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 relates to a process for the production of bio-oil-based renewable streams for composing a diesel or aviation kerosene (AVK) pool by combining the technologies of hydroprocessing esters and fatty acids (HEFA) and thermochemical conversion of lignocellulosic biomass for generating bio-oil. The integration of conventional raw material from the HEFA pathway with a bio-oil fraction has the advantages of the use of a stream originating from the conversion of lignocellulosic material, which is widely available on the market, and also the production of a renewable stream containing aromatics in its composition.

The present invention addresses to a process for the integrated production of H.sub.2 and aviation kerosene from renewable raw materials aiming at reducing CO.sub.2 emissions and consequently bringing benefits to reduce the impact of global warming on the planet. The process involves a hydrotreatment section to obtain n-paraffins followed by a hydroisomerization section to produce isoparaffins. The water and light hydrocarbons obtained in the isoparaffin production process are used for the production of H.sub.2 by the steam reforming process. An alcohol, such as ethanol or glycerin, with less than 6 carbon atoms, is fed into the hydrotreating section to make up the light hydrocarbon stream used in the production of renewable hydrogen.

The invention relates to producing upgraded renewable oil. Renewable crude oil is provided whose oxygen content, water content, and total acid number are within predetermined ranges. Respective fractions of the oil have boiling points below 350° C. and above 450° C. After the oil is pressurized, and hydrogen is added, the mixture is heated and contacted with a heterogeneous catalyst in a first reaction zone with weight based hourly space velocity (WHSV) of 0.1 to 1 h-1. The resultant partially hydrogenated and deoxygenated oil is further heated and contacted with a heterogeneous catalyst in a second reaction zone at WHSV of 0.1 to 1.5 h-1. Low and high boiling point liquid hydrocarbon fractions of the product of the second reaction zone are sent to third and fourth reaction zones, respectively, to be contacted with hydrogen and a heterogeneous catalyst under respective heating conditions and WHSV of 0.1 to 1 h-1.

A process for treating effluent streams in a renewable transportation fuel production process is described. One or more of the sour water stream and an acid gas stream are treated directly in thermal oxidation section. The process allows the elimination or size reduction of a sour water stripper unit, waste water treatment plant, and sulfur recovery unit.

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 an 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.

Catalytic conversion of ketoacids is disclosed, including methods for increasing the molecular weight of ketoacids. An exemplary method includes providing in a reactor a feedstock having at least one ketoacid. The feedstock is then subjected to one or more C—C-coupling reaction(s) in the presence of a catalyst system having a first metal oxide and a second metal oxide.

This disclosure relates to the field of renewable oil compositions and to the use of renewable oil compositions for production of hydrocarbon compositions, which can be used for traffic fuels and other solutions. An exemplary composition contains free fatty acids and triglycerides, in a concentration of free fatty acids from 15 wt-% to 80 wt-% and a remainder being predominantly triglycerides. A method for producing hydrocarbons from a renewable oil feedstock, in which the feedstock which contains free fatty acids from 15 wt-% to 80 wt-%, and a remainder being predominantly triglycerides, is subjected to a pretreatment process followed by a hydrotreatment process for obtaining hydrocarbons.

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 unstaurations 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 present technology relates to hydrocarbon fuels comprising renewable content. More particularly, the technology relates to manufacture of renewable diesel for potential use as aviation turbine fuel blendstock.