TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Components: The HCl/water wt./wt. ratio is 0.2-1.0. The carbohydrate/water wt./wt. ratio is 2-20. The HCl/carbohydrate wt./wt. ratio is 0.02-0.15. The second organic solvent/water wt./wt. ratio in the viscous fluid is R2, where the second organic solvent forms a heterogeneous azeotrope with water and the second organic solvent/water wt./wt. ratio in the azeotrope is R22 and where R2 is greater than R22 by at least 10%. The second organic solvent forms a heterogeneous azeotrope with water, where the second organic solvent has a boiling point at 1 atm of 100-200 degrees C and where the heterogeneous azeotrope has a boiling point at 1 atm of less than 100 degrees C. The first organic solvent in lignin composition forms a heterogeneous azeotrope with water, where the first organic solvent has a boiling point at 1 atm of 100-200 degrees C and where the heterogeneous azeotrope has a boiling point at 1 atm of less than 100 degrees C. The organic compound is a wood extractive. Preferred Fluid: The viscous fluid is under a pressure of less than 400 mbar. The viscous fluid further comprises glucose and at least one carbohydrate selected from mannose, galactose, xylose, arabinose, and fructose; or glucose and at least two carbohydrates selected from mannose, galactose, xylose, arabinose, and fructose. Preferred Method: The method (M3) for the production of a carbohydrate composition involves: ib) providing a lignocellulosic material feed comprising a polysaccharide and lignin; iib) hydrolyzing the polysaccharide in an HCl-comprising hydrolysis medium to form a first aqueous solution comprising carbohydrates, HCl and water, where the wt./wt. ratio of carbohydrates to water is 0.4-3 and where the wt./wt. ratio of HCl to water is 0.17-0.50; iiib) contacting the first aqueous solution with a second organic solvent to form a second evaporation feed, which second organic solvent forms with water a heterogeneous azeotrope and is indicated by at least one of (a2), (b2) and (c2), and forming a heterogeneous azeotrope with water, where the wt./wt. ratio of the second organic solvent to water is 5-0.2, and where the solubility of water in the organic solvent is less than 20%; and ivb) evaporating water, HCl and a second organic solvent from the second evaporation feed at a temperature below 100 degrees C and at a pressure below 1 atm, where a second vapor phase and the viscous fluid (F1) are formed. In method (M1), providing the first aqueous solution involves hydrolyzing a polysaccharide-comprising material in an HCl-comprising hydrolysis medium, where HCl concentration is greater than azeotropic. The wt./wt. ratio of the second organic solvent to water in the second evaporation feed is R23, where the wt./wt. ratio of the second organic solvent to water in the azeotrope is R22 and where R23 is greater than R22 by at least 10%. The method (M1) further involves the steps of condensing the vapors in the second vapor phase to form two phases, a second organic solvent-rich one and a first water-rich one separating the phases, using the second organic solvent-rich phase in step (ii) and using the first water-rich phase for generating the hydrolysis medium. The method (M1) further involves the step of spray drying the viscous fluid to form a de-acidified solid carbohydrate composition. In method (M1), the wt./wt. ratio of HCl to carbohydrates in the de-acidified solid carbohydrate composition is less than 0.03. In method (M3), the wt./wt. ratio of the second organic solvent to water in the second evaporation feed is R23, where the wt./wt. ratio of the second organic solvent to water in the azeotrope is R22 and where R23 is greater than R22 by at least 10%. The method (M3) further involves the steps of condensing the vapors in the second vapor phase to form two phases, a second organic solvent-rich one and a first water-rich one, separating the phases, using the second organic solvent-rich phase in step (iiib) and using the first water-rich phase for generating the hydrolysis medium. The method (M3) further involves the step of spray drying the viscous fluid to form a de-acidified solid carbohydrate composition. In method (M3), the wt./wt. ratio of HCl to carbohydrates in the de-acidified solid carbohydrate composition is less than 0.03. In method (M3), the hydrolyzing forms a hydrolysate, where forming the first aqueous solution involves separating a portion of the HCl from the hydrolysate to form a first separated HCl stream and an HCl-depleted hydrolysate and where the first separated HCl stream is used for generating the hydrolysis medium. In method (M3), the amount, the purity and the concentration of HCl in the hydrolysate are W4, P4 and C4, respectively and the amount, the purity and the concentration of HCl in the first separated HCl stream are W5, P5 and C5, respectively and where W5/W4 is greater than 0.1, P5/P4 is greater than 1.8, and C5/C4 is greater than 1.8. The method (M3) further involves the steps of separating another portion of HCl from the HCl-depleted hydrolysate to form a second separated HCl stream and using the second separated HCl stream for generating the hydrolysis medium. In method (M3), the amount, the purity and the concentration of HCl in the second separated HCl stream are W7, P7 and C7, respectively and where W7/W4 is greater than 0.1, P7/P4 is greater than 1.8, and C7/C4 is greater than 0.4.    TECHNOLOGY FOCUS - PHARMACEUTICALS - Preferred Composition: The lignin composition further comprises at least one carbohydrate, where the concentration of the carbohydrate is less than 5 wt.%. The first organic solvent/water wt./wt. ratio in the lignin composition is R1, where the first organic solvent forms a heterogeneous azeotrope with water, where the wt./wt. ratio of the first organic solvent to water in the azeotrope is R12 and where R1 is greater than R12 by at least 10%. Preferred Method: The method (M2) for the deacidification of a second lignin stream involves: ia) providing a second lignin stream comprising lignin, HCl and water, where the wt./wt. ratio of lignin to water is 0.1-2 and where the wt./wt. ratio of HCl to water is 0.15-1; iia) contacting the second lignin stream with a first organic solvent to form a first evaporation feed, which first organic solvent forms with water a heterogeneous azeotrope and is indicated by at least one of (a1), (b1) and (c1), and forming a heterogeneous azeotrope with water, where the wt./wt. ratio of the first organic solvent to water is 5-0.2, and where the solubility of water in the organic solvent is less than 20%; and iiia) evaporating water, HCl and the first organic solvent from the first evaporation feed at a temperature below 100 degrees C and at a pressure below 1 atm, where a first vapor phase and the lignin composition are formed. The method (M4) for the production of lignin involves: ic) providing a lignocellulosic material feed comprising a polysaccharide and lignin; iic) hydrolyzing the polysaccharide in an HCl-comprising hydrolysis medium to form a second lignin stream comprising lignin, HCl and water, where the wt./wt. ratio of lignin to water is 0.1-2 and where the wt./wt. ratio of HCl to water is 0.15-1; iiic) contacting the second lignin stream with a first organic solvent to form a first evaporation feed, which first organic solvent forms with water a heterogeneous azeotrope and is indicated by at least one of (a1), (b1) and (c1), and forming a heterogeneous azeotrope with water, where the wt./wt. ratio of the first organic solvent to water is 5-0.2, and where the solubility of water in the organic solvent is less than 20%; and ivc) evaporating water, HCl and the first organic solvent from the first evaporation feed at a temperature below 100 degrees C and at a pressure below 1 atm, where a first vapor phase and the lignin composition are formed. The method (M5) for processing a lignocellulosic material and for the production of a carbohydrate composition involves: id) providing a lignocellulosic material feed comprising a polysaccharide and lignin; iid) hydrolyzing the polysaccharide in an HCl-comprising hydrolysis medium to form a first aqueous solution comprising carbohydrates, HCl and water, where wt./wt. ratio of carbohydrates to water is 0.4-3 and where the wt./wt. ratio of HCl to water is 0.17-0.50; and a second lignin stream comprising lignin, HCl and water, where the wt./wt. ratio of the lignin to water is 0.1-2.0 and where the wt./wt. ratio of HCl to water is 0.15-1; iiid) contacting the first aqueous solution with a second organic solvent to form a second evaporation feed, which second organic solvent forms with water a heterogeneous azeotrope and is indicated by at least one of (a2), (b2), and (c2) and forming a heterogeneous azeotrope with water, where the wt./wt. ratio of the second organic solvent to water is 5-0.2, and where the solubility of water in the organic solvent is less than 20%; ivd) evaporating water, HCl and the second organic solvent from the second evaporation feed at a temperature below 100 degrees C and at a pressure below 1 atm, where a second vapor phase and the viscous fluid (F1) are formed; vd) contacting the second lignin stream with a first organic solvent to form a first evaporation feed, which first organic solvent forms a heterogeneous azeotrope with water and is indicated by at least one of (a1), (b1) and (c1), and forming a heterogeneous azeotrope with water, where the wt./wt. ratio of the first organic solvent to water is 5-0.2, and where the solubility of water in the organic solvent is less than 20%; and vid) evaporating water, HCl and the first organic solvent from the first evaporation feed at a temperature below 100 degrees C and at a pressure below 1 atm, where a first vapor phase and the lignin composition are formed. In method (M2), providing the second lignin stream involves hydrolyzing a lignocellulosic material in an HCl-comprising hydrolysis medium, where HCl concentration is greater than azeotropic. In method (M2), the wt./wt. ratio of the first organic solvent to water in the first evaporation feed is R13, where the wt./wt. ratio of the first organic solvent/water in the azeotrope is R12 and where R13 is greater than R12 by at least 10%. The method (M2), further involves the steps of condensing the vapors in the first vapor phase to form two phases, a first organic solvent-rich one and a second water-rich one; separating the phases; and using the first organic solvent-rich phase in step (iia). In method (M5), the first organic solvent and the second organic solvent are of the same chemical composition. In method (M5), the hydrolysis medium is made with a recycled reagent HCl stream, where HCl purity and concentration are P6 and C6, respectively and where P6 is greater than 80% and C6 is greater than 30% (as calculated by 100 time HCl wt. divided by the combined wt. of HCl and water). In method (M5), the wt./wt. ratio of the second organic solvent to water in the second evaporation feed is R23, where the wt./wt. ratio of the second organic solvent to water in the azeotrope is R22 and where R23 is greater than R2 by at least 10%. The method (M5) further involves the steps of condensing the vapors in the second vapor phase to form two phases, a second organic solvent-rich one and a first water-rich one, separating the phases, using the second organic solvent-rich phase in step (iiid) and using the first water-rich phase for generating the hydrolysis medium. In method (M5), when the viscous fluid comprises oligomers, the method further involves at least one of HCl hydrolysis of the oligomers, enzymatic hydrolysis of the oligomers, fermentation of the carbohydrates and simultaneous saccharification and fermentation of the oligomers. The method (M5) further involves the step of spray drying the viscous fluid to form a de-acidified solid carbohydrate composition. In method (M5), the wt./wt. ratio of HCl to carbohydrates in the de-acidified solid carbohydrate composition is less than 0.03. In method (M5), when the de-acidified solid carbohydrate composition comprises oligomers, the method further involves at least one of acid hydrolysis of the oligomers, enzymatic hydrolysis of the oligomers, fermentation of the carbohydrates and simultaneous saccharification and fermentation of the oligomers. The method (M5) further involves a step of treating the lignin composition to effect at least one of deacidification and solvent removal. In method (M5), the treating involves at least one of neutralizing a residual amount of HCl, displacement of residual solvent with water, centrifugation and drying. In method (M5), the wt./wt. ratio of the first organic solvent to water in the first evaporation feed is R13, where the wt./wt. ratio of the first organic solvent to water in the azeotrope is R12 and where R13 is greater than R12 by at least 10%. The method (M5) further involves the steps of condensing the vapors in the first vapor phase to form two phases, a first organic solvent-rich one and a second water-rich one, separating the phases, using the first organic solvent-rich phase in step (vd) and using the second water-rich phase for generating the hydrolysis medium. In method (M5), the hydrolyzing forms a hydrolysate, where forming the first aqueous solution involves separating a portion of the HCl from the hydrolysate to form a first separated HCl stream and an HCl-depleted hydrolysate and where the first separated HCl stream is used for generating the hydrolysis medium. In method (M5), the amount, the purity and the concentration of HCl in the hydrolysate are W4, P4 and C4, respectively the amount, the purity and the concentration of HCl in the first separated HCl stream are W5, P5 and C5, respectively and where W5/W4 is greater than 0.1, P5/P4 is greater than 1.8, and C5/C4 is greater than 1.8. The method (M5) further involves the steps of separating another portion of HCl from the HCl-depleted hydrolysate to form a second separated HCl stream; and using the second separated HCl stream for generating the hydrolysis medium. In method (M5), the amount, the purity and the concentration of HCl in the second separated HCl stream are W7, P7 and C7, respectively, and where W7/W4 is greater than 0.1, P7/P4 is greater than 1.8, and C7/C4 is greater than 0.4. In method (M5), the hydrolyzing forms an HCl-comprising lignin stream, where forming the second lignin stream includes separating HCl from the HCl-comprising lignin stream to form a third separated HCl stream and an HCl-depleted lignin stream and where the third separated HCl stream is used for generating the hydrolysis medium. In method (M5), the amount, the purity and the concentration of HCl in the HCl-comprising lignin stream are W8, P8 and C8, respectively, the amount, the purity and the concentration of HCl in the third separated HCl stream are W9, P9 and C9, respectively, and where W9/W8 is greater than 0.1, P9/P8 is greater than 1.1, and C9/C8 is greater than 1.8. The method (M5) further involves the steps of separating HCl from the HCl-depleted lignin stream to form a fourth separated HCl stream, and using the fourth separated HCl stream for generating the hydrolysis medium. In method (M5), the amount of HCl in the fourth separated HCl stream is W10 and where W10/W8 is greater than 0.1. In method (M5), when the hydrolysate further comprises an organic compound, the method further involves the steps of contacting the hydrolysate with a third organic solvent, where the organic compound selectively transfers to the third organic solvent to form an organic compound-depleted hydrolysate and a first organic compound-carrying solvent; and optionally, recovering the third organic solvent and the organic compound from the first organic compound-carrying solvent to form a separated organic compound and regenerated third organic solvent. In method (M5), when the HCl-comprising lignin stream comprises an organic compound, the method further involves the steps of contacting the HCl-comprising lignin stream with a fourth organic solvent, where the organic compound selectively transfers to the fourth organic solvent to form an organic compound-depleted lignin stream and a second organic compound-carrying solvent; and optionally, recovering the fourth organic solvent and the organic compound from the second organic compound-carrying solvent to form separated organic compound and regenerated the fourth organic solvent. In method (M5), when the second lignin stream comprises an organic compound, the method further involves the steps of contacting it with a fifth organic solvent, where the organic compound selectively transfers to the fifth organic solvent to form an organic compound-depleted second lignin stream and a third organic compound-carrying solvent; and optionally, recovering the fifth organic solvent and organic compound from the third organic compound-carrying solvent to form the separated organic compound and regenerated fifth organic solvent. The method (M4) further involves the steps of condensing the vapors in the first vapor phase to form two phases, a first organic solvent-rich one and a second water-rich one, separating the phases, using the first organic solvent-rich phase in step (iiic) and using the second water-rich phase for generating the hydrolysis medium. The method (M4) further involves a step of treating the lignin composition to effect at least one of deacidification and solvent removal. In method (M4), the treating involves at least one of neutralizing a residual amount of HCl, centrifugation, displacement of residual solvent with water and drying. In method (M4), the hydrolyzing forms HCl-comprising lignin stream, where forming the second lignin stream comprises separating HCl from the HCl-comprising lignin stream to form a third separated HCl stream and an HCl-depleted lignin stream and where the third separated HCl stream is used for generating the hydrolysis medium. In method (M4), the amount, the purity and the concentration of HCl in the HCl-comprising lignin stream are W8, P8 and C8, respectively the amount, the purity and the concentration of HCl in the third separated HCl stream are W9, P9 and C9, respectively and where W9/W8 is greater than 0.1, P9/P8 is greater than 1.1, and C9/C8 is greater than 1.8. The method (M4) further involves the steps of separating HCl from the HCl-depleted lignin stream to form a fourth separated HCl stream and using the fourth separated HCl stream for generating the hydrolysis medium. In method (M4), the amount of HCl in the fourth separated HCl stream is W10 and where W10/W8 is greater than 0.1. In method (M4), the wt./wt. ratio of the first organic solvent to water in the first evaporation feed is R13, where the wt./wt. ratio of the first organic solvent to water in the azeotrope is R12 and where R13 is greater than R12 by at least 10%. EXAMPLE - Preparation of first aqueous solution was carried out as follows: HCl, water and glucose (CH) were mixed to form HCl/(HCl+water) = 0.248 and CH/(CH+water) = 0.64. The mixture was kept at 40 degrees C for 3 hours, in which time oligomers were formed. The first aqueous solution (33.6 g) was combined in a flask with 8.2 g hexanol to form an evaporation feed. Evaporation was applied at 100-150 mbar for about 0.5 hour at a temperature that increased from 62 degrees C at the beginning of the distillation to 76 degrees C at its end. The distillate was cooled and collected to form an organic solvent-rich light phase (light) and an aqueous phase (heavy). At the end of the distillation, two phases were observed in the flask: a small amount of a light one and a heavy viscous fluid. The four phases were weighed and analyzed. The viscous fluid was centrifuged for separation of the solvent prior to analysis. The solvent content there was less than 10 wt.%. The formed viscous fluid had HCl to carbohydrates weight/weight ratio of about 0.058, which represented HCl removal greater than 95% from a typical hydrolysate, where HCl/carbohydrate weight/weight ratio was greater than 1. Its carbohydrate/water weight/weight ratio was about 10, representing removal of about 95% of the water in the hydrolysate (where water/carbohydrate weight/weight ratio was greater than 2). The viscous fluid (as was, before the separation of the solvent) had at 80 degrees C viscosity of about 80cP, low enough to be fed to a spray drier.