A non-aqueous extraction (NAE) process for producing bitumen from oil sands ore can include a multistage bitumen extraction step where paraffinic solvent and deasphalted oil are added at a downstream stage of extraction at solvent-to-bitumen ratios below asphaltene precipitation onset threshold to remove bitumen from the solid mineral material, while the ore is added to a first stage to mix with the solvent-bitumen mixture and produce solvent diluted bitumen. The process includes recovering the solvent diluted bitumen and the solvent diluted tailings from the extraction step. The solvent diluted bitumen is subjected to deasphalting to produce solvent diluted deasphalted bitumen that is used as a source of the paraffinic solvent and deasphalted oil supplied to extraction. The tailings and asphaltene fraction from deasphalting can be subjected to washing and the washed material can then be subjected to sand solvent recovery. The NAE process can be operated within an operating envelop for effective and efficient performance.

The present disclosure relates to methods for producing renewable base oil and other valuable renewable fuel components from a feedstock of biological origin comprising free fatty acids and glycerides. The feedstock is first separated to two or more effluent streams containing a fatty acid fraction and glyceride fraction. The glycerides are hydrolyzed to free fatty acids and glycerol, and the fatty acids thus obtained are recycled to the separating. The fatty acids are then converted to the base oil by ketonisation, hydrodeoxygenation and hydroisomerisation. The glycerol is converted to propanols by selective hydrogenolysis.

A method for steam cracking of a hydrocarbon feed is disclosed. The method can include heating a hydrocarbon feed stream with a first quench water stream to form a heated hydrocarbon feed stream and a second quench water stream having a temperature lower than the first quench water stream, steam cracking the heated hydrocarbon feed stream to form a cracked stream comprising cracked gases, contacting the cracked stream with a quench water to form a gaseous stream comprising quenched cracked gases and a crude water stream comprising heated quench water and pyrolysis gasoline, and separating the crude water stream to form the first quench water stream.

The present disclosure relates to methods for preparing aviation fuel component from a feedstock containing fossil hydrotreating feed and a second feed containing esters of fatty acids and rosins, free fatty acids and resin acids. The method includes subjecting the feedstock to hydrotreatment reaction conditions to produce a hydrotreated stream, separating the hydrotreated stream to three fractions from which at least part the highest boiling fraction is subjected to hydrocracking reaction to produce a hydrocracked stream. At least part of the hydrocracked stream is admixed with at least part of the hydrotreated stream, and their admixture is processed further until desired conversion of the feedstock to the aviation fuel component is obtained.

A process for the removal of residual sulfur compounds from rich liquid caustic is disclosed where a single column containing two reaction zones catalytically oxidizes mercaptans to disulfide oils. The second reaction zone utilizes a bundle of vertical hanging fibers and is maintained as a gas continuous phase comprising from about 20% to about 100% by volume vapor. This process is especially useful as part of a hydrocarbon desulfurization process flow scheme.

The present disclosure relates to the thermal liquefaction of lignin, and more particularly to lignin solvolysis of a lignin feedstock chosen based on its molecular weight. The process comprises subjecting a feed mixture (30) of lignin feedstock (10) and solvent (20) to a thermal liquefaction step by heating (110) the feed mixture (30) at a temperature between 360 and 420 ° C., separating (120) a liquid product mix (50) from a product mix (40); and recirculating at least part of said liquid product mix (50) as an oil fraction of said solvent (20).

Provided is a hydrotreating step (A) containing a hydroisomerization step (A1) that obtains a hydroisomerized oil (a1) by bringing a FT synthesis oil into contact with a hydroisomerization catalyst and/or a hydrocracking step (A2) that obtains a hydrocracked oil (a2) by bringing it into contact with a hydrocracking catalyst, and a fractionation step (B) that transfers at least a portion of the hydrotreated oil (a) composed of the hydroisomerized oil (a1) and/or the hydrocracked oil (a2) to a fractionator and, at the very least, obtains a middle distillate (b1) with a 5% distillation point of 130 to 170° C. and a 95% distillation point of 240 to 300° C., and a heavy oil (b2) that is heavier than the middle distillate (b1).

Disclosed is a method for maximizing ethylene or propene production, the main steps thereof being: taking crude oil and distillate thereof, pre-processing urban mixed-waste plastics as raw material, then entering same into a catalytic cracking reactor, removing via a two-stage pre-wash tower and related separation, then cooling the reacted high-temperature oil and gas and removing impurities to obtain light and heavy distillate oils; performing a hydrogenation reaction operation on the heavy distillate oil; performing light distillate oil separation, performing a recombination operation on its olefins, its alkanes entering a steam cracking apparatus to produce rich ethylene, and its aromatic components being separated as by-products; the product of the described hydrogenation and recombination reaction and the steam-cracked distillate oil is recycled to the catalytic cracking reactor. In the production method of the present invention, the yield of ethylene and propene together is 45-75 m % of the raw material, and the yield of aromatics is 15-30 m % of the raw material; in particular, when using urban mixed-waste plastics as raw material, the ethylene or propene thus produced are used to produce new plastics by way of a conventional polymerization process, achieving the chemical recycling of waste plastics.

A process for the production of ultralow aromatic specialty distillate from different refinery streams particularly high sulfur streams. The process produces de-aromatized distillates with benzene content below 1 ppmw. Hydrocarbon feedstock having boiling temperature in the range of 90 and 350° C., preferably 140 and 320° C. The hydrocarbon feedstocks are obtained from any petroleum-refinery or bio-refinery or any other source producing hydrocarbon streams.

A new catalyst hydroisomerizes C18 paraffins from fatty acids to a high degree to produce a composition with acceptable freeze point which retains 18 carbon atoms in the hydrocarbon molecule for jet fuel. We have discovered a fuel composition comprising at least 14 wt % hydrocarbon molecules having at least 18 carbon atoms and a freeze point not higher than −40° C. The composition also may exhibit a exhibiting a final boiling point of no more than 300° C. The hydroisomerization process can be once through or a portion of the product diesel stream may be selectively hydrocracked or recycled to hydroisomerization to obtain a fuel composition that meets jet fuel specifications.