The present invention relates to a process for the conversion of plant oils, animal fats, waste food oils and carboxylic acids into renewable liquid fuels, such as bio-naphtha, bioQAV and renewable diesel, for use in combination with fossil fuels. The process is composed of two steps: hydrotreatment and hydrocracking. The effluent from the hydrotreatment step contains aromatics, olefins and compounds resulting from the polymerization of esters and acids. This is due to the use of partially reduced catalysts without the injection of a sulfiding agent and allows for the production of bioQAV of suitable quality for use in combination with fossil kerosene. Concurrently, the process generates, in addition to products in the distillation range of naphtha, kerosene and diesel, high molecular weight linear paraffins (up to 40 carbon atoms).

The present invention provides a process for producing one or more of hydrocarbon products from a renewable feedstock comprising triglycerides, free fatty acids or combinations thereof. The process may comprise the steps of mixing the renewable feedstock with a diluent to form a diluted feedstock; supplying or providing hydrogen gas to the diluted feedstock so that the hydrogen gas may dissolve in the diluted feedstock to form a diluted feedstock enriched with dissolved hydrogen; and feeding the diluted feedstock enriched with dissolved hydrogen to at least a reactor having at least a reaction zone comprising at least a catalyst bed under predefined conditions, thereby producing a reaction effluent which can be further processed (e.g. by using one or more distillation units and one or more adsorption units) to form one or more of hydrocarbon products.

The present invention relates to a process and system for forming a hydrocarbon feedstock from a biomass material, and the hydrocarbon feedstock formed therefrom. The present invention also relates to a process and system for forming a bio-derived naphtha fuel from a hydrocarbon feedstock, and the bio-derived naphtha fuel formed therefrom, as well as intermediate treated hydrocarbon feedstocks formed during the process.

Hydrodeoxygenating a biorenewable feed that is concentrated in free fatty acids with 10-13 carbon atoms at a moderate hydrodeoxygenation ratio that is less than the ratio of hydrodeoxygenation utilized for traditional biorenewable feeds such as vegetable oil or even mineral feedstocks, normal paraffins in the range desired by the detergents industry can be produced. Either hydroisomerization or an iso-normal separation can be performed to provide green fuel streams. Two reactors are proposed, one for hydrodeoxygenation of the biorenewable feed that is concentrated in free fatty acids with 10-13 carbon atoms and the other for a traditional biorenewable feed or even a mineral feed operated at a higher deoxygenation ratio.

A hydrodeoxygenation catalyst takes self-made porous large-specific surface nano-alumina as a carrier, takes Ni.sub.xMoW, Ni.sub.xCoW or Ni.sub.xCoMo as an active component, and takes Mn as an assistant. Hydrothermal stability of the catalyst and dispersion of active components may be increased by enlarging a pore channel and a specific surface area of the carrier, thereby prolonging the life of the hydrodeoxygenation catalyst. A hydroisomerization catalyst takes multi-walled carbon nanotube composite hierarchical-pore-channel NiAPO-11 or NiSAPO-11 as a carrier and takes Ni.sub.xMoLa, Ni.sub.xCoLa or Ni.sub.xWLa as an active component. Due to the adding of the carbon nanotubes, the pore channel of the carrier is enriched, and connection between the active components and the carrier is effectively enhanced, thereby prolonging the life of the catalyst on a basis of increasing selectivity of aviation kerosene component. Moreover, the biological aviation kerosene satisfying usage conditions is prepared by virtue of mild reaction conditions.

Hydrodeoxygenating a biorenewable feed that is concentrated in free fatty acids with 12 and 14 carbon atoms at a moderate hydrodeoxygenation ratio that is less than the ratio of hydrodeoxygenation utilized for traditional biorenewable feeds such as vegetable oil or even mineral feedstocks, normal paraffins in the range desired by the detergents industry can be produced. Either hydroisomerization or an iso-normal separation can be performed to provide green fuel streams. Two reactors are proposed, one for hydrodeoxygenation of the biorenewable feed that is concentrated in free fatty acids with 12 and 14 carbon atoms and the other for a traditional biorenewable feed or even a mineral feed operated at a higher deoxygenation ratio.

The invention relates to a process for hydrotreating a liquid oil stream such as pyrolysis oil stream by, in continuous operation, reacting the liquid oil stream with hydrogen in the presence of a nickel-molybdenum (NiMo) based catalyst at a temperature of 20-240? C., a pressure of 100-200 barg and a liquid hourly space velocity (LHSV) of 0.1-1.1 h.sup.?1, and a hydrogen to liquid oil ratio, defined as the volume ratio of hydrogen to the flow of the liquid oil stream, of 1000-6000 NL/L thereby forming a stabilized liquid oil stream.

The present invention discloses a catalytic process for the manufacture of hydrogen and hydrocarbons simultaneously in the same reactor from renewable source, i.e. lipids, glycerides and fatty acids from plant, animal or algae oil, where in the multiple unsaturations in the renewable feedstock and the catalytic intermediates produced in the process from renewable feedstock is converted catalytically using simultaneous combination of in-situ occurring reactions. These in-situ occurring reactions are simultaneous combination of hydroconversion, reforming and water gas shift reactions wherein the reaction is performed in the presence of one or more metal sulfides form of metals of Group VI and/or Group IX and/or Group X elements, specifically comprises of one or more active metal combinations such as Co, W, Mo, Ni, P, with Pt, Pd encapsulated inside sodalite cages for prevention against poisoning from sulfur based compounds. The hydroconversion comprises of reactions in presence of hydrogen such as hydrocracking, dehydrogenation, dehydrocyclization, hydrodeoxygenation, hydrodesulfurization, hydrodenitrogenation, decarboxylation, decarbonylation, cyclization and aromatization reactions. The catalyst along with the active metals also includes porous silica-alumina, zeolite, silica, alumina, silicoaluminophosphates or a combination of two or more thereof used as support for the above said process. These catalysts are loaded in a graded beds (two or more beds of different catalyst mixtures) or simultaneously (mixture of different catalyst systems) and reacted specifically at lower temperatures than the steam reforming conditions i.e. at pressure from 10 to 150 atmosphere, average temperature of the catalytic bed from 250 C. to 500 C., space-velocity of from 0.5 h.sup.1 to 8 h.sup.1, and hydrogen to feed ratio of from 300 NL of hydrogen/L of feed to 3500 NL hydrogen/L of feed. Initially hydrogen gas is supplied for conversion of the renewable feed stocks, as the reaction process the hydrogen consumed during the conversion of plant, animal or algae oil into hydrocarbons is balanced from the in-situ reactions such as reforming, dehydrogenation, water gas shift etc occurring during the same process. This production of hydrogen makes the entire process refinery independent and more economical and sustainable. Along with hydrogen the renewable feed stock is also converted into hydrocarbons ranging between C1-C24 carbon number, comprising of n-paraffins, isoparaffins, cyclo paraffins, naphthenes, and aromatics and polynuclear aromatics.

The use of bio oil from at least one renewable source in a hydrotreatment process, in which process hydrocarbons are formed from said glyceride oil in a catalytic reaction, and the iron content of said bio oil is less than 1 w-ppm calculated as elemental iron. A bio oil intermediate including bio oil from at least one renewable source and the iron content of said bio oil is less than 1 w-ppm calculated as elemental iron.

The present application 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 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.