Abstract: A graphics processing system comprising: a tiling unit configured to tile a first view of a scene into a plurality of tiles; a processing unit configured to identify a first subset of the tiles that are associated with regions of the scene that are viewable in a second view; and a rendering unit configured to render to a render target each of the identified tiles.

Abstract: A flexible process for gasoline refineries is described. The process can vary depending on the available feedstock and the desired products. At one time, the process can involve disproportionating pentanes to a product mixture including isobutane and isohexane. At other times, by switching the feedstock and operating conditions, the process can convert a mixture of C4 and C7 paraffins to a low aromatic blendstock with suitable octane and a vapor pressure lower than butanes. The process can be performed in separate stand-alone units operated at different times, or a single unit can be operated according to one process at one time and according to the other process at another time.

Abstract: A hydrocarbon conversion process is described. The process involves contacting a hydrocarbon feed with a lactamium based ionic liquid catalyst in a reaction zone under reaction conditions to form a mixture comprising reaction products, and the lactamium based ionic liquid catalyst. Typical hydrocarbon conversion processes include alkylation, oligomerization, isomerization, disproportionation, and reverse disproportionation.

Abstract: A process utilizing an ionic liquid is described. The process includes contacting a hydrocarbon feed with an ionic liquid component, the ionic liquid component comprising a mixture of a first ionic liquid and a viscosity modifier, wherein a viscosity of the ionic liquid component is at least about 10% less than a viscosity of the first ionic liquid.

Abstract: An integrated alkylation and disproportionation process and apparatus are described. n-C4 and n-C5 are routed to a disproportionation reaction zone for conversion to iso-C4 and C6+ isoparaffin-rich product. The iso-C4 is routed to an alkylation reaction zone and reacted with refinery propylene and butenes to produce alkylate product. The C6+ isoparaffin-rich product and alkylate product are recovered. Unconverted iso-C4 and/or olefins are recycled to the alkylation reaction zone, and unconverted n-C4 and n-C5 are recycled to the disproportionation reaction zone.

Abstract: An integrated process for gasoline production is described. The process includes introducing a feed comprising n-C5 hydrocarbons into a disproportionation reaction zone in the presence of a disproportionation catalyst to form a disproportionation mixture comprising iso-C4 and C6+ disproportionation products and unreacted n-C5 hydrocarbons. An iso-C4 hydrocarbon stream and an olefin feed are introduced into an alkylation reaction zone in the presence of an alkylation catalyst to produce an alkylation mixture comprising alkylate and unreacted iso-C4 paraffins. The disproportionation mixture and the alkylation mixture are combined, and the combined mixture is separated into at least a stream comprising the alkylate product, an iso-C4 stream, and an unreacted n-C5 hydrocarbon stream. The iso-C4 stream is recycled to the alkylation reaction zone, and the unreacted n-C5 hydrocarbon stream is recycled to the disproportionation reaction zone. The stream comprising the alkylate product is recovered.

Abstract: A hydrocarbon disproportionation process is described. The process includes contacting a hydrocarbon feed in a disproportionation reaction zone with a disproportionation catalyst in the presence of hydrogen and an added chloride promoter under disproportionation conditions including to obtain disproportionation products, wherein the disproportionation catalyst comprises a solid catalyst comprising a refractory inorganic oxide having a metal halide dispersed thereon.

Abstract: A flexible hydrocarbon conversion process utilizing the same reaction zone for isomerization and disproportionation is described. The feed and type of products are selected. The hydrocarbon feed is contacted with a catalyst and in the presence of hydrogen and an added chloride promoter. The catalyst comprises a solid catalyst comprising a refractory inorganic oxide having a metal halide dispersed thereon. The operating conditions are varied depending on whether isomerization or disproportionation is desired.

Abstract: A hydrocarbon conversion process is described. The process includes contacting a hydrocarbon feed with an acidic catalyst under hydrocarbon conversion conditions in a hydrocarbon conversion zone. The hydrocarbon feed reacts to form a mixture comprising reaction products, the acidic catalyst, and deactivated acidic catalyst containing conjunct polymer. The mixture is separated into at least two streams, a first stream comprising the reaction products and a second stream comprising the deactivated acidic catalyst. The reaction products are recovered. The deactivated acidic catalyst is contacted with at least one silane or borane compound in a regeneration zone under regeneration conditions, the conjunct polymer reacting with the at least one silane or borane compound resulting in a catalyst phase and an organic phase containing the conjunct polymer and at least one silyl or boryl compound.

Abstract: Various embodiments of the present invention relate to a multilayered structure and balloon including the same. In various embodiments, the present invention provides a multilayered structure including at least one A layer (a) including a linear olefin polymer or copolymer, at least one B layer (b) including a cyclic olefin polymer or copolymer, and at least one A layer (c) including a linear olefin polymer or copolymer. The cyclic olefin polymer or copolymer of the at least one B layer is a polymer or copolymer of a substituted or unsubstituted norbornene.

Abstract: A method for regenerating deactivated ionic liquid catalyst containing conjunct polymer. The deactivated ionic liquid catalyst containing the conjunct polymer is contacted with either at least one metal complex having a general formula M1n+Rn, or at least one metal complex having a general formula [M2a+]x[M3b+yRz](xa/(z?by)). The conjunct polymer reacts with the reagent and can be extracted from the ionic liquid. The mixture is separated into a hydrocarbon effluent and an ionic liquid effluent.

Abstract: Processes for the disproportionation and isomerization of a C5 hydrocarbon feed using a liquid catalyst comprising an ionic liquid and a carbocation promoter are described. The ionic liquid is unsupported, and the reactions occur at temperatures below about 200° C.

Abstract: A hydrocarbon conversion process is described. The process involves contacting a hydrocarbon feed with a lactamium based ionic liquid catalyst in a reaction zone under reaction conditions to form a mixture comprising reaction products, and the lactamium based ionic liquid catalyst. Typical hydrocarbon conversion processes include alkylation, oligomerization, isomerization, disproportionation, and reverse disproportionation.

Abstract: Processes for the disproportionation and isomerization of a C5 hydrocarbon feed using a liquid catalyst comprising an ionic liquid and a carbocation promoter are described. The ionic liquid is unsupported, and the reactions occur at temperatures below about 200° C.

Abstract: A hydrocarbon conversion process is described. The process includes contacting a hydrocarbon feed with an acidic catalyst under hydrocarbon conversion conditions in a hydrocarbon conversion zone. The hydrocarbon feed reacts to form a mixture comprising reaction products, the acidic catalyst, and deactivated acidic catalyst containing conjunct polymer. The mixture is separated into at least two streams, a first stream comprising the reaction products and a second stream comprising the deactivated acidic catalyst. The reaction products are recovered. The deactivated acidic catalyst is contacted with at least one silane or borane compound in a regeneration zone under regeneration conditions, the conjunct polymer reacting with the at least one silane or borane compound resulting in a catalyst phase and an organic phase containing the conjunct polymer and at least one silyl or boryl compound.

Abstract: Systems and methods for imaging a volume-of-interest, which may include an object or point of interest to be analyzed in a display of three-dimensional data.

Abstract: A flexible process for gasoline refineries is described. The process can vary depending on the available feedstock and the desired products. At one time, the process can involve disproportionating pentanes to a product mixture including isobutane and isohexane. At other times, by switching the feedstock and operating conditions, the process can convert a mixture of C4 and C7 paraffins to a low aromatic blendstock with suitable octane and a vapor pressure lower than butanes. The process can be performed in separate stand-alone units operated at different times, or a single unit can be operated according to one process at one time and according to the other process at another time.

Abstract: A process for refining naphtha and upgrading butanes is described. The process involves separating a hydrotreated heavy naphtha feed into a C7-rich fraction and a C8+-rich fraction in a separation zone and then reacting the C7-rich fraction with C4 paraffins to form to a low aromatic gasoline blendstock. The C8+-rich fraction is sent to a reforming zone to form a reformed product with higher octane and lower RVP than a reformed product derived from heavy naphtha.

Abstract: Processes for the disproportionation and isomerization of a C5 hydrocarbon feed using a liquid catalyst comprising an ionic liquid and a halocarbon carbocation promoter are described. The ionic liquid is unsupported, and the reactions occur at temperatures below about 200° C.

Abstract: Processes for the disproportionation and isomerization of a hydrocarbon feed using a liquid catalyst comprising an ionic liquid and a carbocation promoter are described. The ionic liquid is unsupported, and the reactions occur at temperatures below about 200° C.