The invention relates to a process for the recovery of aliphatic hydrocarbons from a liquid stream comprising aliphatic hydrocarbons, heteroatom containing organic compounds and optionally aromatic hydrocarbons, involving a) liquid-liquid extraction of said liquid stream with an extraction solvent; b) mixing the extract stream, comprising extraction solvent, heteroatom containing organic compounds and optionally aromatic hydrocarbons, with a demixing solvent to remove part of the heteroatom containing organic compounds and optional aromatic hydrocarbons; and c) separation of the remaining stream into a demixing solvent stream and an extraction solvent stream, wherein before and/or after step c) additional heteroatom containing organic compounds and optional aromatic hydrocarbons are removed from that remaining stream and/or from a stream resulting from step c), respectively, by contacting the latter stream (s) with a sorption agent. Further, the invention relates to a process for the recovery of aliphatic hydrocarbons from plastics comprising the above-mentioned process; and to a process for steam cracking a hydrocarbon feed comprising aliphatic hydrocarbons as recovered in one of the above-mentioned processes.

The invention relates to a process for the recovery of aliphatic hydrocarbons from a liquid stream comprising aliphatic hydrocarbons, heteroatom containing organic compounds and optionally aromatic hydrocarbons, involving a) liquid-liquid extraction of said liquid stream with an extraction solvent; b) mixing the extract stream, comprising extraction solvent, heteroatom containing organic compounds and optionally aromatic hydrocarbons, with a demixing solvent to remove part of the heteroatom containing organic compounds and optional aromatic hydrocarbons; and c) separation of the remaining stream into a demixing solvent stream and an extraction solvent stream, wherein before and/or after step c) additional heteroatom containing organic compounds and optional aromatic hydrocarbons are removed from that remaining stream and/or from a stream resulting from step c), respectively, by contacting the latter stream (s) with a sorption agent. Further, the invention relates to a process for the recovery of aliphatic hydrocarbons from plastics comprising the above-mentioned process; and to a process for steam cracking a hydrocarbon feed comprising aliphatic hydrocarbons as recovered in one of the above-mentioned processes.

Described is a novel process for disaggregating biomass pyrolysis oil quantitatively into energy dense hydrophobic aromatic fraction (HAF), fermentable pyrolytic sugars and phenolics based products in a highly economical and energy efficient manner. Phase separation of the esterified pyrolysis oil after an oxidative pre-treatment and the quantitative recovery of the separate fractions is described. Phase separation uses batch as well as continuous reactor systems. The resulting HAF is an energy dense, thermally stable, water free, non-corrosive to carbon steel, and is a free flowing liquid suitable for combustion and for upgrading to transportation fuels. Pyrolytic sugars which are mainly anhydrosugars can be further converted by fermentation to ethanol or other products. Monomeric phenols are useful industrial intermediates and the organic acids in the original pyrolysis oil are mainly recovered as esters of the separation solvents.

Provided are a mineral base oil satisfying the following requirements (I) to (IV), which is excellent in safety and environmental aspects and has good compatibility with resin; a molded article formed of a resin composition containing the mineral base oil and a resin; and a method for producing the mineral base oil. Requirement (I): The flash point is 200° C. or higher. Requirement (II): The pour point is 0° C. or lower. Requirement (III); The aromatic content (% C.sub.A) is 2.6 or more. Requirement (IV): The toluene content, as measured according to JIS A1965:2015, is more than 0 μg/m.sup.3 and less than 500 μg/m.sup.3.

Provided are a mineral base oil satisfying the following requirements (I) to (IV), which is excellent in safety and environmental aspects and has good compatibility with resin; a molded article formed of a resin composition containing the mineral base oil and a resin; and a method for producing the mineral base oil. Requirement (I): The flash point is 200° C. or higher. Requirement (II): The pour point is 0° C. or lower. Requirement (III); The aromatic content (% C.sub.A) is 2.6 or more. Requirement (IV): The toluene content, as measured according to JIS A1965:2015, is more than 0 μg/m.sup.3 and less than 500 μg/m.sup.3.

The methods described herein produce a naphthenic process oil, as classified by ASTM D-2226, containing 35-65% saturates and 35-65% aromatics as determined by ASTM D-2007. The produced naphthenic process oil also contains polyaromatic hydrocarbons (PAH), more specifically the EU/US EPA 8-regulated PAHs, less than 10 ppm. The naphthenic process oil is produced by first feeding gas oil ranging in viscosities up to 20 cSt at 100° C. through counter-current liquid-liquid extraction towers with a solvent having a selective affinity for aromatics. The extract is then cooled and either continuously processed through a coalescing separator or batch processed in a tank or decanter to produce a second raffinate, which can be further distilled to produce the naphthenic process oil.

The methods described herein produce a naphthenic process oil, as classified by ASTM D-2226, containing 35-65% saturates and 35-65% aromatics as determined by ASTM D-2007. The produced naphthenic process oil also contains polyaromatic hydrocarbons (PAH), more specifically the EU/US EPA 8-regulated PAHs, less than 10 ppm. The naphthenic process oil is produced by first feeding gas oil ranging in viscosities up to 20 cSt at 100° C. through counter-current liquid-liquid extraction towers with a solvent having a selective affinity for aromatics. The extract is then cooled and either continuously processed through a coalescing separator or batch processed in a tank or decanter to produce a second raffinate, which can be further distilled to produce the naphthenic process oil.

Metals, such as mercury, may be removed from aqueous, hydrocarbon, or mixed oilfield or refinery fluids by: applying a sulfur compound having the general formula HS—X, where X is a heteroatom substituted alkyl, cycloalkyl, aryl, and/or alkylaryl group either alone or in combination with or as a blend with at least one demulsifier, a buffering agent, a pour point depressant, and/or a water clarifier to chelate the at least one metal and form a chelate complex of the sulfur compound with the at least one metal and then separating the chelate complex from the fluid.

Metals, such as mercury, may be removed from aqueous, hydrocarbon, or mixed oilfield or refinery fluids by: applying a sulfur compound having the general formula HS—X, where X is a heteroatom substituted alkyl, cycloalkyl, aryl, and/or alkylaryl group either alone or in combination with or as a blend with at least one demulsifier, a buffering agent, a pour point depressant, and/or a water clarifier to chelate the at least one metal and form a chelate complex of the sulfur compound with the at least one metal and then separating the chelate complex from the fluid.

Methods are provided for processing deasphalted gas oils derived from thermally cracked resid fractions to form Group I, Group II, and/or Group III lubricant base oils. The yield of lubricant base oils (optionally also referred to as base stocks) can be increased by thermally cracking a resid fraction at an intermediate level of single pass severity relative to conventional methods. By performing thermal cracking to a partial level of conversion, compounds within a resid fraction that are beneficial for increasing both the viscosity and the viscosity index of a lubricant base oil can be retained, thus allowing for an improved yield of higher viscosity lubricant base oils from a thermally cracked resid fraction.