A process for separating and upgrading a hydrocarbon feed includes passing the hydrocarbon feed to a distillation unit to separate it into at least a naphtha stream and a residue, passing the naphtha stream to a NHT that hydrotreats the naphtha stream to produce a hydrotreated naphtha, passing the hydrotreated naphtha to a NREF that reforms the hydrotreated naphtha to produce a reformate, passing the reformate to an ARC that processes the reformate to produce at least one aromatic product effluent and an aromatic bottoms stream, passing at least a portion of the residue to a residue hydroprocessing unit that hydroprocesses the portion of the residue to produce a hydroprocessed effluent, and passing a portion of the aromatic bottoms stream to the residue hydroprocessing unit to increase the solubility of the asphaltene compounds and reduce sedimentation. Systems for conducting the process are also disclosed.

The present invention relates to a process for converting vegetable oils, animal fats, residual edible oils and carboxylic acids into renewable liquid fuels, such as bionaphtha, bioJET-A1 and renewable diesel, for use in a mixture with fossil fuels. The process consists of two steps: hydrotreating and hydrocracking. The effluent from the hydrotreatment step presents aromatics, olefins and compounds resulting from the polymerization of esters and acids in its composition. This fact occurs due to the use of partially reduced catalysts and without injection of sulfide agent and allows obtaining a bioJET-A1 with adequate quality for use in a mixture with fossil kerosene. At the same time, the process generates, in addition to products in the distillation range of naphtha, kerosene and diesel, high molecular weight linear paraffins (with up to 40 carbon atoms).

The invention is a process for dearomatization and isomerization of a feedstock having less than or equal to 10 ppm by weight of sulphur, the process comprising: Hydrodearomatizing the feedstock at a temperature ranging from 150 to 220° C. and at a pressure ranging from 20 to 150 bars, in order to provide a dearomatized product; Hydroisomerizing the dearomatized product at a temperature ranging from 250 to 320° C. and at a pressure ranging from 40 to 60 bars in the presence of a catalyst based on platinum or palladium, in order to provide an isomerized product; Hydrodearomatizing the isomerized product at a temperature ranging from 150 to 220° C. and at a pressure ranging from 20 to 150 bars, in order to provide an isomerized and dearomatized product.

A method for upgrading mixed pyrolysis oil may include contacting the mixed pyrolysis oil with hydrogen in the presence of a mixed metal oxide catalyst at reaction conditions to produce a reaction effluent including light aromatic compounds. The mixed pyrolysis oil includes multi-ring aromatic compounds and is formed from light pyrolysis oil and heavy pyrolysis oil at a ratio of 10:90 to 40:60 with light pyrolysis oil representing a bottom stream of a gas steam cracker and heavy pyrolysis oil representing a bottom stream of a naphtha steam cracker. The mixed metal oxide catalyst includes a plurality of catalyst particles with each catalyst particles including a plurality of metal oxides. An associated system for upgrading mixed pyrolysis oil may include a pyrolysis upgrading unit housing the mixed metal oxide catalyst and a separation unit operable to separate used mixed metal oxide catalyst from the reaction effluent.

The present invention relates to a process for the production of polymers from waste plastics feedstocks comprising the steps in this order of: (a) providing a hydrocarbon stream A obtained by treatment of a waste plastics feedstock; (b) optionally providing a hydrocarbon stream B; (c) supplying a feed C comprising a fraction of the hydrocarbon stream A and a fraction of the hydrocarbon stream B to a thermal cracker furnace comprising cracking coil(s); (d) performing a thermal cracking operation in the presence of steam to obtain a cracked hydrocarbon stream D; (e) supplying the cracked hydrocarbon stream D to a separation unit; (f) performing a separation operation in the separation unit to obtain a product stream E comprising a monomer; (g) supplying the product stream E to a polymerisation reactor; and (h) performing a polymerisation reaction in the polymerisation reactor to obtain an polymer. The process of the present invention allows for optimisation of the quantity of waste plastic material that finds its way back into a polymer that is produced as outcome of the process.

In accordance with one or more embodiments of the present disclosure, a method for hydrodearylating aromatic bottoms oil includes contacting at least one aromatic bottoms oil stream with at least one catalyst composition and hydrogen in a reactor in order to hydrodearylate the aromatic bottoms oil stream. The catalyst composition includes a catalyst support comprising framework-substituted ultra-stable Y-type (USY) zeolite substituted with at least zirconium atoms. The catalyst composition does not include a hydrogenative metal component disposed on the support.

In the hydrocracking process in accordance with the invention, which comprises a hydrocracking section, a high pressure hot separator and a fractionation section, upstream of the fractionation section, a stripper or reboiler column type separation column is added which treats at least a portion of the heavy effluent obtained from the high pressure hot separator. All or a portion of the bottom fraction from said column, which is rich in polynuclear aromatic compounds, is purged. At least a portion of the bottom fraction obtained from the fractionation section, which is constituted by unconverted products, is recycled to the reaction section.

Hydrogenation of at least one aromatic or polyaromatic compound contained in a hydrocarbon feedstock having a final boiling point below or equal to 650° C., at a temperature of between 30 and 350° C., at a pressure of between 0.1 and 20 MPa, at a hydrogen/(aromatic compounds to be hydrogenated) molar ratio between 0.1 and 10 and at an hourly space velocity HSV of between 0.05 and 50 h.sup.−1, in the presence of a catalyst comprising an alumina support and an active phase comprising nickel, prepared by i) contacting the support with a solution containing a nickel precursor; ii) bringing the support into contact with a solution containing an organic compound comprising a carboxylic acid, or alcohol, or ester, or amide function; iii) drying the impregnated support at a temperature below 250° C.; i) and ii) being carried out separately, in any order, or at the same time.

A hydrocarbon cracker stream is combined with recycle content pyrolysis oil to form a combined cracker stream and the combined cracker stream is cracked in a cracker furnace to provide an olefin-containing effluent. The r-pyoil can be fed to the cracker feed. Alternatively, the r-pyoil with a predominantly c8+ fraction can be fed to the cracker feed. The furnace can be a gas fed furnace, or split cracker furnace.

Embodiments of the disclosure include processes for selective ring-opening of cycloparaffins in hydrocarbon feeds to produce hydrocracked cycloparaffins. In particular, the process comprises contacting a hydrocarbon feed comprising cycloparaffins with hydrogen and a catalyst comprising an unsulfided, low-acidity, metal-containing zeolite under hydrocracking conditions; wherein the metal is selected from the group consisting of platinum, nickel, rhodium and mixtures thereof. The processes are useful for upgrading petroleum streams to lubricant base stocks.