Abstract: Process and apparatus for producing a naphtha stream is provided. The process comprises providing a kerosene stream to a hydrocracking reactor. The kerosene stream is hydrocracked in the presence of a hydrogen stream and a hydrocracking catalyst in the hydrocracking reactor at hydrocracking conditions comprising a hydrocracking pressure, a hydrocracking temperature, and a liquid hourly space velocity at a net conversion of at least about 90%, to provide a hydrocracked effluent stream comprising liquefied petroleum gas, heavy naphtha fraction and light naphtha fraction. One or more of the hydrocracking conditions are adjusted to maintain a ratio of the light naphtha fraction to the heavy naphtha fraction of at least about 2 by weight, suitably at least about 2.2 and preferably at least about 2.5 in the hydrocracked effluent stream while maintaining the net conversion of at least about 90%.

Abstract: Process and apparatus for producing a naphtha stream is provided. The process comprises providing a kerosene stream to a hydrocracking reactor. The kerosene stream is hydrocracked in the presence of a hydrogen stream and a hydrocracking catalyst in the hydrocracking reactor at hydrocracking conditions comprising a hydrocracking pressure, a hydrocracking temperature, and a liquid hourly space velocity at a net conversion of at least about 90%, to provide a hydrocracked effluent stream comprising liquefied petroleum gas, heavy naphtha fraction and light naphtha fraction. One or more of the hydrocracking conditions are adjusted to maintain a ratio of the light naphtha fraction to the heavy naphtha fraction of at least about 2 by weight, suitably at least about 2.2 and preferably at least about 2.5 in the hydrocracked effluent stream while maintaining the net conversion of at least about 90%.

Abstract: GCI fuel compositions and methods of making them are described. The GCI fuel compositions comprises a fuel blend having an initial boiling point in a range of about 26° C. to about 38° C. and a final boiling point in a range of about 193° C. to less than 250° C., a density of about 0.72 kg/l to about 0.8 kg/l at 15° C., a research octane number of about 70 to about 85, and a cetane number of less than about 27, the fuel blend comprising a naphtha stream and a kerosene stream.

Abstract: A process is presented for recovering the hydrocarbon components from a naphtha feed to pass to a gasoline blending pool or to change the operations to increase the production of light olefins. The process includes the separation of the naphtha feedstock into a light naphtha stream and a heavy naphtha stream. The process further includes separating the light naphtha stream to recovery high quality non-normal hydrocarbons, and to separate normal hydrocarbons to the feed to the cracking unit.

Abstract: A process is presented for improving the feed to a cracking unit and a reforming unit from a naphtha feedstock. The process includes the use of a separation unit to generate a light naphtha feed and a heavy naphtha feed. The process further includes separating the light naphtha feed into a light naphtha feed comprising normal hydrocarbons and a light naphtha feed comprising non-normal hydrocarbons. The light naphtha feed comprising normal hydrocarbon is passed to the cracking unit and the heavy naphtha feed is passed to the reforming unit.

Abstract: GCI fuel compositions and methods of making them are described. The GCI fuel compositions comprises a fuel blend having an initial boiling point in a range of about 26° C. to about 38° C. and a final boiling point in a range of about 193° C. to less than 250° C., a density of about 0.72 kg/l to about 0.8 kg/l at 15° C., a research octane number of about 70 to about 85, and a cetane number of less than about 27, the fuel blend comprising a naphtha stream and a kerosene stream.

Abstract: A process for increasing the yields of light olefins and the yields of aromatics from a hydrocarbon stream is presented. The process includes a first separation to direct the light components that are not reformable to a cracking unit, with the remainder passed to a second separation unit. The second separation unit extracts normal components from the hydrocarbon stream to pass to the cracking unit. The resulting hydrocarbon stream with reduced light ends and reduced normals is passed to a reforming unit.

Abstract: A process for increasing the yields of light olefins and the yields of aromatics from a hydrocarbon stream is presented. The process includes a first separation to direct the light components that are not reformable to a cracking unit, with the remainder passed to a second separation unit. The second separation unit extracts normal components from the hydrocarbon stream to pass to the cracking unit. The resulting hydrocarbon stream with reduced light ends and reduced normals is passed to a reforming unit.

Abstract: The invention reduces the potential for catalyst fluidization in a reduction vessel of a continuous catalyst regeneration system. The gas exit area from the catalyst reduction zone is increased by ventilating the cylindrical baffle of the upper reduction zone. This provides an increased exit cross-sectional area for the upper reduction gas to escape and reduce the overall exit velocity of the combined upper and lower reduction gases and reduces the potential for catalyst fluidization.

Abstract: A process for increasing the yields of light olefins or shifting to increase the hydrocarbon components to gasoline blending pools from a hydrocarbon feedstock is presented. The process includes separating a naphtha feedstock to components to a first stream that are more readily processed in a cracking unit and to components in a second stream that are more readily processed in a reforming unit. The process includes the ability to convert components from the cracking stream to the reforming stream, and to convert components from the reforming stream to the cracking stream.

Abstract: A process for increasing the yields of light olefins and the yields of aromatics from a hydrocarbon stream is presented. The process includes a first separation to direct the light components that are not reformable to a cracking unit, with the remainder passed to a second separation unit. The second separation unit extracts normal components from the hydrocarbon stream to pass to the cracking unit. The resulting hydrocarbon stream with reduced light ends and reduced normals is passed to a reforming unit.

Abstract: A process for increasing the yields of light olefins and the yields of aromatics from a hydrocarbon stream is presented. The process includes a first separation to direct the light components that are not reformable to a cracking unit, with the remainder passed to a second separation unit. The second separation unit extracts normal components from the hydrocarbon stream to pass to the cracking unit. The resulting hydrocarbon stream with reduced light ends and reduced normals is passed to a reforming unit.

Abstract: A process is presented for the increasing the yields of aromatics from reforming a hydrocarbon feedstream. The process includes splitting a naphtha feedstream into a light hydrocarbon stream, and a heavier stream having a relatively rich concentration of naphthenes. The heavy stream is reformed to convert the naphthenes to aromatics and the resulting product stream is further reformed with the light hydrocarbon stream to increase the aromatics yields. The process includes passing a catalyst stream in a counter-current flow relative to the hydrocarbon process stream.

Abstract: The invention involves a process that reduces the potential for catalyst fluidization in a reduction vessel of a continuous catalyst regeneration system. The gas exit area from the catalyst reduction zone is increased by ventilating the cylindrical baffle of the upper reduction zone. This provides an increased exit cross-sectional area for the upper reduction gas to escape and reduce the overall exit velocity of the combined upper and lower reduction gases and reduces the potential for catalyst fluidization.

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 is presented for the increasing the yields of aromatics from reforming a hydrocarbon feedstream. The process includes splitting a naphtha feedstream into a light hydrocarbon stream, and a heavier stream having a relatively rich concentration of naphthenes. The heavy stream is reformed to convert the naphthenes to aromatics and the resulting product stream is further reformed with the light hydrocarbon stream to increase the aromatics yields. The process includes passing a catalyst stream in a counter-current flow relative to the hydrocarbon process stream.

Abstract: Systems and processes for the alkylation of a hydrocarbon are provided that utilize a plurality of moving bed radial flow reactors. An olefin injection point can be provided prior to each reactor by providing a mixer that mixes olefin with a hydrocarbon feed, or with the effluent stream from an upstream reactor, to produce a reactor feed stream. Catalyst can be provided from the reaction zone of one reactor to the reaction zone of a downstream reactor through catalyst transfer pipes, and can be regenerated after passing through the reaction zones of the reactors. The moving bed radial flow reactors can be stacked in one or more reactor stacks.

Abstract: The invention reduces the potential for catalyst fluidization in a reduction vessel of a continuous catalyst regeneration system. The gas exit area from the catalyst reduction zone is increased by ventilating the cylindrical baffle of the upper reduction zone. This provides an increased exit cross-sectional area for the upper reduction gas to escape and reduce the overall exit velocity of the combined upper and lower reduction gases and reduces the potential for catalyst fluidization.

Abstract: The invention involves a process that reduces the potential for catalyst fluidization in a reduction vessel of a continuous catalyst regeneration system. The gas exit area from the catalyst reduction zone is increased by ventilating the cylindrical baffle of the upper reduction zone. This provides an increased exit cross-sectional area for the upper reduction gas to escape and reduce the overall exit velocity of the combined upper and lower reduction gases and reduces the potential for catalyst fluidization.

Abstract: Systems and processes for hydrocarbon conversion are provided that utilize a plurality of moving bed reactors. The reactors may be moving bed radial flow reactors. Optional mixers that mix a portion of a second hydrocarbon feed with the effluent stream from an upstream reactor, to produce reactor feed streams may be employed, and the reactor feed streams may be introduced at injection points prior to each reactor. Catalyst can be provided from the reaction zone of one reactor to the reaction zone of a downstream reactor through catalyst transfer pipes, and can be regenerated after passing through the reaction zones of the reactors. The moving bed reactors can be stacked in one or more reactor stacks.