The present disclosure relates to a process for the production of bio-oil which involves heating a mixture of a biomass slurry and a first catalyst composition at a temperature ranging from 200 to 350 C. and at a pressure ranging from 70 to 250 bars to obtain a mass containing crude bio oil, a residue and the catalyst; separating the crude bio oil from said mass to obtain a separated crude bio oil; extracting said separated crude bio oil with at least one solvent and evaporating said solvent to obtain a solvent free crude bio oil; subjecting said solvent free crude bio oil to reduction in the presence of a second catalyst composition and hydrogen source at temperature and pressure conditions similar to those employed for the conversion of bio mass into crude bio oil to obtain bio-oil. The second catalyst composition is the same as that of the first catalyst composition. The process also comprises a method step of recovering the first catalyst and reusing it either for preparing crude bio oil or bio oil or both.

The present application provides a composition comprising 8-30 mass % of C.sub.4-12 linear alkanes, 5-50 mass % of .sub.C4-12 branched alkanes, 25-60 mass % of C.sub.5-12 cycloalkanes, 1-25 mass of C.sub.6-12 aromatic hydrocarbons, no more than 1 mass% of alkenes, and no more than 0.5 mass % in total of oxygen-containing compounds; wherein the total amount of C.sub.4-12 alkanes is 40-80 mass %, and the total amount of C.sub.4-12 alkanes, C.sub.5-12 cycloalkanes and C.sub.6-12 aromatic hydrocarbons is at least 95 mass %; and wherein the amounts are based on the mass of the composition. Also described is a method for producing the composition comprising the step of hydroprocessing a biological feedstock using a catalyst and the step of fractionating the product of the hydroprocessing step.

The present invention provides a composition comprising 8-30 mass % of C.sub.4-12 linear alkanes, 5-50 mass % of C.sub.4-12 branched alkanes, 25-60 mass % of C.sub.5-12 cycloalkanes, 1-25 mass of C.sub.6-12 aromatic hydrocarbons, no more than 1 mass % of alkenes, and no more than 0.5 mass % in total of oxygen-containing compounds; wherein the total amount of C.sub.4-12 alkanes is 40-80 mass %, and the total amount of C.sub.4-12 alkanes, C.sub.5-12 cycloalkanes and C.sub.6-12 aromatic hydrocarbons is at least 95 mass %; and wherein the amounts are based on the mass of the composition. Also provided is a method for producing the composition comprising the step of hydroprocessing a biological feedstock using a catalyst and the step of fractionating the product of the hydroprocessing step.

The present application relates to a process for production of hydrocarbons comprising the steps of converting a feed stream comprising alcohols, ethers or mixtures hereof over a metal-containing zeolite based catalyst, active in dehydrogenation of hydrocarbons, in a conversion step thereby obtaining a conversion effluent, separating said effluent to obtain art aqueous process condensate stream, a liquid hydrocarbon stream and a gaseous stream, removing part of the hydrogen formed in the conversion step, and recycling at least part of the gaseous and/or liquid hydrocarbon stream to the conversion step.

A process for hydrotreating a renewable feedstock with improved carbon monoxide management is disclosed. A mixture of renewable feedstock and hydrocarbon feedstock is treated in a hydrotreating reactor to produce a hydrotreated effluent stream and contacting the hydrotreated effluent stream with a water gas shift catalyst bed to produce a shift reactor effluent stream. The shift reactor effluent stream is passed to a cold separator to recover a cold vapor stream and recycling the cold vapor stream having reduced concentration of carbon monoxide to the hydrotreating zone. The subject matter disclosed provides an improved process and apparatus to reduce the accumulation of CO by converting CO present in the hydrotreated effluent stream to CO.sub.2 using the water shift gas reaction.

The present invention relates to a method for producing renewable aviation fuel D or components thereto from renewable feedstock A comprising separate hydrodeoxygenation (20) hydroisomerization step (40), wherein the hydroisomerization is catalysed by metal impregnated hierarchical zeolite catalyst.

In alternative embodiments, provided processes for the integration of hydrolysis of renewable glycerides for the subsequent generation of paraffins (or a mixture of saturated hydrocarbons, or a mixture of alkanes containing around 80% to 90% linear chains (n-paraffin) with about 20 to 30 carbons in length) and propylene glycol. In alternative embodiments, provided is an improved and integrated process for producing paraffins and propylene glycol from renewable feedstocks comprising first subjecting renewable glycerides to a hydrolysis process step to generate free fatty acids (FFAs) and glycerol. The generated FFAs are suitable for use in a hydro-processing step to produce products suitable for use as transportation fuels, and the generated glycerol can be used in a hydrogenolysis step for producing propylene glycol.

Methods and reactor systems for conversion of bio-oils into renewable diesel, jet fuel, and gasoline. Phosphorus and metals containing feedstock is subjected to hydrodeoxygenation in a reactor comprising a solid catalyst suspended in a heavy oil.

Disclosed is a process for converting lower linear and branched mono-olefins, derived from C.sub.2-C.sub.5 bio-based alcohols to higher hydrocarbons, to one or more C.sub.8-C.sub.24 hydrocarbons. Certain embodiments provide a process for oligomerization of branched and/or linear C.sub.3-C.sub.8 olefins to renewable diesel fuel and/or jet fuel in overall yields of at least 70% in the presence of tungstated -alumina or tungstated silica catalysts admixed with ZSM-5 type zeolites.

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.