Abstract: A process for producing diluent for use in a hydrocarbon recovery process includes heating a dilbit feed stream comprising hydrocarbons produced from a hydrocarbon reservoir and an added diluent, to a temperature of 350° C. or less, fractionating the dilbit feed stream after heating to produce a light fraction and a heavy fraction, the light fraction comprising the diluent, additional light hydrocarbons, and sour water, separating the sour water from a remainder of the light fraction, and stabilizing the remainder of the light fraction to provide recovered diluent and cooling the recovered diluent. A volume of the recovered diluent is greater than a volume of the added diluent.

Abstract: A process for producing diluent for use in a hydrocarbon recovery process includes heating a dilbit feed stream comprising hydrocarbons produced from a hydrocarbon reservoir and an added diluent, to a temperature of 350° C. or less, fractionating the dilbit feed stream after heating to produce a light fraction and a heavy fraction, the light fraction comprising the diluent, additional light hydrocarbons, and sour water, separating the sour water from a remainder of the light fraction, and stabilizing the remainder of the light fraction to provide recovered diluent and cooling the recovered diluent. A volume of the recovered diluent is greater than a volume of the added diluent.

Abstract: Low vapor pressure hydrocarbon blends are provided, comprising miscible and separable hydrocarbon fractions. A high-octane low-boiling point diluent fraction may be combined with a high-boiling point bitumen fraction. In select embodiments, and the blend may have a viscosity of less than about 350 cSt and a density of less than about 940 kg/m3 over a temperature range of from 7.5° C. to 18.5° C. After transportation, for example by pipeline, the high-octane low-boiling point diluent fraction may be recovered from the blend, and may for example be used as a high-octane gasoline blendstock.

Abstract: Low vapor pressure hydrocarbon blends are provided, comprising miscible and separable hydrocarbon fractions. A high-octane low-boiling point diluent fraction may be combined with a high-boiling point bitumen fraction. In select embodiments, and the blend may have a viscosity of less than about 350 cSt and a density of less than about 940 kg/m3 over a temperature range of from 7.5° C. to 18.5° C. After transportation, for example by pipeline, the high-octane low-boiling point diluent fraction may be recovered from the blend, and may for example be used as a high-octane gasoline blendstock.

Abstract: A process for treating a vacuum gas oil and Diesel feed includes the steps of providing reaction feed containing vacuum gas oil, Diesel and sulfur-containing compounds; providing a stripping gas; providing a washing feed; and mixing the reaction feed, the stripping gas and the washing feed in a stripping and washing zone so as to obtain a gas phase containing the sulfur-containing compounds and a liquid phase substantially free of the sulfur-containing compounds. The washing feed comprises at least one of Diesel, light vacuum gas oil and mixtures thereof produced in the process or added from external source.

Abstract: A process for upgrading a nitrogen and sulfur rich heavy naphtha feedstock includes the steps of providing a naphtha feedstock having an initial nitrogen content, an initial sulfur content and an initial octane number; contacting the naphtha feedstock with an acid source so as to provide a reduced nitrogen feedstock having a reduced nitrogen content which is less than the initial nitrogen content; contacting the reduced nitrogen feedstock with a hydroconversion catalyst system under a hydrogen atmosphere, temperature and pressure so as to provide a final product having a final nitrogen content which is less than the initial nitrogen content, a final sulfur content which is less than the initial sulfur content, and having a final octane number which is substantially equal to or greater than the initial octane number of the feedstock, and wherein the final product has an increased isomerized component and substantially no increase in aromatic content with respect to the feedstock.