The present disclosure provides processes for refining hydrocarbon feedstocks and apparatus thereof. In at least one embodiment, a process includes hydroprocessing a mineral hydrocarbon feedstock in the presence of a first catalyst in a first reactor, and removing a first reactor effluent from the first reactor. The process includes hydroprocessing a biocomponent feedstock in the presence of a second catalyst in a second reactor, and removing a second reactor effluent from the second reactor. The process includes mixing the first reactor effluent and the second reactor effluent to form a mixture. The process includes introducing the mixture to a separation unit to form a fuel product. In at least one embodiment, an apparatus includes a first hydroprocess reactor. The apparatus includes a second hydroprocess reactor coupled with the first hydroprocess reactor. The apparatus includes a separation unit coupled with the second hydroprocess reactor.

The invention pertains to a process for deep desulphurization of low sulphur content feedstock comprising the steps of providing a low sulphur content hydrocarbon feedstock and contacting said hydrocarbon feedstock with a cobalt-molybdenum desulphurizing system or a nickel-molybdenum desulphurizing system in an oxide form in order to obtain a very low sulphur product comprising less than 5 ppm by weight sulphur.

The invention pertains to a process for deep desulphurization of low sulphur content feedstock comprising the steps of providing a low sulphur content hydrocarbon feedstock and contacting said hydrocarbon feedstock with a cobalt-molybdenum desulphurizing system or a nickel-molybdenum desulphurizing system in an oxide form in order to obtain a very low sulphur product comprising less than 5 ppm by weight sulphur.

Processes for producing olefins include integration of steam cracking with a dual catalyst metathesis process. The processes include steam cracking a hydrocarbon feed to form a cracking reaction effluent containing butenes, separating the cracking reaction effluent to produce a cracking C4 effluent including normal butenes, isobutene, and 1,3-butadiene, subjecting the cracking C4 effluent to selective hydrogenation to convert 1,3-butadiene in the cracking C4 effluent to normal butenes, removing isobutene from a hydrogenation effluent to produce a metathesis feed containing normal butenes, and contacting the metathesis feed with a metathesis catalyst and a cracking catalyst directly downstream of the metathesis catalyst to produce a metathesis reaction effluent. Contacting with the metathesis catalyst causes metathesis of normal butenes to produce ethylene, propene, and C5+ olefins, and contacting with the cracking catalyst causes C5+ olefins produced through metathesis to undergo cracking reactions to produce additional propene, ethylene, or both.

Processes for producing olefins include integration of steam cracking with a dual catalyst metathesis process. The processes include steam cracking a hydrocarbon feed to form a cracking reaction effluent containing butenes, separating the cracking reaction effluent to produce a cracking C4 effluent including normal butenes, isobutene, and 1,3-butadiene, subjecting the cracking C4 effluent to selective hydrogenation to convert 1,3-butadiene in the cracking C4 effluent to normal butenes, removing isobutene from a hydrogenation effluent to produce a metathesis feed containing normal butenes, and contacting the metathesis feed with a metathesis catalyst and a cracking catalyst directly downstream of the metathesis catalyst to produce a metathesis reaction effluent. Contacting with the metathesis catalyst causes metathesis of normal butenes to produce ethylene, propene, and C5+ olefins, and contacting with the cracking catalyst causes C5+ olefins produced through metathesis to undergo cracking reactions to produce additional propene, ethylene, or both.

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.

Systems and methods are provided for hydroprocessing of bio-derived feeds, such as bio-oils and/or other types of feeds including triglycerides, fatty acids, and/or fatty acid derivatives. The systems and methods can assist with maintaining a desired temperature profile within a reactor while performing hydroprocessing on a feed with substantial oxygen content. In various aspects, the initial bed of the reactor can be exposed to 30 vol % or less of the total fresh feed. The remaining portions of the fresh feed can be introduced below one or more of the catalyst beds in the reactor. By reducing or minimizing the amount of fresh feed introduced upstream from the initial catalyst bed that contains a catalyst with hydrodeoxygenation activity, the net amount of product recycle can be reduced or minimized while still maintaining a target temperature profile across individual catalyst beds and/or across the reactor.

Systems and methods are provided for hydroprocessing of bio-derived feeds, such as bio-oils and/or other types of feeds including triglycerides, fatty acids, and/or fatty acid derivatives. The systems and methods can assist with maintaining a desired temperature profile within a reactor while performing hydroprocessing on a feed with substantial oxygen content. In various aspects, the initial bed of the reactor can be exposed to 30 vol % or less of the total fresh feed. The remaining portions of the fresh feed can be introduced below one or more of the catalyst beds in the reactor. By reducing or minimizing the amount of fresh feed introduced upstream from the initial catalyst bed that contains a catalyst with hydrodeoxygenation activity, the net amount of product recycle can be reduced or minimized while still maintaining a target temperature profile across individual catalyst beds and/or across the reactor.

A hydrocracking process for maximization of naphtha while producing base oil is disclosed. The hydrocracking process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking unit in the presence of a hydrogen stream and a hydrocracking catalyst to produce a hydrocracked effluent stream. The hydrocracked effluent stream is separated in a separator to provide a vapor hydrocracked stream and a liquid hydrocracked stream. The liquid hydrocracked stream is fractionated to provide a naphtha stream, a kerosene stream, a diesel stream and a first unconverted oil stream. A recycle stream comprising a portion of the kerosene stream, a portion of the diesel stream, and a portion of the first unconverted oil stream is recycled to the hydrocracking unit to provide a second unconverted oil stream. A remaining portion of the first unconverted oil stream is withdrawn for base oil production.

A hydrocracking process for maximization of naphtha while producing base oil is disclosed. The hydrocracking process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking unit in the presence of a hydrogen stream and a hydrocracking catalyst to produce a hydrocracked effluent stream. The hydrocracked effluent stream is separated in a separator to provide a vapor hydrocracked stream and a liquid hydrocracked stream. The liquid hydrocracked stream is fractionated to provide a naphtha stream, a kerosene stream, a diesel stream and a first unconverted oil stream. A recycle stream comprising a portion of the kerosene stream, a portion of the diesel stream, and a portion of the first unconverted oil stream is recycled to the hydrocracking unit to provide a second unconverted oil stream. A remaining portion of the first unconverted oil stream is withdrawn for base oil production.