Processing of a reaction product mixture of cellulosic biomass material containing at least one volatile organic compound at least one of lignin, a lignin-derived compound, unextracted cellulose, unextracted hemicellulose, a caramelan, and any combination thereof by vaporizing the at least one volatile organic compound using at least thermal energy generated by combusting at least a portion of the reaction product mixture. In a particular embodiment, the reaction product mixture comes from reactions involving deconstruction (or digestion) of cellulosic biomass which contains various polysaccharides (e.g., carbohydrates) and lignin.

The invention relates to a hydrocarbon blend for input to a refinery and comprising a first blend component containing a renewable hydrocarbon component and a second blend component containing petroleum derived hydrocarbon to form at least part of a final hydrocarbon blend for processing in a refinery where the first blend component is characterized by comprising a hydrocarbon substance with at least 70% by weight having a boiling point above 220° C. and by having the characteristics (δ.sub.d1, δ.sub.ρ1, δ.sub.h1)=(17-20, 6-12, 6-12) and; where the second blend component is characterised by having the characteristics (δ.sub.{acute over (α)}2, δ.sub.ρ2, δ.sub.h2)=(17-20, 3-5, 4-7), where the first blend component is present in the final hydrocarbon blend in a relative amount of up to 80 wt %.

The invention relates to a hydrocarbon blend for input to a refinery and comprising a first blend component containing a renewable hydrocarbon component and a second blend component containing petroleum derived hydrocarbon to form at least part of a final hydrocarbon blend for processing in a refinery where the first blend component is characterized by comprising a hydrocarbon substance with at least 70% by weight having a boiling point above 220° C. and by having the characteristics (δ.sub.d1, δ.sub.ρ1, δ.sub.h1)=(17-20, 6-12, 6-12) and; where the second blend component is characterised by having the characteristics (δ.sub.{acute over (α)}2, δ.sub.ρ2, δ.sub.h2)=(17-20, 3-5, 4-7), where the first blend component is present in the final hydrocarbon blend in a relative amount of up to 80 wt %.

The present disclosure relates to a method for controlling product slate of hydrothermal liquefaction by adjusting pH of hydrothermal liquefaction product aqueous phase. The pH of the hydrothermal liquefaction product aqueous phase can be adjusted by heating during hydrothermal liquefaction (110) a mix (30) comprising lignocellulosic feedstock (10) together with acids, alkalis and/or buffers (20) added under aqueous conditions. The method typically comprises separating (120) aqueous phase (53) and oil phase (50), and optionally gas (51) and/or char (52), of the obtained hydrothermal liquefaction product (40). Preferably the separated aqueous phase (53) is recirculated to be mixed 100 with lignocellulosic feedstock (10).

The present disclosure relates to a method for controlling product slate of hydrothermal liquefaction by adjusting pH of hydrothermal liquefaction product aqueous phase. The pH of the hydrothermal liquefaction product aqueous phase can be adjusted by heating during hydrothermal liquefaction (110) a mix (30) comprising lignocellulosic feedstock (10) together with acids, alkalis and/or buffers (20) added under aqueous conditions. The method typically comprises separating (120) aqueous phase (53) and oil phase (50), and optionally gas (51) and/or char (52), of the obtained hydrothermal liquefaction product (40). Preferably the separated aqueous phase (53) is recirculated to be mixed 100 with lignocellulosic feedstock (10).

The disclosure relates to a process for converting lignocellulosic feedstock (10) to renewable product (80), wherein the process comprises the following steps; treating (100) lignocellulosic feedstock (10) with aqueous solution (20) to obtain a mixture (30); heating (110) the mixture (30) of step (a) to a temperature between 290 and 340° C., under a pressure from 90 to 120 bar, to obtain a first product mix (40); separating aqueous phase (53) and oil phase (50), and optionally gas (51) and solids (52), of the first product mix (40) of step (b); and heating (130) the oil phase (50) of step (c) and solvent (60). The heating (130) is optionally followed by fractionation (200) to obtain a light fraction (90) and a heavy fraction (91) and optionally a bottom residue fraction (92) and/or a gaseous fraction.

The disclosure relates to a process for converting lignocellulosic feedstock (10) to renewable product (80), wherein the process comprises the following steps; treating (100) lignocellulosic feedstock (10) with aqueous solution (20) to obtain a mixture (30); heating (110) the mixture (30) of step (a) to a temperature between 290 and 340° C., under a pressure from 90 to 120 bar, to obtain a first product mix (40); separating aqueous phase (53) and oil phase (50), and optionally gas (51) and solids (52), of the first product mix (40) of step (b); and heating (130) the oil phase (50) of step (c) and solvent (60). The heating (130) is optionally followed by fractionation (200) to obtain a light fraction (90) and a heavy fraction (91) and optionally a bottom residue fraction (92) and/or a gaseous fraction.

Provided is a conversion process for an organic oil, relating to the field of biomass utilization, energy and chemical industry. The conversion process is carried out in presence of an aqueous slurry and a catalyst selected from the group consisting of an iron oxide compound, a waste agent resulting from use of an iron oxide compound as desulfurizer, and a regeneration product of the waste agent, under a controlled molar ratio of iron element to sulfur element. It is found that free radical condensation polymerization of organic oil during cracking process can be blocked effectively by using carbonylation, and hydrogenation is achieved with active hydrogen produced from the conversion of CO and water. In the conversion process, organic material, especially biomass solid, can be directly converted without dehydration, and water can be additionally added to the biomass liquid or the mineral oil.

Provided is a conversion process for an organic oil, relating to the field of biomass utilization, energy and chemical industry. The conversion process is carried out in presence of an aqueous slurry and a catalyst selected from the group consisting of an iron oxide compound, a waste agent resulting from use of an iron oxide compound as desulfurizer, and a regeneration product of the waste agent, under a controlled molar ratio of iron element to sulfur element. It is found that free radical condensation polymerization of organic oil during cracking process can be blocked effectively by using carbonylation, and hydrogenation is achieved with active hydrogen produced from the conversion of CO and water. In the conversion process, organic material, especially biomass solid, can be directly converted without dehydration, and water can be additionally added to the biomass liquid or the mineral oil.

A process for converting lignocellulosic feedstock includes providing a lignocellulosic feedstock into a first inlet of a first reactor at a first end, and providing a hot feedstock into a second inlet of the first reactor at a second end of the first reactor. The process includes heating and reacting the lignocellulosic feedstock with the hot feedstock and outputting a first product stream from a first product outlet of the first reactor. The first product stream is an alkane rich product stream. A reactor system includes a first reactor having a first inlet at a first end, a second inlet at a second end and at least one product outlet. The first reactor is configured to receive a lignocellulosic feedstock at the first inlet and a hot feedstock at the second inlet. The system includes a second reactor having a first inlet downstream from the at least one product outlet.