The present disclosure relates to processes that catalytically convert a hydrocarbon feed stream predominantly comprising both isopentane and n-pentane to yield upgraded hydrocarbon products that are suitable for use either as a blend component of liquid transportation fuels or as an intermediate in the production of other value-added chemicals. The hydrocarbon feed stream is isomerized in a first reaction zone to convert at least a portion of the n-pentane to isopentane, followed by catalytic-activation of the isomerization effluent in a second reaction zone with an activation catalyst to produce an activation effluent. The process increases the conversion of the hydrocarbon feed stream to olefins and aromatics, while minimizing the production of C1-C4 light paraffins. Certain embodiments provide for further upgrading of at least a portion of the activation effluent by either oligomerization or alkylation.

A method of hydroprocessing is performed wherein non-petroleum feedstocks, such as those containing from about 10% or more olefinic compounds or heteroatom contaminants by weight, are treated in a first reaction zone to provide reaction products. The process involves introducing the feedstock along with diluents or a recycle and hydrogen in a first reaction zone and allowing the feed and hydrogen to react in a liquid phase within the first reaction zone to produce reaction products. The reaction products are cooled and/or water is removed from the reaction products. At least a portion of the cooled and/or separated reaction product are introduced as a feed along with hydrogen into a second reaction zone containing a hydroprocessing catalyst. The feed and hydrogen are allowed to react in a liquid phase within the second reaction zone to produce a second-reaction-zone reaction product.

Methods and systems for mixing a catalyst precursor with a heavy oil feedstock preparatory to hydroprocessing the heavy oil feedstock in a reactor to form an upgraded feedstock. Achieving very good dispersion of the catalyst precursor facilitates and maximizes the advantages of the colloidal or molecular hydroprocessing catalyst. A catalyst precursor and a heavy oil feedstock having a viscosity greater than the viscosity of the catalyst precursor are provided. The catalyst precursor is pre-mixed with a hydrocarbon oil diluent, forming a diluted catalyst precursor. The diluted precursor is then mixed with at least a portion of the heavy oil feedstock so as to form a catalyst precursor-heavy oil feedstock mixture. Finally, the catalyst precursor-heavy oil feedstock mixture is mixed with any remainder of the heavy oil feedstock, resulting in the catalyst precursor being homogeneously dispersed on a colloidal and/or molecular level within the heavy oil feedstock.

A method for recalculating the solvent power of a light oil, SP.sub.(LO recalculated), is provided. The method comprises: titrating the light oil against a reference oil, optionally in the presence of a titrant, to determine a volume fraction of the light oil at the onset of asphaltene precipitation, V.sub.(onset fraction LO), a volume fraction of the reference oil at the onset of asphaltene precipitation, V.sub.(onset fraction RO), and, where a titrant is present, a volume fraction of the titrant at the onset of asphaltene precipitation, V.sub.(onset fraction T), and determining the recalculated solvent power of the light oil, SP.sub.(LO recalculated), according to the following formula:

[00001]${\mathrm{SP}}_{\left(\mathrm{LO}.Math..Math.\mathrm{recalculated}\right)}=\frac{\left({\mathrm{CSP}}_{\left(\mathrm{RO}\right)}-{\mathrm{SP}}_{\left(\mathrm{RO}\right)}*V_{\left(\mathrm{onset}.Math..Math.\mathrm{fraction}.Math..Math.\mathrm{RO}\right)}-x*{\mathrm{SP}}_{\left(T\right)}*V_{\left(\mathrm{onset}.Math..Math.\mathrm{fraction}.Math..Math.T\right)}\right)}{V_{\left(\mathrm{onset}.Math..Math.\mathrm{fraction}.Math..Math.\mathrm{LO}\right)}}$

wherein: CSP.sub.(RO) is the critical solvent power of the reference oil, SP.sub.(RO) is the solvent power of the reference oil, SP.sub.(T) is the solvent power of the titrant, and x is 1 where a titrant is present, and otherwise is 0.

The recalculated solvent power may be used in methods for preventing asphaltene precipitation during processing of crude oils in a refinery.

A method for processing bitumen froth comprised of bitumen, water containing chlorides and solids is provided for producing a final diluted bitumen product having reduced chlorides. In particular, fine water droplets containing chlorides that are present in raw diluted bitumen are captured by washing the raw diluted bitumen with low salinity water to produce the final diluted bitumen product having reduced chlorides.

A method for processing bitumen froth comprised of bitumen, water and solids to produce a final diluted bitumen product having a reduced water content is provided whereby demulsifier is added to the bitumen froth after a first separation stage and prior to a second separation stage to produce the final diluted bitumen product having reduced water content.

Processes and systems for stabilization and subsequent hydrogenation of an immiscible olefin are described. In certain embodiments, the hydrogenation is conducted in a fixed bed reactor in presence of a hydrogenation catalyst.

A multi-stage process is described for upgrading pyrolysis tar, such as steam cracker tar, by hydroprocessing in at least two stages. Hydroprocessing in a first stage is performed in the presence of a utility fluid. The utility fluid has a boiling point distribution from about 120 C. to about 480 C. and is separated from the first stage product.

A multi-stage process for upgrading tars is provided. A predominantly hydrotreating stage can be applied before a cracking stage, which can be a hydrocracking or a thermal cracking stage. Alternatively, a predominantly cracking stage, which can be a hydrocracking or a thermal cracking stage, can be applied before a hydrotreating stage. Apparatus suitable for performing the method is also provided.

The invention relates to a process for the manufacture of diesel range hydrocarbons wherein a feed is hydrotreated in a hydrotreating step and isomerised in an isomerisation step, and a feed comprising fresh feed containing more than 5 wt % of free fatty acids and at least one diluting agent is hydrotreated at a reaction temperature of 200-400 C., in a hydrotreating reactor in the presence of catalyst, and the ratio of the diluting agent/fresh feed is 5-30:1.