D2887; 3) oligomerizing the intermediate cut obtained in the separation step; characterized in that in step 3), oligomerization is carried out in the presence of an olefinic C4 and/or C5 hydrocarbon cut in a weight ratio of intermediate cut to olefinic C4 and/or C5 cut in the range of 60/40 to 80/20.

Abstract: An integrated isomerization-alkylation process is disclosed that uses a common distillation zone. The process can comprise halogen removal. The process is suitable for the production of motor fuels from isoparaffins and olefins using solid alkylation and isomerization catalysts.

Abstract: A method for removing conjugated olefins from a composition comprising contacting the composition with a Diels-Alder dienophile to convert conjugated olefins to a Diels-Alder adduct and arresting the Diels-Alder adduct. A method comprising confining a Diels-Alder dienophile to a first side of a selectively permeable barrier wherein the barrier is more permeable to conjugated olefins and less permeable to Diels-Alder dienophile and Diels-Alder adduct, and contacting a composition comprising mono-olefins and conjugated olefins with the Diels-Alder dienophile to form Diels-Alder adduct, wherein the contacting reduces the concentration of conjugated olefins in the composition. A method for removing conjugated olefins from a composition comprising bubbling the composition through a liquid comprising Diels-Alder dienophile to form a liquid comprising Diels-Alder adduct.

Abstract: C2-C8-olefins are oligomerized in a process in which a stream of an olefin-containing hydrocarbon mixture is passed over a heterogeneous, nickel-containing oligomerization catalyst in n successive adiabatically operated reaction zones, where n?2, and the hydrocarbon mixture experiences a temperature increase 66 Treact in each reaction zone and the hydrocarbon mixture enters the first reaction zone at a temperature Tin and before entering each further reaction zone is cooled to a temperature which in each case may be up to 20° C. above or below Tin, and the relative catalyst volumes of the individual reaction zones are such that the difference in ?Treact between any two reaction zones is not more than 20° C.

Abstract: Catalyst component for the polymerization of alpha-olefins of general formula (I) wherein: M is a transition metal of groups 3, 4-10 of the periodic table of the elements, Each X group can be equal or different and it is hydride, halogen, alkyl, cycloalkyl, aryl, alkenyl, arylalkyl, arylalkenyl or alkylaryl with 1 to 20 carbon atoms, linear or branched. L is a neutral Lewis base A is a ring with delocalized &pgr; electrons, that directly coordinates to the transition metal M. Each E group can be equal to or different from each other and it is BRIII, CRIV2, SiRIII2, GeRIII2; at least one E is SiRIII2. RII is hydrogen, alkyl, cycloalkyl, aryl, alkenyl, arylalkyl, arylalkenyl or alkylaryl from 1 to 20 carbon atoms, linear or branched, whose hydrogens can be substituted by SiR3, GeR3, OR, NR2, OSiR3 or any combination of thereof. It can moreover form a condensed ring through another bond with E.

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: 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 cyclic process for the purification of a diolefin hydrocarbon stream produced in a naphtha steam cracker to produce a high quality diolefin hydrocarbon stream having extremely low levels of acetylene over an extended period because of the ability to readily cyclically regenerate catalyst contained in an off-line selective hydrogenation reaction zone. The spent or partially spent catalyst is contacted with a stream containing naphtha and hydrogen to restore at least a portion of the fresh catalyst activity by the extraction of polymer compounds therefrom.

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 motor fuel alkylate by reacting an alkene hydrocarbon, an alkane hydrocarbon and a hydrogen halide with a solid alkylation catalyst disposed in swing beds. The spent solid alkylation catalyst is regenerated in a highly integrated flow scheme associated with the alkylate recovery.

Abstract: A method is disclosed for the pretreatment of olefinic hydrocarbon feedstock to remove conjugated dienes and/or basic nitrogen compounds that deactivate acidic catalyst particles used in olefin conversion processes by reacting the dienes with one or more dienophiles to form the corresponding Diels-Alder adduct, followed by catalytic conversion of the olefinic hydrocarbon feedstock containing the adduct. The formation of the Diels-Alder adduct essentially eliminates the role of dienes in the feedstock as catalyst deactivating agents. When maleic anhydride (MA) is employed as the dienophile, basic nitrogen reacts with maleic anhydride, or with the tetrahydrophthalic anhydride adduct, to lower the amount of catalyst deactivating basic nitrogen compounds in the feedstock. Where the olefin conversion process comprises etherification of isoolefins with alkanol in a C.sub.4 + or C.sub.

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

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: A process is disclosed for the preparation of alkyl tertiary-alkyl ether concurrent with the alkylation of isoparaffins with olefins. The composite zeolite catalyst is reactivated in the alkyl tertiary-alkyl ether synthesis reactor.

Abstract: A process for the production of aromatic hydrocarbons from petroleum fractions containing paraffins which comprises passing said charge in the presence of hydrogen at 400.degree. C.-550.degree. C. over a catalyst containing from 0.1 to 1.5% by weight of at least one metal selected from the group consisting of platinum, rhenium, iridium, tin and germanium and containing sulfur in a sulfur/metals atomic ratio of from 0 to less than 1, supported on a crystalline, aluminum silicate zeolite containing alkaline cations, said zeolite having a pore dimension larger than 6.5 Angstroms, wherein the catalysts are in fixed beds in two reactors or sets of reactors arranged in parallel and operate at a pressure on the order of from 0.5 to 8 absolute bars wherein when a reactor set (DHC.sub.1 ) is producing aromatic hydrocarbons the other reactor set (DHC.sub.2 ) is swept by the hydrogen produced by the first reactor set (DHC.sub.