Abstract: Systems and methods are provided to allow for characterization of feeds, intermediate effluents, and/or products during lubricant base stock production. More generally, the systems and methods can allow for characterization of aromatics in various types of hydroprocessed intermediate effluents and/or products. In some aspects, the characterization can include measuring a fluorescence excitation-emission matrix spectrum for a sample, and then generating a representation of the spectrum by fitting the measured spectrum to a linear combination of spectra corresponding to compounds or compound classes. As the hydroprocessing process continues, additional measured spectra and comparing the fit quality of the representation to the subsequently measured spectra. When the fit quality falls below a threshold value, the loss in fit quality indicates a change in the number and/or distribution of aromatics in the sample.

Abstract: A method of converting naphtha is disclosed. The method includes heating the naphtha in stages in different heating units. The naphtha is vaporized in the first heating unit. And the vaporized naphtha undergoes the largest temperature change of the process in the second heating unit. A third heating unit can be a part of the reactor. The reactor includes a catalyst which is contacted with the pre-heated naphtha to convert it to C2 to C4 olefins.

Abstract: The invention is an integrated process for treating residual oil of a hydrocarbon feedstock. The oil is first subjected to delayed coking and then oxidative desulfurization. Additional, optional steps including hydrodesulfurization, and hydrocracking, may also be incorporated in to the integrated process.

Abstract: Provided is a hydrodesulfurization catalyst for hydrocarbon oil, the catalyst comprising: an inorganic oxide carrier comprising Si, Ti and Al; and at least one metal component, carried on the inorganic oxide carrier, being selected from the group consisting of group 6 elements, group 8 elements, group 9 elements and group 10 elements, wherein the content of Al in the inorganic oxide carrier is 50% by mass or higher in terms of Al2O3; the content of Si therein is 1.0 to 10% by mass in terms of SiO2; and the content of Ti therein is 12 to 28% by mass in terms of TiO2; and in the inorganic oxide carrier, the absorption edge wavelength of an absorption peak from Ti is 364 nm or shorter as measured by ultraviolet spectroscopy.

Abstract: A process and system is provided including hydroisomerization reaction zone for production of high octane gasoline blending components that provide high selectivity for producing high octane isomers of light paraffins. A light paraffin feed is enriched by incorporation of dissolved hydrogen, thereby permitting a reaction phase that is liquid or substantially liquid to produce high octane gasoline blending components. Accordingly, a substantially two phase isomerization reactor system is provided, with a hydrogen-enriched liquid feedstock phase and a solid phase catalyst.

Abstract: A delayed coking furnace (100) for heating coker feedstock (101) is disclosed. The furnace (100) includes a first heating zone (102) adapted to provide heat to the coker feedstock (101) through a convective heat transfer and then a second heating zone (104) positioned below the first heating zone (102) and adapted to heat the coker feedstock (101) through radiative heat transfer, wherein the second heating zone (104) include a lower portion and an upper portion. Further, said furnace (100) includes a plurality of burners (106) located at the lower portion of the second heating zone (104) and at least one baffle (111) disposed in the upper portion of the second heating zone (104). Further, the present disclosure provides that the at least one baffle (111) is adapted to increase a convective heat transfer coefficient associated with a flue gas flowing from the second heating zone (104) to the first heating zone (102).

Abstract: Embodiments of the disclosure provide a visbreaking system and method for upgrading heavy hydrocarbons. A heavy hydrocarbon feed is introduced to a furnace to produce a soaker feed stream. The soaker feed stream is introduced to a soaker to produce a soaker effluent stream. The soaker effluent stream is introduced to a fractionator to produce a visbreaker distillate stream and a visbreaker residue stream. The visbreaker residue stream and a water feed are introduced to a supercritical water reactor operated at supercritical conditions of water to produce an effluent stream. The effluent stream is introduced to a flash column to produce a gas phase stream including water and a liquid phase stream including water. A portion of the liquid phase stream and the heavy hydrocarbon feed is combined. Optionally, a portion of the gas phase stream and the heavy hydrocarbon feed is combined. Optionally, a portion of the gas phase stream is introduced to the fractionator.

Abstract: Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a petrochemicals production complex for conversion into light olefins and other hydrocarbon products. Feeds to the deep hydrogenation zone include middle distillate range streams from a distillate hydrotreating zone, a vacuum gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a middle distillate range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

Abstract: Methods for cracking a hydrocarbon oil include contacting the hydrocarbon oil with a catalyst system in a fluidized catalytic cracking unit to produce light olefins and gasoline fuel. The catalyst system includes a FCC base catalyst and a catalyst additive. The FCC base catalyst includes a Y-zeolite. The catalyst additive includes a framework-substituted *BEA-type zeolite. The framework-substituted *BEA-type zeolite has a modified *BEA framework. The modified *BEA framework is a *BEA aluminosilicate framework modified by substituting a portion of framework aluminum atoms of the *BEA aluminosilicate framework with beta-zeolite Al-substitution atoms selected from titanium atoms, zirconium atoms, hafnium atoms, and combinations thereof. The FCC base catalyst may include a framework-substituted ultra-stable Y (USY)-zeolite as the Y-zeolite.

Abstract: Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a steam cracker for conversion into light olefins. Feeds to the deep hydrogenation zone include diesel range streams from a diesel hydrotreating zone, a gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a diesel range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

Abstract: Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a steam cracker for conversion into light olefins. Feeds to the deep hydrogenation zone include diesel range streams from a diesel hydrotreating zone, a gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a diesel range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

Abstract: A feedstock is processed in an FCC unit to produce at least light olefins, FCC naphtha, light cycle oil and heavy cycle oil. Light cycle oil, and in certain embodiments hydrotreated light cycle oil, is subjected to deep hydrogenation to produce a deeply hydrogenated middle distillate fraction. All or a portion of the deeply hydrogenated middle distillate fraction is used as feed to the stream cracking zone to produce light olefins.

Abstract: Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a steam cracker for conversion into light olefins. Feeds to the deep hydrogenation zone include diesel range streams from a diesel hydrotreating zone, a gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a diesel range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

Abstract: Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a steam cracker for conversion into light olefins. Feeds to the deep hydrogenation zone include diesel range streams from a diesel hydrotreating zone, a gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a diesel range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

Abstract: A feedstock is processed in an FCC unit to produce at least light olefins, FCC naphtha, light cycle oil and heavy cycle oil. Light cycle oil, and in certain embodiments hydrotreated light cycle oil, is subjected to hydrogenation to produce a deeply hydrogenated middle distillate fraction. All or a portion of the deeply hydrogenated middle distillate fraction is used as feed to a petrochemicals production complex to produce light olefins.

Abstract: A method and a system for hydrocracking an oil feedstock to produce a light oil stream without build-up of heavy polynuclear aromatic (HPNA) hydrocarbons in the recycle stream. The method may include hydrocracking an oil feedstock, separating the produced effluent into a first, second, and third product stream, and hydrogenating the third product stream in a third reactor over a noble metal hydrogenation catalyst at an operational pressure equal to or less than the second reactor.

Abstract: A feedstock is processed in a coking zone unit to produce at least light gases, coker naphtha, light coker gas oil and petroleum coke. Light coker gas oil, and in certain embodiments hydrotreated light coker gas oil, is subjected to deep hydrogenation to produce a deeply hydrogenated middle distillate fraction. All or a portion of the deeply hydrogenated middle distillate fraction is used as feed to the stream cracking zone to produce light olefins.

Abstract: The present disclosure relates to an FCC catalyst additive for cracking of petroleum feedstock and a process for its preparation. The FCC catalyst additive of the present disclosure comprises at least one zeolite, at least one clay, at least one binder, phosphorous in the form of P2O5, and at least one Group IVB metal compound. The FCC catalyst additive of the present disclosure is hydrothermally stable and has improved matrix surface area even after various hydrothermal treatments. The FCC catalyst additive of the present disclosure can be used in combination with the conventional FCC catalyst for catalytic cracking to selectively enhance the propylene and LPG yields.

Abstract: Techniques for processing residuum include receiving a feed stream that includes a residuum hydrocarbon fraction at an ebullated bed hydroconversion reactor; contacting the residuum hydrocarbon fraction with hydrogen and a hydroconversion catalyst in the ebullated bed hydroconversion reactor to produce a partially converted reactor effluent product; separating, in a first separation zone, the partially converted reactor effluent product into a distillate stream and a heavy hydrocarbon stream; feeding the distillate stream to a bottom portion of an integrated hydrocracking/hydrofinishing reactor; and feeding the heavy hydrocarbon stream to a top portion of the hydrofinishing reactor.

Abstract: A feedstock is processed in a coking zone unit to produce at least light gases, coker naphtha, light coker gas oil and petroleum coke. Light coker gas oil, and in certain embodiments hydrotreated light coker gas oil, is subjected to deep hydrogenation to produce a deeply hydrogenated middle distillate fraction. All or a portion of the deeply hydrogenated middle distillate fraction is used as feed to a petrochemicals production complex to produce light olefins.