The present invention provides a process for producing liquid hydrocarbon products from solid biomass and/or residual waste feedstocks, said process comprising the steps of: a) a first stage of hydropyrolysing the solid feedstock in a hydropyrolysis reactor vessel in the presence of molecular hydrogen and one or more deoxygenation catalysts, producing a product stream comprising partially deoxygenated hydropyrolysis product, H.sub.2O, H.sub.2, CO.sub.2, CO, C.sub.1-C.sub.3 gases, char and catalyst fines; b) removing said char and catalyst fines from said product stream; c) a second stage of hydroconverting said partially deoxygenated hydropyrolysis product in a hydroconversion reactor vessel in the presence of one or more hydroconversion catalysts and of the H.sub.2O, CO.sub.2, CO, H.sub.2, and C.sub.1-C.sub.3 gas generated in step a), producing a vapour phase product comprising substantially fully deoxygenated hydrocarbon product, H.sub.2O, CO, CO.sub.2, and C.sub.1-C.sub.3 gases; d) condensing the vapour phase product of step d) to provide a liquid phase product comprising substantially fully deoxygenated C4+ hydrocarbon liquid and aqueous material and separating said liquid phase product from a gas phase product comprising H.sub.2, CO, CO.sub.2, and C.sub.1-C.sub.3 gases; e) removing the aqueous material from the substantially fully deoxygenated C4+ hydrocarbon liquid; and f) a third stage comprising combining an aliphatic hydrocarbon precursor or an aromatic hydrocarbon precursor with at least a portion of the substantially fully deoxygenated C4+ hydrocarbon liquid and co-processing the resultant liquid in a hydroprocessing reactor vessel in the presence of hydrogen and one or more hydroprocessing catalysts.

A process the production of a crude liquid lignin oil (CLO), the process includes the steps of providing a lignin-rich solid feedstock and subjecting the lignin-rich solid feedstock to a treatment in a polar organic solvent in the absence of an effective amount of added reaction promoter, such as a heterogeneous and/or homogeneous catalyst and/or hydrogen, and providing a lignin composition, the treatment includes a step of contacting the lignin-rich solid feedstock with a polar organic solvent under operating conditions of an operating temperature up to 210 C., an operating pressure lower than 50 bar and a residence time up to 240 minutes, wherein the ratio (w/v) of lignin (in lignin-rich feedstock) to polar organic solvent ranges between 1:1.5 and 1:15, or between 1:2 and 1:10 or between 1:2 and 1:5.

The present invention provides a catalytic fast pyrolysis process for the production of fuel blendstocks and chemicals. In addition, the invention provides compositions of renewable blendstocks, compositions of renewable fuel blends, and compositions of 100 percent renewable fuels compatible with gasoline specifications and regulations.

The present invention relates generally to the generation of bio-products from organic matter feedstocks. More specifically, the present invention relates to improved methods for the hydrothermal/thermochemical conversion of lignocellulosic and/or fossilised organic feedstocks into biofuels (e.g. bio-oils) and/or chemical products (e.g. platform chemicals).

A method of making a multifunctional catalyst for upgrading pyrolysis oil includes contacting a zeolite support with a solution including at least a first metal catalyst precursor and a second metal catalyst precursor, the first metal catalyst precursor, the second metal catalyst precursor, or both, including a heteropolyacid. Contacting the zeolite support with the solution deposits or adsorbs the first metal catalyst precursor and the second catalyst precursor onto outer surfaces and pore surfaces of the zeolite support to produce a multifunctional catalyst precursor. The method further includes removing excess solution from the multifunctional catalyst precursor and calcining the multifunctional catalyst precursor to produce the multifunctional catalyst comprising at least a first metal catalyst and a second metal catalyst deposited on the outer surfaces and pore surfaces of the zeolite support.

A method for thermal processing and catalytic cracking of a biomass to effect distillate oil recovery can include, particle size reduction. slurrying the biomass with a carrier fluid to create a reaction mixture, slurrying a catalyst with a carrier fluid to create a catalyst slurry, heating the reaction mixture and/or the catalyst slurry, and depolymerizing the reaction mixture with the catalyst. The reaction mixture can undergo distillation and fractionation to produce distillate fractions that include naphtha, kerosene, and diesel. In some embodiments, thermal processing and catalytic cracking includes vaporization of the biomass followed by distillation and fractionation. In some embodiments, a resulting distillate can be used as a carrier fluid. In some embodiments, the method can include desulfurization, dehydration, and/or decontamination.

A process for processing mixed plastics comprising simultaneous pyrolysis and dechlorination of the mixed plastics, the process comprising contacting the mixed plastics with a zeolitic catalyst in a pyrolysis unit to produce a hydrocarbon product comprising a gas phase and a liquid phase; and separating the hydrocarbon product into a hydrocarbon gas stream and a hydrocarbon liquid stream, wherein the hydrocarbon gas stream comprises at least a portion of the gas phase of the hydrocarbon product, wherein the hydrocarbon liquid stream comprises at least a portion of the liquid phase of the hydrocarbon product, wherein the hydrocarbon liquid stream comprises one or more chloride compounds in an amount of less than about 100 ppmw chloride, based on the total weight of the hydrocarbon liquid stream, and wherein the hydrocarbon liquid stream is characterized by a viscosity of less than about 400 cP at a temperature of 300 C.

The present invention provides a composition for biomass oil, and a preparation method and use thereof. The composition comprises a biomass and a liquid oil, wherein, based on weight of the biomass, the biomass has a moisture content of 3 wt % to 18 wt %. The biomass is mixed with the liquid oil to obtain a liquid mixture, i.e., the composition for biomass oil. According to the use of the composition for biomass oil in preparation of biomass oil, high-pressure high-temperature hydrolysis is carried out by using water in the biomass, and the polycondensation of coke is avoided under the co-action of hydrogen gas and a catalyst, so that the yield of the coke is lowered, and the yield of the biomass oil is increased.

This disclosure provides a process based on hydrothermal liquefaction (HTL) treatment for co-processing of high-water-content wastewater sludge and other lignocellulosic biomass for co-production of biogas and bio-crude oil. The mixture of waste activated sludge and lignocellulosic biomass such as birchwood sawdust/cornstalk/MSW was converted under HTL conditions in presence of KOH as the homogeneous catalyst. The operating conditions including reaction temperature, reaction time and solids concentration were optimized based on the response surface methodology for the maximum bio-crude oil production. The highest bio-crude oil yield of around 34 wt % was obtained by co-feeding waste activated sludge with lignocellulosic biomass at an optimum temperature of 310 C., reaction time of 10 min, and solids concentration of 10 wt %. The two by-products from this process (bio-char and water-soluble products) can be used to produce energy as well. Water-soluble products were used to produce biogas through Bio-methane Potential Test (BMP) and were found to produce around 800 mL bio-methane cumulatively in 30 days per 0.816 g of total organic carbon (TOC) or 2.09 g of chemical oxygen demand (COD) of water-soluble products.

A process for the preparation of aromatic compounds from a feed stream containing biomass or mixtures of biomass, the process comprising: a) subjecting a feed stream containing biomass or mixtures of biomass to a process to afford a conversion product comprising aromatic compounds; b) recovering the aromatic compounds from said conversion product; c) separating a higher molecular weight fraction comprising polyaromatic hydrocarbons (PAH) from a lower molecular weight fraction comprising benzene, toluene and xylene (BTX) by distillation; d) reducing at least part of said higher molecular weight fraction to obtain a reduced fraction comprising polycyclic aliphatics (PCA); and e) subjecting the higher molecular weight fraction obtained in step c), the reduced fraction obtained in step d), or a mixture thereof, to a process to obtain lower molecular weight aromatics (BTX).