A process for operating a reforming system by operating a reforming section containing a plurality of reactors, wherein each of the plurality of reactors containing a reforming catalyst capable of catalyzing the conversion of at least a portion of the hydrocarbons in a treated hydrocarbon stream into a reactor effluent comprising aromatic hydrocarbons, and operating a sulfur guard bed (SGB) to remove sulfur and sulfur-containing hydrocarbons from a hydrocarbon feed to provide the treated hydrocarbon stream, where the SGB contains at least a layer of a SGB catalyst comprising the same catalyst as the reforming catalyst, and where each reactor of the plurality of reactors within the reforming section may be operated at a higher operating temperature than an operating temperature of the SGB. A system for carrying out the process is also provided.

A process for operating a reforming system by operating a reforming section containing a plurality of reactors, wherein each of the plurality of reactors containing a reforming catalyst capable of catalyzing the conversion of at least a portion of the hydrocarbons in a treated hydrocarbon stream into a reactor effluent comprising aromatic hydrocarbons, and operating a sulfur guard bed (SGB) to remove sulfur and sulfur-containing hydrocarbons from a hydrocarbon feed to provide the treated hydrocarbon stream, where the SGB contains at least a layer of a SGB catalyst comprising the same catalyst as the reforming catalyst, and where each reactor of the plurality of reactors within the reforming section may be operated at a higher operating temperature than an operating temperature of the SGB. A system for carrying out the process is also provided.

Method of refining whole crude oil or a wide cut crude oil, the methods comprising a combination of a hydrotreating reactor, a distillation tower, and an optional flash evaporation separator. The methods can also include light ends processing, fluid catalytic cracking, reforming, hydrocracking, and demetalization. In some methods a whole crude oil is first processed through a flash evaporation separator to create a wide cut crude oil and in other methods, the flash evaporation separator is not used as the whole crude oil is first treated in a hydrotreater.

A process for producing light olefins comprising thermal cracking. Hydrocracked streams are thermally cracked in a steam cracker to produce light olefins. A pyrolysis gas stream is separated into a light stream and a heavy stream. A light stream is separated into an aromatic naphtha stream and a non-aromatic naphtha stream. The aromatics can be saturated and thermally cracked. The integrated process may be employed to obtain olefin products of high value from a crude stream.

A method for producing a low-viscosity high-aromatic non-carcinogenic petroleum-based process oil which can be used as a plasticizer oil or an extender oil in the manufacture of synthetic rubber and tyres is described. The oil is obtained from by-product fractions of secondary petrochemical processes by fractional distillation, wherein the used by-product fractions of secondary petrochemical processes are products of catalytic cracking, or products of catalytic reforming, or aromatic extracts, or mixtures thereof, which have an initial boiling point of no less than 200° C. and above and a final boiling point of no less than 360° C. at atmospheric pressure, and contain no less than 85% of aromatic constituents and no more than 10.0 mg/kg of the sum of the following polycyclic aromatic hydrocarbons: benz[a]anthracene; chrysene; benzo[b]fluoranthene; benzo[i]fluoranthene; benzo[k]fluoranthene; benzo[e]pyrene; benzo[a]pyrene; and dibenzo[a,h]anthracene.

A naphtha reforming reactor system comprising a first reactor comprising a first inlet and a first outlet, wherein the first reactor is configured to operate as an adiabatic reactor, and wherein the first reactor comprises a first naphtha reforming catalyst; and a second reactor comprising a second inlet and a second outlet, wherein the second inlet is in fluid communication with the first outlet of the first reactor, wherein the second reactor is configured to operate as an isothermal reactor, and wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, a heat source configured to heat the interior of the reactor furnace; and a second naphtha reforming catalyst disposed within the plurality of tubes, wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different.

A naphtha reforming reactor system comprising a first reactor comprising a first inlet and a first outlet, wherein the first reactor is configured to operate as an adiabatic reactor, and wherein the first reactor comprises a first naphtha reforming catalyst; and a second reactor comprising a second inlet and a second outlet, wherein the second inlet is in fluid communication with the first outlet of the first reactor, wherein the second reactor is configured to operate as an isothermal reactor, and wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, a heat source configured to heat the interior of the reactor furnace; and a second naphtha reforming catalyst disposed within the plurality of tubes, wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different.

The present disclosure is directed to a non-destructive process for removing metals, metal ions and metal oxides in alumina-based materials without destroying alumina, allowing the regeneration of alumina-based catalysts. The non-destructive process uses an extracting agent that sequesters metals, metal ions and/or metal oxides present in alumina-based materials without destroying the alumina, allowing the regeneration of alumina-based catalysts.

Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into light and heavy fractions utilizing convection heat from heaters used in steam cracking. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize either an ebullated bed reactor with extrudate catalysts or a slurry hydrocracking reactor using a homogeneous catalyst system, such as a molybdenum based catalysts which may optionally be promoted with nickel. Products from the upgrading operations can be finished olefins and/or aromatics, or, for heavier products from the upgrading operations, may be used as feed to the steam cracker.

This application relates to renewable diesel production and to production of renewable naphtha in a renewable diesel unit. Disclosed herein is an example of a method of renewable diesel production. Examples embodiments of the method may include hydrotreating the biofeedstock by reaction with hydrogen to form a hydrotreated biofeedstock; contacting at least a portion of the hydrotreated biofeedstock with a dewaxing catalyst to produce a renewable diesel product and a renewable naphtha product; separating the renewable diesel product and the renewable naphtha product in a product splitter; and monitoring an octane number of the renewable naphtha product with an analyzer.