The invention provides a process for preparing a fluid having a boiling point in the range of from 150 to 260° C. and comprising more than 80% by weight of isoparaffins and less than 50 ppm of aromatics, comprising the step of catalytically hydrogenating a feed comprising more than 85% by weight of oligomerized olefins, at a temperature from 115 to 195° C. and at a pressure from 30 to 70 bars. The invention also provides the fluid obtainable by the process of the invention and the use of said fluid.

In accordance with one or more embodiments of the present disclosure, a method for producing aromatic compounds from pyrolysis gasoline comprising C.sub.5-C.sub.6 non-aromatic hydrocarbons includes aromatizing the pyrolysis gasoline in an aromatization unit, thereby converting the C.sub.5-C.sub.6 non-aromatic hydrocarbons to a first stream comprising benzene-toluene-xylenes (BTX); hydrotreating the first stream comprising BTX in a selective hydrotreatment unit, thereby producing a de-olefinated stream comprising BTX; hydrodealkylating and transalkylating the de-olefinated stream comprising BTX in a hydrodealkylation-transalkylation unit, thereby producing a second stream comprising BTX, the second stream comprising BTX having a greater amount of benzene and xylenes than the first stream comprising BTX; and processing the second stream comprising BTX in an aromatics recovery complex, thereby producing the aromatic compounds from the pyrolysis gasoline, the aromatic compounds comprising benzene, toluene, and xylenes.

A process for the catalytic cracking of hydrocarbon oils includes the step of contacting a hydrocarbon oil feedstock with a catalytic cracking catalyst in a reactor having one or more fast fluidized reaction zones for reaction. At least one of the fast fluidized reaction zones of the reactor is a full dense-phase reaction zone, and the axial solid fraction ε of the catalyst is controlled within a range of about 0.1 to about 0.2 throughout the full dense-phase reaction zone. When used for catalytic cracking of hydrocarbon oils, particularly heavy feedstock oils, the process, reactor and system show a high contact efficiency between oil and catalyst, a selectivity of the catalytic reaction, an effectively reduced yield of dry gas and coke, and an improved yield of high value-added products such as ethylene and propylene.

Oxidized disulfide oil (ODSO) compounds or ODSO compounds and disulfide oil (DSO) compounds are reacted with a hydrogen addition feed in a hydroprocessing complex. The hydrogen addition process can include naphtha hydrotreatment, middle distillate hydrotreatment, vacuum gas oil hydrocracking, and vacuum gas oil hydrotreatment. The ODSO or ODSO and DSO components are converted to hydrogen sulfide, water and alkanes.

In chemical processes for cracking hydrocarbons, reactors are subject to coking During the decoke process carburization of the metal substrate can occur, negatively impacting reactor life. Decokes are also costly due to down-time where costs are incurred without production of commercial products. Reducing the frequency of decokes provides an opportunity to reduce the financial impacts of downtimes. A start-up procedure is described herein that limits initial coke deposition, leading to a reduced tendency for carburization of the metal substrate, improving reactor life, and more importantly, extending reactor run length.

A multi-stage process for transforming a high sulfur ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process that produces a Product Heavy Marine Fuel Oil that can be used as a feedstock for subsequent refinery process such as anode grade coking, needle coking and fluid catalytic cracking. The Product Heavy Marine Fuel Oil exhibits multiple properties desirable as a feedstock for those processes including a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process is also disclosed.

A system and method for processing pyrolysis gasoline is disclosed. The system and method involves separating a pyrolysis gasoline stream to produce a first stream comprising primarily un-hydrogenated C.sub.9+ compounds. The separating of the pyrolysis e gasoline occurs without hydrogenation being carried out on the pyrolysis gasoline before the separating.

Systems and methods are provided for performing slurry hydroconversion of feeds that include substantial amounts of 1050° F+ (566° C+) components. The productivity of the slurry hydroconversion reaction is improved by recycling slurry hydroconversion pitch or bottoms back to the slurry hydroprocessing reaction system. The mass flow rate of the recycle stream can correspond to 50% or more of the mass flow rate of the fresh feed to the reaction system, and the recycle stream can include more than 50 wt % of 566° C+ components. It has been discovered that using a substantial recycle stream composed of a majority of unconverted 566° C+ bottoms can increase the productivity of the slurry hydroprocessing reaction system when operating at a net conversion relative to 524° C (975° F) of less than 90 wt %. Additionally, by using a recycle stream composed of a majority of 566° C+ components, the amount of lower boiling components (in the heavy hydrocarbon feed and/or in the recycle stream) that are exposed multiple times to the slurry hydroprocessing environment is reduced or minimized This can allow for formation of slurry hydroconversion products with increased amounts of vacuum gas oil boiling range components.

A process for reducing the environmental contaminants in a ISO 8217: 2017 Table 2 compliant Feedstock Heavy Marine Fuel Oil and resulting product, the process involving: mixing a Feedstock Heavy Marine Fuel Oil with a Activating Gas to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture; separating the Product Heavy Marine Fuel Oil from the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil complies with ISO 8217:2017 Table 2 for residual marine fuel and the Environmental Contaminants, which are selected from the group consisting of: a sulfur; vanadium, nickel, iron, aluminum and silicon and combinations thereof, are less than 0.5 wt. %. The Product Heavy Marine Fuel Oil can be used as blending stock for an ISO 8217:2017 Table 2 compliant, IMO 2020 compliant, low sulfur heavy marine fuel composition.

A non-petroleum or renewable feedstock containing oxygen and contaminants of metals, gums, and resins is treated by introducing the feedstock into a reactor at a flow velocity of at least 20 ft/sec. The feedstock is heated within the reactor and cooled to form a reduced-temperature reactor product. At least a portion of the reduced-temperature reactor product is feed into a hydroprocessing reactor containing a hydroprocessing catalyst to form a hydroprocessed product. The hydroprocessed product is cooled and non-condensable gases, metals and water are separated and removed to form a final product. The final product has an oxygen content that is 60% or less of that of the feedstock, and wherein the final product comprises 25 wt % or less any triglycerides, monoglycerides, diglycerides, free fatty acids, phosphatides, sterols, tocopherols, tocotrienols, or fatty alcohols, from 5 wt % to 30 wt % naphtha, and 50 wt % or more diesel.