AU2013216823A1 - Enhancing fermentation of starch-and sugar-based feedstocks - Google Patents

Abstract

Provided are methods, systems, and compositions for increasing the rate and/or yield of fermentation processes using blended feedstocks. Also provided are methods, systems, and compositions for decreasing the yield of one or more undesirable products during fermentation.

Description

WO 2013/120035 PCT/US2013/025457 ENHANCING FERMENTATION OF STARCH- AND SUGAR-BASED FEEDSTOCKS CROSS-REFERENCE [0001] This application claims the benefit of U.S. Patent Application Serial No. 13/731,633, filed December 31, 2012, U.S. Provisional Application No. 61/597,347, filed February 10, 2012, and U.S. Provisional Application No. 61/648,567, filed May 17, 2012, each of which application is incorporated herein by reference in its entirety. BACKGROUND OF THE INVENTION [0002] The demand for renewable fuels and chemical is growing significantly and is required to reduce reliance on petroleum-based products and to lower gas emissions. At the same time, interest in biofuels, such as ethanol, as an alternative to petroleum has greatly increased, in part due to the desire to promote domestic rural economics. Ethanol is the most commonly used biofuel, and current U.S. biofuel is almost exclusively derived from corn. To meet some of the higher ethanol production goals would require more corn than the United States currently produces. At the same time, a concern over the use of food crops for fuel is an obstacle to use of further corn for ethanol. Another obstacle to widespread adoption of biofuels and bio-products is the economic cost of producing the ethanol. A major contributing factor to this cost is transportation of biomass feedstock from the location where feedstock is grown to the location where it is processed into biofuels and chemicals. More efficient use of starch fermentation, supplemented with sugars from non-starch cellulosic materials would help defray these costs. Although the supplementation of cellulosic sugars assists in starch production, it would be helpful to optimize this process in a manner wherein fermenting organisms can utilize the maximum amount of sugar provided to them. SUMMARY OF THE INVENTION [0003] Disclosed herein are methods of producing one or more fermentation end-products comprising: (a) combining a first biomass comprising non-cellulosic saccharides with a saccharide stream comprising C6 monosaccharides to produce a blended feedstock in a broth; (b) contacting the blended feedstock with one or more biocatalysts; (c) fermenting the non cellulosic saccharides of the first biomass and the C6 monosaccharides of the saccharides stream to produce one or more fermentation end-products comprising an alcohol and a polyol, wherein an alcohol yield is increased and a polyol yield is decreased in comparison to fermentation of the first biomass without the saccharide stream. In some embodiments, the alcohol is ethanol. In some embodiments, the polyol is glycerol. In some embodiments, the 1 WO 2013/120035 PCT/US2013/025457 broth comprising the blended feedstock has a lower osmolarity than a broth containing only the first biomass at an equivalent total saccharide level in monosaccharide equivalents. In some embodiments, saccharide stream further comprises C5 monosaccharides. In some embodiments, the C6 monosaccharides comprise cellulosic-derived C6 monosaccharides, non-cellulosic derived C6 monosaccharides, or a combination thereof In some embodiments, the alcohol yield is increased by about 1% to about 100% relative to fermentation of the first biomass without the saccharide stream. In some embodiments, the alcohol is produced at a rate that is faster relative to fermentation of the first biomass without the saccharide stream. In some embodiments, the alcohol is produced at a rate that is about 1% to about 100% faster relative to fermentation of the first biomass without the saccharide stream. In some embodiments, the C6 monosaccharides of the saccharide stream are at a concentration that differs from a concentration of the non-cellulosic saccharides in the first biomass by less than +/- 50%, wherein the concentration of non-cellulosic saccharides in the first biomass is in monosaccharide equivalents. In some embodiments, the C6 monosaccharides of the saccharide stream are at a concentration that differs from a concentration of the non cellulosic saccharides in the first biomass by less than +/- 25%, wherein the concentration of non-cellulosic saccharides in the first biomass is in monosaccharide equivalents. In some embodiments, the method is a fed-batch fermentation wherein the saccharide stream is added over time. In some embodiments, the saccharide stream is added at a rate of from about 0.01 mL/min/L of broth to about 5 mL/min/L of broth during the fermenting. In some embodiments, the polyols yield is decreased by about 1% to about 100% relative to the non fed batch fermentation. In some embodiments, the first biomass comprises starch, sucrose, or a combination thereof In some embodiments, the first biomass comprises corn, corn mash, sugar cane, sugar beets, sugar palms, sweet sorghum, nypa palm, cassava, rice, milo, sorghum, sweet potatoes, wheat, molasses, tubers, roots, stems, whole grains, barley, rye, milo, sago, cassaya, tapioca, rice peas, beans, potatoes, beets, fruits, or a combination thereof In some embodiments, the saccharide stream is produced from the pretreatment and/or hydrolysis of cellulose, hemicellulose, lignocellulose material, starch, or a combination thereof In some embodiments, the saccharide stream is produced by the pretreatment and/or hydrolysis of a second biomass comprising cellulose, hemicellulose, and/or lignocellulose. In some embodiments, the second biomass comprises corn, corn syrup, corn stover, corn cobs, molasses, silage, grass, straw, grain hulls, bagasse, distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, 2 WO 2013/120035 PCT/US2013/025457 prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof In some embodiments, the one or more biocatalysts comprise one or more fermenting microorganisms. In some embodiments, the one or more biocatalysts comprise one or more yeasts and/or one or more bacteria. In some embodiments, the one or more biocatalysts comprise one or more yeasts. In some embodiments, the one or more biocatalysts comprise one or more strains of Saccharomyces cerevisiae. In some embodiments, at least one of the one or more biocatalysts is a genetically-modified yeast that ferments C5 and C6 saccharides. In some embodiments, at least one of the one or more biocatalysts is a bacteria that hydrolyzes and/or ferments C5 and C6 saccharides. In some embodiments, at least one of the one or more biocatalysts is a hydrolytic enzyme. In some embodiments, the one or more biocatalysts comprise an endoglucanase, an exoglucanase, a cellobiohydrolase, a cellulase, a beta-glucosidase, a glycoside hydrolase, a glycosyltransferase, a lyase, an esterase, a glucamylase, or a combination thereof In some embodiments, at least one of the one or more biocatalysts is an enzyme that hydrolyzes starch. In some embodiments, at least one of the one or more biocatalysts is an alpha-amylase, glucoamylase, beta-amylase, exo-alpha-1,4 glucanase, or pullulanase. In some embodiments, the one or more biocatalysts comprise at least one fermenting microorganism and at least one hydrolytic enzyme. In some embodiments, the one or more biocatalysts comprise at least one fermenting microorganism that is a yeast or bacteria and at least one enzyme that hydrolyzes starch. In some embodiments, the blended feedstock comprises less than 100 g/L monosaccharides prior to contacting with the one or more biocatalysts. In some embodiments, the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides prior to contacting with the one or more biocatalysts. In some embodiments, the first biomass and the saccharide stream are combined in a ratio of from about 50:50 to 99:1 (first biomass: saccharide stream) by volume or by weight:volume. In some embodiments, the first biomass and the saccharide stream are combined in a ratio of about 80:20 (first biomass: saccharide stream) by volume or by weight:volume. In some embodiments, the first biomass and the saccharide stream are combined in a ratio of about 90:10 (first biomass: saccharide stream) by volume or by weight:volume. In some embodiments, the blended feedstock comprises from about 10% to about 50% solids from the first biomass. In some embodiments, the blended feedstock comprises from about 20% to about 40% solids from the first biomass. In some embodiments, the blended feedstock comprises from about 30% to about 36% solids from the first biomass. 3 WO 2013/120035 PCT/US2013/025457 In some embodiments, the C6 monosaccharides of the saccharide stream are at a concentration of from about 10% to about 70% w/v prior to combining with the first biomass. In some embodiments, the C6 monosaccharides of the saccharide stream are at a concentration of from about 20% to about 50% w/v prior to combining with the first biomass. Also disclosed are fermentation end-products produced by these methods. In some embodiments, the fermentation end-product is ethanol. [0004] Disclosed herein are methods of producing one or more fermentation end-products comprising: (a) combining a first biomass with one or more cellulosic-derived C6 monosaccharides to produce a blended feedstock in a broth; (b) contacting the blended feedstock with one or more biocatalysts; and (c) fermenting the first biomass and the one or more cellulosic-derived C6 monosaccharides for sufficient time to produce one or more fermentation end-products from the blended feedstock, wherein a yield of at least one of the one or more fermentation end-products is increased relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some embodiments, the yield of the at least one of the one or more fermentation end-products is increased by about 1% to about 100% relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some embodiments, at least one of the one or more fermentation end-products is produced at a rate that is faster relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some embodiments, at least one of the one or more fermentation end products is produced at a rate that is about 1% to about 100% faster relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration that differs from a concentration of saccharides in the first biomass by less than +/- 50%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration that differs from a concentration of saccharides in the first biomass by less than +/- 25%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents. In some embodiments, the one or more fermentation end products comprise one or more alcohols. In some embodiments, the one or more fermentation end-products comprise ethanol. In some embodiments, the method is a fed-batch fermentation wherein the one or more cellulosic-derived C6 monosaccharides are added over time. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are added at a rate of from about 0.01 mL/min/L of broth to about 5 mL/min/L of broth during 4 WO 2013/120035 PCT/US2013/025457 the fermenting. In some embodiments, a yield of one or more other products is decreased relative to a non-fed batch fermentation. In some embodiments, the yield of the one or more other products is decreased by about 1% to about 100% relative to the non-fed batch fermentation. In some embodiments, the one or more other products comprise one or more polyols or sugar alcohols. In some embodiments, the one or more other products comprise methanol, glycol, glycerol, erythritol, threitol, arabitol, xylitol, ribitol, mannitol, sorbitol, dulcitol, fucitol, iditol, inositol, volemitol, isomalt, maltitol, lactitol, polyglycitol, or a combination thereof. In some embodiments, the one or more other products comprise glycerol. In some embodiments, the first biomass comprises non-cellulosic sugars. In some embodiments, the first biomass comprises non-cellulosic oligosaccharides. In some embodiments, the first biomass comprises starch. In some embodiments, the first biomass comprises corn, corn mash, sugar cane, sugar beets, sugar palms, sweet sorghum, nypa palm, cassava, rice, milo, sorghum, sweet potatoes, wheat, molasses, tubers, roots, stems, whole grains, barley, rye, milo, sago, cassaya, tapioca, rice peas, beans, potatoes, beets, fruits, or a combination thereof. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are produced from the pretreatment and/or hydrolysis of cellulose, hemicellulose, or lignocellulose material. In some embodiments, the one or more cellulosic derived C6 monosaccharides are produced by the pretreatment and/or hydrolysis of a second biomass comprising cellulose, hemicellulose, or lignocellulose. In some embodiments, the second biomass comprises corn, corn syrup, corn stover, corn cobs, molasses, silage, grass, straw, grain hulls, bagasse, distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof. In some embodiments, the one or more biocatalysts comprise one or more fermenting microorganisms. In some embodiments, the one or more biocatalysts comprise one or more yeasts and/or one or more bacteria. In some embodiments, the one or more biocatalysts comprise one or more yeasts. In some embodiments, the one or more biocatalysts comprise one or more strains of Saccharomyces cerevisiae. In some embodiments, at least one of the one or more biocatalysts is a genetically modified yeast that ferments C5 and C6 saccharides. In some embodiments, at least one of the one or more biocatalysts is a bacteria that hydrolyzes and/or ferments C5 and C6 saccharides. In some embodiments, at least one of the one or more biocatalysts is a hydrolytic 5 WO 2013/120035 PCT/US2013/025457 enzyme. In some embodiments, the one or more biocatalysts comprise an endoglucanase, an exoglucanase, a cellobiohydrolase, a cellulase, a beta-glucosidase, a glycoside hydrolase, a glycosyltransferase, a lyase, an esterase, a glucamylase, or a combination thereof In some embodiments, at least one of the one or more biocatalysts is an enzyme that hydrolyzes starch. In some embodiments, at least one of the one or more biocatalysts is an alpha amylase, glucoamylase, beta-amylase, exo-alpha-1,4-glucanase, or pullulanase. In some embodiments, the one or more biocatalysts comprise at least one fermenting microorganism and at least one hydrolytic enzyme. In some embodiments, the one or more biocatalysts comprise at least one fermenting microorganism that is a yeast or bacteria and at least one enzyme that hydrolyzes starch. In some embodiments, the blended feedstock comprises less than 100 g/L monosaccharides prior to contacting with the one or more biocatalysts. In some embodiments, the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides prior to contacting with the one or more biocatalysts. In some embodiments, the first biomass and the one or more cellulosic-derived C6 monosaccharides are combined in a ratio of from about 50:50 to 99:1 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume. In some embodiments, the first biomass and the one or more cellulosic-derived C6 monosaccharides are combined in a ratio of about 80:20 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume. In some embodiments, the first biomass and the one or more cellulosic derived C6 monosaccharides are combined in a ratio of about 90:10 (first biomass: cellulosic derived C6 monosaccharides) by volume or by weight:volume. In some embodiments, the blended feedstock comprises from about 10% to about 50% solids from the first biomass. In some embodiments, the blended feedstock comprises from about 20% to about 40% solids from the first biomass. In some embodiments, the blended feedstock comprises from about 30% to about 36% solids from the first biomass. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 10% to about 70% w/v prior to combining with the first biomass. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 20% to about 50% w/v prior to combining with the first biomass. [0005] Also provided are fermentation end-products produced by the methods disclosed herein. In some embodiments, the fermentation end-product is an alcohol. In some embodiments, the fermentation end-product is ethanol. [0006] Also disclosed herein are methods of producing one or more fermentation end products comprising: (a) combining a first biomass with one or more cellulosic-derived C6 6 WO 2013/120035 PCT/US2013/025457 monosaccharides to produce a blended feedstock in a broth; (b) contacting the blended feedstock with one or more biocatalysts; and (c) fermenting the first biomass and the one or more cellulosic-derived C6 monosaccharides for sufficient time to produce one or more fermentation end-products from the blended feedstock, wherein at least one of the one or more fermentation end-products is produced at a rate that is faster relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some embodiments, a yield of at least one of the one or more fermentation end-products is increased relative to fermentation of the first biomass without the one or more cellulosic derived C6 monosaccharides. In some embodiments, a yield of at least one of the one or more fermentation end-products is increased by about 1% to about 100% relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some embodiments, the rate that the at least one of the one or more fermentation end-products is produced is about 1% to about 100% faster relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration that differs from a concentration of saccharides in the first biomass by less than +/- 50%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration that differs from a concentration of saccharides in the first biomass by less than +/- 25%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents. In some embodiments, the one or more fermentation end-products comprise one or more alcohols. In some embodiments, the one or more fermentation end-products comprise ethanol. In some embodiments, the method is a fed-batch fermentation wherein the one or more cellulosic-derived C6 monosaccharides are added over time. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are added at a rate of from about 0.01 mL/min/L of broth to about 5 mL/min/L of broth during the fermenting. In some embodiments, a yield of one or more other products is decreased relative to a non-fed batch fermentation. In some embodiments, the yield of the one or more other products is decreased by about 1% to about 100% relative to the non-fed batch fermentation. In some embodiments, the one or more other products comprise one or more polyols or sugar alcohols. In some embodiments, the one or more other products comprise methanol, glycol, glycerol, erythritol, threitol, arabitol, xylitol, ribitol, mannitol, sorbitol, dulcitol, fucitol, iditol, inositol, volemitol, isomalt, maltitol, lactitol, polyglycitol, or a combination thereof In some embodiments, the one or more other products comprise glycerol. In some embodiments, the first biomass 7 WO 2013/120035 PCT/US2013/025457 comprises non-cellulosic sugars. In some embodiments, the first biomass comprises non cellulosic oligosaccharides. In some embodiments, the first biomass comprises starch. In some embodiments, the first biomass comprises corn, corn mash, sugar cane, sugar beets, sugar palms, sweet sorghum, nypa palm, cassava, rice, milo, sorghum, sweet potatoes, wheat, molasses, tubers, roots, stems, whole grains, barley, rye, milo, sago, cassaya, tapioca, rice peas, beans, potatoes, beets, fruits, or a combination thereof In some embodiments, the one or more cellulosic-derived C6 monosaccharides are produced from the pretreatment and/or hydrolysis of cellulose, hemicellulose, or lignocellulose material. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are produced by the pretreatment and/or hydrolysis of a second biomass comprising cellulose, hemicellulose, or lignocellulose. In some embodiments, the second biomass comprises corn, corn syrup, corn stover, corn cobs, molasses, silage, grass, straw, grain hulls, bagasse, distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof In some embodiments, the one or more biocatalysts comprise one or more fermenting microorganisms. In some embodiments, the one or more biocatalysts comprise one or more yeasts and/or one or more bacteria. In some embodiments, the one or more biocatalysts comprise one or more yeasts. In some embodiments, the one or more biocatalysts comprise one or more strains of Saccharomyces cerevisiae. In some embodiments, at least one of the one or more biocatalysts is a genetically-modified yeast that ferments C5 and C6 saccharides. In some embodiments, at least one of the one or more biocatalysts is a bacteria that hydrolyzes and/or ferments C5 and C6 saccharides. In some embodiments, at least one of the one or more biocatalysts is a hydrolytic enzyme. In some embodiments, the one or more biocatalysts comprise an endoglucanase, an exoglucanase, a cellobiohydrolase, a cellulase, a beta-glucosidase, a glycoside hydrolase, a glycosyltransferase, a lyase, an esterase, a glucamylase, or a combination thereof In some embodiments, at least one of the one or more biocatalysts is an enzyme that hydrolyzes starch. In some embodiments, at least one of the one or more biocatalysts is an alpha-amylase, glucoamylase, beta-amylase, exo-alpha-1,4 glucanase, or pullulanase. In some embodiments, the one or more biocatalysts comprise at least one fermenting microorganism and at least one hydrolytic enzyme. In some embodiments, the one or more biocatalysts comprise at least one fermenting microorganism 8 WO 2013/120035 PCT/US2013/025457 that is a yeast or bacteria and at least one enzyme that hydrolyzes starch. In some embodiments, the blended feedstock comprises less than 100 g/L monosaccharides prior to contacting with the one or more biocatalysts. In some embodiments, the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides prior to contacting with the one or more biocatalysts. In some embodiments, the first biomass and the one or more cellulosic-derived C6 monosaccharides are combined in a ratio of from about 50:50 to 99:1 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume. In some embodiments, the first biomass and the one or more cellulosic-derived C6 monosaccharides are combined in a ratio of about 80:20 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume. In some embodiments, the first biomass and the one or more cellulosic-derived C6 monosaccharides are combined in a ratio of about 90:10 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume. In some embodiments, the blended feedstock comprises from about 10% to about 50% solids from the first biomass. In some embodiments, the blended feedstock comprises from about 20% to about 40% solids from the first biomass. In some embodiments, the blended feedstock comprises from about 30% to about 36% solids from the first biomass. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 10% to about 70% w/v prior to combining with the first biomass. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 20% to about 50% w/v prior to combining with the first biomass. [0007] Also disclosed herein are methods of producing one or more fermentation end products comprising: (a) combining a first biomass with one or more cellulosic-derived C6 monosaccharides to produce a blended feedstock in a broth; (b) contacting the blended feedstock with one or more biocatalysts; and (c) fermenting the first biomass and the one or more cellulosic-derived C6 monosaccharides for sufficient time to produce one or more fermentation end-products from the blended feedstock, wherein the one or more cellulosic derived C6 monosaccharides are at a concentration that differs from a concentration of saccharides in the first biomass by less than +/- 50%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents. In some embodiments, a yield of at least one of the one or more fermentation end-products is increased relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some embodiments, a yield of at least one of the one or more fermentation end-products is increased by about 1% to about 100% relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some 9 WO 2013/120035 PCT/US2013/025457 embodiments, at least one of the one or more fermentation end-products is produced at a rate that is faster relative to fermentation of the first biomass without the one or more cellulosic derived C6 monosaccharides. In some embodiments, at least one of the one or more fermentation end-products is produced at a rate that is about 1% to about 100% faster relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some embodiments, the concentration of the one or more cellulosic derived C6 monosaccharides differs from the concentration of saccharides in the first biomass by less than +/- 25%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents. In some embodiments, the one or more fermentation end products comprise one or more alcohols. In some embodiments, the one or more fermentation end-products comprise ethanol. In some embodiments, the method is a fed-batch fermentation wherein the one or more cellulosic-derived C6 monosaccharides are added over time. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are added at a rate of from about 0.01 mL/min/L of broth to about 5 mL/min/L of broth during the fermenting. In some embodiments, a yield of one or more other products is decreased relative to a non-fed batch fermentation. In some embodiments, the yield of the one or more other products is decreased by about 1% to about 100% relative to the non-fed batch fermentation. In some embodiments, the one or more other products comprise one or more polyols or sugar alcohols. In some embodiments, the one or more other products comprise methanol, glycol, glycerol, erythritol, threitol, arabitol, xylitol, ribitol, mannitol, sorbitol, dulcitol, fucitol, iditol, inositol, volemitol, isomalt, maltitol, lactitol, polyglycitol, or a combination thereof In some embodiments, the one or more other products comprise glycerol. In some embodiments, the first biomass comprises non-cellulosic sugars. In some embodiments, the first biomass comprises non-cellulosic oligosaccharides. In some embodiments, the first biomass comprises starch. In some embodiments, the first biomass comprises corn, corn mash, sugar cane, sugar beets, sugar palms, sweet sorghum, nypa palm, cassava, rice, milo, sorghum, sweet potatoes, wheat, molasses, tubers, roots, stems, whole grains, barley, rye, milo, sago, cassaya, tapioca, rice peas, beans, potatoes, beets, fruits, or a combination thereof In some embodiments, the one or more cellulosic-derived C6 monosaccharides are produced from the pretreatment and/or hydrolysis of cellulose, hemicellulose, or lignocellulose material. In some embodiments, the one or more cellulosic derived C6 monosaccharides are produced by the pretreatment and/or hydrolysis of a second biomass comprising cellulose, hemicellulose, or lignocellulose. In some embodiments, the second biomass comprises corn, corn syrup, corn stover, corn cobs, molasses, silage, grass, 10 WO 2013/120035 PCT/US2013/025457 straw, grain hulls, bagasse, distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof In some embodiments, the one or more biocatalysts comprise one or more fermenting microorganisms. In some embodiments, the one or more biocatalysts comprise one or more yeasts and/or one or more bacteria. In some embodiments, the one or more biocatalysts comprise one or more yeasts. In some embodiments, the one or more biocatalysts comprise one or more strains of Saccharomyces cerevisiae. In some embodiments, at least one of the one or more biocatalysts is a genetically modified yeast that ferments C5 and C6 saccharides. In some embodiments, at least one of the one or more biocatalysts is a bacteria that hydrolyzes and/or ferments C5 and C6 saccharides. In some embodiments, at least one of the one or more biocatalysts is a hydrolytic enzyme. In some embodiments, the one or more biocatalysts comprise an endoglucanase, an exoglucanase, a cellobiohydrolase, a cellulase, a beta-glucosidase, a glycoside hydrolase, a glycosyltransferase, a lyase, an esterase, a glucamylase, or a combination thereof In some embodiments, at least one of the one or more biocatalysts is an enzyme that hydrolyzes starch. In some embodiments, at least one of the one or more biocatalysts is an alpha amylase, glucoamylase, beta-amylase, exo-alpha-1,4-glucanase, or pullulanase. In some embodiments, the one or more biocatalysts comprise at least one fermenting microorganism and at least one hydrolytic enzyme. In some embodiments, the one or more biocatalysts comprise at least one fermenting microorganism that is a yeast or bacteria and at least one enzyme that hydrolyzes starch. In some embodiments, the blended feedstock comprises less than 100 g/L monosaccharides prior to contacting with the one or more biocatalysts. In some embodiments, the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides prior to contacting with the one or more biocatalysts. In some embodiments, the first biomass and the one or more cellulosic-derived C6 monosaccharides are combined in a ratio of from about 50:50 to 99:1 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume. In some embodiments, the first biomass and the one or more cellulosic-derived C6 monosaccharides are combined in a ratio of about 80:20 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume. In some embodiments, the first biomass and the one or more cellulosic derived C6 monosaccharides are combined in a ratio of about 90:10 (first biomass: cellulosic 11 WO 2013/120035 PCT/US2013/025457 derived C6 monosaccharides) by volume or by weight:volume. In some embodiments, the blended feedstock comprises from about 10% to about 50% solids from the first biomass. In some embodiments, the blended feedstock comprises from about 20% to about 40% solids from the first biomass. In some embodiments, the blended feedstock comprises from about 30% to about 36% solids from the first biomass. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 10% to about 70% w/v prior to combining with the first biomass. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 20% to about 50% w/v prior to combining with the first biomass. [0008] Disclosed herein are systems for producing one or more fermentation end-products comprising: (a) combining a fermentor comprising a broth; (b) a blended feedstock comprising a first biomass and one or more cellulosic-derived C6 monosaccharides in the broth; and (c) one or more biocatalysts. In some embodiments, yield of at least one of the one or more fermentation end-products is increased relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some embodiments, the yield of the at least one of the one or more fermentation end-products is increased by about 1% to about 100% relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some embodiments, at least one of the one or more fermentation end-products is produced at a rate that is faster relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some embodiments, at least one of the one or more fermentation end products is produced at a rate that is about 1% to about 100% faster relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration that differs from a concentration of saccharides in the first biomass by less than +/- 50%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration that differs from a concentration of saccharides in the first biomass by less than +/- 25%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents. In some embodiments, the one or more fermentation end products comprise one or more alcohols. In some embodiments, the one or more fermentation end-products comprise ethanol. In some embodiments, the system further comprises a feeder to add the one or more cellulosic-derived C6 monosaccharides to the broth over time. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are added at a rate of 12 WO 2013/120035 PCT/US2013/025457 from about 0.01 mL/min/L of broth to about 5 mL/min/L of broth. In some embodiments, a yield of one or more other products is decreased relative to a system that does not contain the feeder. In some embodiments, the yield of the one or more other products is decreased by about 1% to about 100% relative to the non-fed batch fermentation. In some embodiments, the one or more other products comprise one or more polyols or sugar alcohols. In some embodiments, the one or more other products comprise methanol, glycol, glycerol, erythritol, threitol, arabitol, xylitol, ribitol, mannitol, sorbitol, dulcitol, fucitol, iditol, inositol, volemitol, isomalt, maltitol, lactitol, polyglycitol, or a combination thereof. In some embodiments, the one or more other products comprise glycerol. In some embodiments, the first biomass comprises non-cellulosic sugars. In some embodiments, the first biomass comprises non cellulosic oligosaccharides. In some embodiments, the first biomass comprises starch. In some embodiments, the first biomass comprises corn, corn mash, sugar cane, sugar beets, sugar palms, sweet sorghum, nypa palm, cassava, rice, milo, sorghum, sweet potatoes, wheat, molasses, tubers, roots, stems, whole grains, barley, rye, milo, sago, cassaya, tapioca, rice peas, beans, potatoes, beets, fruits, or a combination thereof. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are produced from the pretreatment and/or hydrolysis of cellulose, hemicellulose, or lignocellulose material. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are produced by the pretreatment and/or hydrolysis of a second biomass comprising cellulose, hemicellulose, or lignocellulose. In some embodiments, the second biomass comprises corn, corn syrup, corn stover, corn cobs, molasses, silage, grass, straw, grain hulls, bagasse, distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof. In some embodiments, the one or more biocatalysts comprise one or more fermenting microorganisms. In some embodiments, the one or more biocatalysts comprise one or more yeasts and/or one or more bacteria. In some embodiments, the one or more biocatalysts comprise one or more yeasts. In some embodiments, the one or more biocatalysts comprise one or more strains of Saccharomyces cerevisiae. In some embodiments, at least one of the one or more biocatalysts is a genetically-modified yeast that ferments C5 and C6 saccharides. In some embodiments, at least one of the one or more biocatalysts is a bacteria that hydrolyzes and/or ferments C5 and C6 saccharides. In some embodiments, at least one of the 13 WO 2013/120035 PCT/US2013/025457 one or more biocatalysts is a hydrolytic enzyme. In some embodiments, the one or more biocatalysts comprise an endoglucanase, an exoglucanase, a cellobiohydrolase, a cellulase, a beta-glucosidase, a glycoside hydrolase, a glycosyltransferase, a lyase, an esterase, a glucamylase, or a combination thereof In some embodiments, at least one of the one or more biocatalysts is an enzyme that hydrolyzes starch. In some embodiments, at least one of the one or more biocatalysts is an alpha-amylase, glucoamylase, beta-amylase, exo-alpha-1,4 glucanase, or pullulanase. In some embodiments, the one or more biocatalysts comprise at least one fermenting microorganism and at least one hydrolytic enzyme. In some embodiments, the one or more biocatalysts comprise at least one fermenting microorganism that is a yeast or bacteria and at least one enzyme that hydrolyzes starch. In some embodiments, the blended feedstock comprises less than 100 g/L monosaccharides. In some embodiments, the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides. In some embodiments, the first biomass and the one or more cellulosic derived C6 monosaccharides are in a ratio of from about 50:50 to 99:1 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume. In some embodiments, the first biomass and the one or more cellulosic-derived C6 monosaccharides are in a ratio of about 80:20 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume. In some embodiments, the first biomass and the one or more cellulosic-derived C6 monosaccharides are in a ratio of about 90:10 (first biomass: cellulosic derived C6 monosaccharides) by volume or by weight:volume. In some embodiments, the blended feedstock comprises from about 10% to about 50% solids from the first biomass. In some embodiments, the blended feedstock comprises from about 20% to about 40% solids from the first biomass. In some embodiments, the blended feedstock comprises from about 30% to about 36% solids from the first biomass. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 10% to about 70% w/v prior to combining with the first biomass. In some embodiments, the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 20% to about 50% w/v prior to combining with the first biomass. In some embodiments, the system further comprises a hydrolysis unit for producing the one or more cellulosic-derived monosaccharides from a second biomass. In some embodiments, the system further comprises a filter for separating solids from the one or more cellulosic derived C6 monosaccharides. [0009] Provided herein are methods of producing one or more fermentation end-products comprising: (a) combining a first biomass with one or more monosaccharides to produce a 14 WO 2013/120035 PCT/US2013/025457 blended feedstock; (b) contacting the blended feedstock with one or more biocatalysts; and (c) fermenting the first biomass and the one or more monosaccharides for sufficient time to produce one or more fermentation end-products from the blended feedstock. In some embodiments, a yield of at least one of the one or more fermentation end-products is increased relative to fermentation of the first biomass without the one or more monosaccharides. In some embodiments, a yield of at least one of the one or more fermentation end-products is increased by about 1% to about 100% relative to fermentation of the first biomass without the one or more monosaccharides. In some embodiments, a rate of production for at least one of the one or more fermentation end-products is increased relative to fermentation of the first biomass without the one or more monosaccharides. In some embodiments, a rate of production for at least one of the one or more fermentation end products is increased by about 1% to about 100% relative to fermentation of the first biomass without the one or more monosaccharides. In some embodiments, the one or more fermentation end-products comprise one or more alcohols. In some embodiments, the one or more fermentation end-products comprise ethanol. In some embodiments, a yield of one or more other products is decreased relative to fermentation of the one or more monosaccharides without the first biomass. In some embodiments, a yield of one or more other products is decreased by about 1% to about 100% relative to fermentation of the one or more monosaccharides without the first biomass. In some embodiments, the one or more other products comprise one or more polyols or sugar alcohols. In some embodiments, the one or more other products comprise methanol, glycol, glycerol, erythritol, threitol, arabitol, xylitol, ribitol, mannitol, sorbitol, dulcitol, fucitol, iditol, inositol, volemitol, isomalt, maltitol, lactitol, polyglycitol, or a combination thereof. In some embodiments, the one or more other products comprise glycerol In some embodiments, the first biomass comprises non-cellulosic sugars. In some embodiments, the first biomass comprises non-cellulosic oligosaccharides. In some embodiments, the first biomass comprises starch. In some embodiments, the first biomass comprises corn or corn mash, sugar cane, sugar beet, sugar palm, sweet sorghum, nypa palm, cassava, rice, milo, sorghum, sweet potato, wheat, molasses, or a combination thereof. In some embodiments, the one or more monosaccharides are produced from the pretreatment and/or hydrolysis of cellulose, hemicellulose, or lignocellulose material. In some embodiments, the one or more monosaccharides are a C6-enriched hydrolysate produced by the pretreatment and/or hydrolysis of a second biomass comprising cellulose, hemicellulose, or lignocellulose. In some embodiments, the second biomass comprises corn, corn syrup, corn stover, corn cobs, molasses, silage, grass, straw, grain hulls, bagasse, 15 WO 2013/120035 PCT/US2013/025457 distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof In some embodiments, the one or more monosaccharides are at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 50%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers. In some embodiments, the one or more monosaccharides are at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 40%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers. In some embodiments, the one or more monosaccharides are at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 30%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers. In some embodiments, the one or more monosaccharides are at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 20%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers. In some embodiments, the one or more monosaccharides are at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 15%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers. In some embodiments, the one or more monosaccharides are at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 10%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers. In some embodiments, the one or more monosaccharides comprises less than about 50% C5 sugars. In some embodiments, the one or more monosaccharides comprises less than about 40% C5 sugars. In some embodiments, the one or more monosaccharides comprises less than about 30% C5 sugars. In some embodiments, the one or more monosaccharides comprises less than about 20% C5 sugars. In some embodiments, the one or more monosaccharides comprises less than about 10% C5 sugars. In some embodiments, the one or more monosaccharides comprises from about 0.1% to about 10% C5 sugars. In some embodiments, at least one of the one or more biocatalysts is a fermenting microorganism. In some embodiments, at least one of the one or more biocatalysts is a hydrolytic enzyme. In some embodiments, the one or more biocatalysts comprise at least one fermenting microorganism and at least one hydrolytic enzyme. In some 16 WO 2013/120035 PCT/US2013/025457 embodiments, the blended feedstock comprises less than about 100 g/L monosaccharides prior to contacting with the one or more biocatalysts. In some embodiments, the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides prior to contacting with the one or more biocatalysts. In some embodiments, the first biomass and the one or more sugars are combined in a ratio of from about 50:50 to 99:1 by volume or by weight:volume. In some embodiments, the first biomass and the one or more sugars are combined in a ratio of about 80:20 by volume or by weight:volume. In some embodiments, the first biomass and the one or more sugars are combined in a ratio of about 90:10 by volume or by weight:volume. In some embodiments, the one or more biocatalysts comprise one or more yeast strains, one or more bacterial strains, or a combination thereof In some embodiments, the one or more biocatalysts comprise Saccharomyces cerevisiae. In some embodiments, the one or more biocatalysts comprise an endoglucanase, an exoglucanase, a cellobiohydrolase, a cellulase, a beta-glucosidase, a glycoside hydrolase, a glycosyltransferase, a lyase, an esterase, a glucamylase, or a combination thereof [0010] Also provided herein are methods of producing one or more fermentation end products comprising: (a) combining a first biomass with a C6-enriched hydrolysate to produce a blended feedstock; (b) contacting the blended feedstock with one or more hydrolytic enzymes and/or one or more fermenting microorganisms; and (c) fermenting the first biomass and the C6-enriched hydrolysate for a time sufficient to produce one or more fermentation end-products from the blended feedstock. In some embodiments, the C6 enriched hydrolysate comprises monosaccharides produced from the pretreatment and/or hydrolysis of a second biomass. In some embodiments, a yield of at least one of the one or more fermentation end-products is increased relative to fermentation of the first biomass without the C6-enriched hydrolysate. In some embodiments, a yield of at least one of the one or more fermentation end-products is increased by about 1% to about 100% relative to fermentation of the first biomass without the C6-enriched hydrolysate. In some embodiments, a rate of production for at least one of the one or more fermentation end-products is increased relative to fermentation of the first biomass without the C6-enriched hydrolysate. In some embodiments, a rate of production for at least one of the one or more fermentation end products is increased by about 1% to about 100% relative to fermentation of the first biomass without the C6-enriched hydrolysate. In some embodiments, the one or more fermentation end-products comprise one or more alcohols. In some embodiments, the one or more fermentation end-products comprise ethanol. In some embodiments, a yield of one or more other products is decreased relative to fermentation of the C6-enriched hydrolysate without 17 WO 2013/120035 PCT/US2013/025457 the first biomass. In some embodiments, a yield of one or more other products is decreased by about 1% to about 100% relative to fermentation of the C6-enriched hydrolysate without the first biomass. In some embodiments, the one or more other products comprise one or more polyols or sugar alcohols. In some embodiments, the one or more other products comprise methanol, glycol, glycerol, erythritol, threitol, arabitol, xylitol, ribitol, mannitol, sorbitol, dulcitol, fucitol, iditol, inositol, volemitol, isomalt, maltitol, lactitol, polyglycitol, or a combination thereof. In some embodiments, the one or more other products comprise glycerol. In some embodiments, the first biomass comprises non-cellulosic sugars. In some embodiments, the first biomass comprises non-cellulosic oligosaccharides. In some embodiments, the first biomass comprises starch. In some embodiments, the first biomass comprises corn or corn mash, sugar cane, sugar beet, sugar palm, sweet sorghum, nypa palm, cassava, rice, milo, sorghum, sweet potato, wheat, molasses, or a combination thereof. In some embodiments, the second biomass comprises cellulose, hemicellulose, or lignocellulose. In some embodiments, the second biomass comprises corn, corn syrup, corn stover, corn cobs, molasses, silage, grass, straw, grain hulls, bagasse, distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof. In some embodiments, the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 50%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers. In some embodiments, the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 40%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers. In some embodiments, the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 30%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers. In some embodiments, the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 20%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers. In some embodiments, the C6-enriched hydrolysate comprises 18 WO 2013/120035 PCT/US2013/025457 monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 15%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers. In some embodiments, the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 10%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers. In some embodiments, the C6-enriched hydrolysate comprises less than about 50% C5 sugars. In some embodiments, the C6-enriched hydrolysate comprises less than about 40% C5 sugars. In some embodiments, the C6-enriched hydrolysate comprises less than about 30% C5 sugars. In some embodiments, the C6-enriched hydrolysate comprises less than about 20% C5 sugars. In some embodiments, the C6-enriched hydrolysate comprises less than about 10% C5 sugars. In some embodiments, the C6-enriched hydrolysate comprises from about 0.1% to about 10% C5 sugars. In some embodiments, the one or more fermenting microorganisms comprise one or more yeast strains, one or more bacterial strains, or a combination thereof. In some embodiments, at least one of the one or more fermenting microorganisms is Saccharomyces cerevisiae. In some embodiments, the one or more hydrolytic enzymes comprise an endoglucanase, an exoglucanase, a cellobiohydrolase, a cellulase, a beta glucosidase, a glycoside hydrolase, a glycosyltransferase, a lyase, an esterase, a glucamylase, or a combination thereof. In some embodiments, the blended feedstock comprises less than about 100 g/L monosaccharides prior to contacting with the one or more fermenting microorganisms and the one or more hydrolytic enzymes. In some embodiments, the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides prior to contacting with the one or more fermenting microorganisms and the one or more hydrolytic enzymes. In some embodiments, the first biomass and the C6-enriched hydrolysate are combined in a ratio of from about 50:50 to 99:1 by volume or by weight:volume. In some embodiments, the first biomass and the C6-enriched hydrolysate are combined in a ratio of about 80:20 by volume or by weight:volume. In some embodiments, the first biomass and the C6-enriched hydrolysate are combined in a ratio of about 90:10 by volume or by weight:volume. [0011] In another aspect, provided herein are methods of producing a C6-enriched hydrolysate comprising: (a) treating a biomass comprising cellulose and hemicellulose and/or lignin to solubilize the hemicellulose and/or lignin; (b) separating the solubilized hemicellulose and/or lignin from the cellulose; and (c) hydrolyzing the cellulose, thereby producing the C6-enriched hydrolysate. In some embodiments, the biomass comprising cellulose and hemicellulose and/or lignin comprises corn, corn syrup, corn stover, corn cobs, 19 WO 2013/120035 PCT/US2013/025457 molasses, silage, grass, straw, grain hulls, bagasse, distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof In some embodiments, the biomass comprises corn stover. In some embodiments, the treating comprises stream treatment, hot water treatment, dilute acid treatment, dilute base treatment, steam explosion, acid-catalyzed steam explosion, or a combination thereof In some embodiments, the treatment comprises steam treatment. In some embodiments, the treating is performed at a temperature of from about 175 to about 250 'C. In some embodiments, the treating is performed at a temperature of about 205 'C. In some embodiments, the treating is performed from about 1 minute to about 30 minutes. In some embodiments, the treating is performed for about 7.5 minutes. In some embodiments, the separating is performed using a filter press. In some embodiments, the separating step comprises washing the biomass with water. In some embodiments, the water is from about 25 to about 100 'C. In some embodiments, the water is about 50 'C. In some embodiments, the water is added in an amount from about 1 to about 5 L/kg of biomass (dry weight). In some embodiments, the water is added in an amount of about 3 L/kg of biomass (dry weight). In some embodiments, the hydrolyzing step comprises enzymatic hydrolysis with one or more enzymes. In some embodiments, the hydrolyzing step is performed at a pH of from about 3 to about 7. In some embodiments, the hydrolyzing step is performed at a pH of about 5. In some embodiments, the hydrolyzing step is performed in a slurry of from about 1 % to about 20% wt/wt biomass/water. In some embodiments, the hydrolyzing step is performed in a slurry of about 8% wt/wt biomass/water. In some embodiments, the hydrolyzing step is performed in a jacketed reactor. Some embodiments further comprise concentrating the C6-enriched hydrolysate. In some embodiments, the C6-enriched hydrolysate is concentrated by evaporation. In some embodiments, the C6-enriched hydrolysate is concentrated using a roto evaporator. In some embodiments, the C6-enriched hydrolysate is concentrated to a C6 sugar concentration of from about 100 g/L to about 500 g/L. In some embodiments, the C6 enriched hydrolysate is concentrated to a C6 sugar concentration of about 300 g/L. In some embodiments, the C6-enriched hydrolysate comprises less than about 50% C5 sugars. In some embodiments, the C6-enriched hydrolysate comprises less than about 40% C5 sugars. In some embodiments, the C6-enriched hydrolysate comprises less than about 30% C5 20 WO 2013/120035 PCT/US2013/025457 sugars. In some embodiments, the C6-enriched hydrolysate comprises less than about 20% C5 sugars. In some embodiments, the C6-enriched hydrolysate comprises less than about 10% C5 sugars. In some embodiments, the C6-enriched hydrolysate comprises from about 0. 1% to about 10% C5 sugars. [0012] Also provided are C6-enriched hydrolysates produced by any of the methods disclosed herein. [0013] Provided herein are methods of producing ethanol comprising: (a) combining a first biomass comprising starch with a C6-enriched hydrolysate to produce a blended feedstock, (i) wherein the C6-enriched hydrolysate comprises monosaccharides produced from the pretreatment and/or hydrolysis of a second biomass, (ii) wherein the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 20%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers, and (iii) wherein the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides; (b) contacting the blended feedstock with one or more fermenting microorganisms and one or more hydrolytic enzymes; and (c) fermenting the first biomass and the C6-enriched hydrolysate to produce ethanol from the blended feedstock, wherein an increase rate of production and/or yield of the ethanol is achieved relative to the hydrolysis and fermentation of the first biomass without the C6 enriched hydrolysate. Also provided are methods of producing ethanol comprising: (a) combining a first biomass comprising starch with a C6-enriched hydrolysate to produce a blended feedstock, (i) wherein the C6-enriched hydrolysate comprises monosaccharides produced from the pretreatment and/or hydrolysis of a second biomass, (ii) wherein the C6 enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 20%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers, and (iii) wherein the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides; (b) contacting the blended feedstock with one or more fermenting microorganisms and one or more hydrolytic enzymes; and (c) fermenting the first biomass and the C6-enriched hydrolysate to produce ethanol from the blended feedstock, wherein a yield of one or more polyols or sugar alcohols is decreased relative to fermentation of the C6 enriched hydrolysate alone. [0014] Ethanol produced by any of the methods disclosed herein is also provided. 21 WO 2013/120035 PCT/US2013/025457 INCORPORATION BY REFERENCE [0015] All publications, patents, and patent applications mentioned in this specification are herein incorporated by reference to the same extent as if each individual publication, patent, or patent application was specifically and individually indicated to be incorporated by reference. BRIEF DESCRIPTION OF THE DRAWINGS [0016] The novel features of the invention are set forth with particularity in the appended claims. A better understanding of the features and advantages of the present invention will be obtained by reference to the following detailed description that sets forth illustrative embodiments, in which the principles of the invention are utilized, and the accompanying drawings of which: [0017] Figure 1 is a graph illustrating the trajectory of how biomass is converted from solids into liquefied C6 sugars during hydrolysis using cellulase enzymes. [0018] Figure 2 is a graph illustrating the improvement in ethanol yield for fermentation of corn mash slurry spiked with various energy sorghum-derived sugar blends as compared to fermentation of corn mash slurry alone. [0019] Figure 3 is a graph of glucose concentration over time for a corn mash control feedstock as compared to a feedstock spiked with sugar from energy sorghum. [0020] Figure 4 is a graph comparing ethanol production for a corn mash control against corn mash spiked with energy sorghum sugars. [0021] Figure 5 is a graph illustrating the improvement in ethanol yield for a corn mash slurry spiked with switchgrass-derived sugar as compared to corn mash slurry alone. [0022] Figure 6 is a graph comparing glucose uptake for a glucose control as compared to a glucose solution spiked with energy sorghum solids and a glucose solution spiked with switchgrass solids. [0023] Figure 7 is a graph comparing ethanol production for a glucose control as compared to a glucose solution spiked with energy sorghum solids and a glucose solution spiked with switchgrass solids. [0024] Figure 8 is a graph comparing ethanol production from corn mash to ethanol production from a fed batch fermentation of a 90:10 blend of corn mash and cellulosic sugar with C5 fermenting yeast. [0025] Figure 9 is a graph comparing ethanol production from corn mash to ethanol production from a fed-batch fermentation of a 90:10 blend of corn mash and wheat straw cellulosic sugar at shake flask level. 22 WO 2013/120035 PCT/US2013/025457 [0026] Figure 10 is a graph comparing ethanol production from corn mash to ethanol production from a fed batch fermentation of a 90:10 blend of corn mash and cellulosic sugar with a C5 fermenting yeast. [0027] Figure 11 is a graph showing the increase in ethanol production in fed-batch fermentations compared to batch fermentations after 72 hours using a 90:10 and a 80:20 blend of corn mash and cellulosic sugars. [0028] Figure 12 (A&B) are progress curves showing mass loss (g) over time during fermentation of corn mash supplemented with varying levels of a C6 Saccharide Stream produced from corn stillage. The treatment IDs in the figure legends correspond to Table 9. [0029] Figure 13 is a chart showing the average mass loss due to carbon dioxide after fermentation of corn mash supplemented with varying levels of a C6 Saccharide Stream produced from corn stillage for 15.67 (dark grey bars) and 62 hours (light grey bars). Bars labeled with the same letter are not statistically different from one another at either 15.67 or 62 hours. Error bars represent one standard deviation of nine independent replicate fermentation flasks at 15.67 hours and three independent replicate fermentation flasks at 62 hours. The treatment IDs in the figure legend corresponds to Table 9. [0030] Figure 14 is a comparison of the average final concentrations of ethanol (left bars) and unfermented sugars as glucose equivalent (right bars) after fermentation of corn mash dosed with varying levels of a C6 Saccharide Stream produced from corn stillage for 62 hours as measured by HPLC. Error bars represent one standard deviation of three independent replicate fermentation flasks, except for QC which represents the standard deviation of six independent replicate flasks. Bars labeled with the same letter in each group are not statistically different from one another. [0031] Figure 15 is a dose-response graph, representing the dose of C6 Saccharide Stream produced from corn stillage versus glycerol concentration accumulated for all treatments identified in Table 9. The dashed lines represent the QC glycerol concentration. Error bars represent one standard deviation of three independent replicate fermentation flasks, except for QC which represents the standard deviation of six independent replicate flasks. [0032] Figure 16 shows the average final pH values after fermentation of corn mash dosed with varying levels of a C6 Saccharide Stream produced from corn stillage for 22 hours (diamonds), 46 hours (squares) and 62 hours (triangles). [0033] Figure 17 shows the average improvement in ethanol yield for corn mash fermentations dosed with varying levels of a C6 Saccharide Stream produced from corn stillage. 23 WO 2013/120035 PCT/US2013/025457 [0034] Figure 18 shows the average increase in ethanol yield (squares; left Y-axis) and residual sugars (triangles; right Y-axis) after fermentation of corn mash dosed with varying levels of a C6 Saccharide Stream produced from corn stillage. [0035] Figure 19 shows the average mass loss for fermentations of 80:20 blends of corn mass and a C6 Saccharide Stream produced from corn stover (squares) or stock sugar (diamonds). [0036] Figure 20 shows the average mass loss for fermentations of 80:20 blends of corn mass and a C6 Saccharide Stream produced from corn stover (squares) or stock sugar (diamonds). [0037] Figure 21 shows the shows the ethanol production rate kinetics throughout fermentation a 70:30 blend of corn mash and C6 Saccharide Stream (cellulosic-derived) (square) compared to corn mash alone (diamond). [0038] Figure 22 shows the shows the glycerol production rate kinetics throughout fermentation a 70:30 blend of corn mash and C6 Saccharide Stream (cellulosic-derived) (square) compared to corn mash alone (diamond). DETAILED DESCRIPTION OF THE INVENTION [0039] As used in the specification and the appended claims, the singular forms "a," "an" and "the" include plural referents unless the context clearly dictates otherwise. Thus, for example, reference to "a purified monomer" includes mixtures of two or more purified monomers. The term "comprising" as used herein is synonymous with "including," "containing," or "characterized by," and is inclusive or open-ended and does not exclude additional, unrecited elements or method steps. [0040] "About" means a referenced numeric indication plus or minus 10% of that referenced numeric indication. For example, the term about 4 would include a range of 3.6 to 4.4. All numbers expressing quantities of ingredients, reaction conditions, and so forth used in the specification are to be understood as being modified in all instances by the term "about." Accordingly, unless indicated to the contrary, the numerical parameters set forth herein are approximations that can vary depending upon the desired properties sought to be obtained. At the very least, and not as an attempt to limit the application of the doctrine of equivalents to the scope of any claims in any application claiming priority to the present application, each numerical parameter should be construed in light of the number of significant digits and ordinary rounding approaches. 24 WO 2013/120035 PCT/US2013/025457 [0041] Wherever the phrase "for example," "such as," "including" and the like are used herein, the phrase "and without limitation" is understood to follow unless explicitly stated otherwise. Therefore, "for example ethanol production" means "for example and without limitation ethanol production." [0042] In this specification and in the claims that follow, reference will be made to a number of terms which shall be defined to have the following meanings. [0043] Definitions [0044] "Optional" or "optionally" means that the subsequently described event or circumstance may or may not occur, and that the description includes instances where said event or circumstance occurs and instances where it does not. For example, the phrase "the medium can optionally contain glucose" means that the medium may or may not contain glucose as an ingredient and that the description includes both media containing glucose and media not containing glucose. [0045] Unless characterized otherwise, technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. [0046] " Fermentive end-product" and "fermentation end-product" are used interchangeably herein to include biofuels, chemicals, compounds suitable as liquid fuels, gaseous fuels, triacylglycerols (TAGs), reagents, chemical feedstocks, chemical additives, processing aids, food additives, bioplastiks and precursors to bioplastiks, and other products. Examples of fermentive end-products include but are not limited to 1,4 diacids (succinic, fumaric and malic), 2,5 furan dicarboxylic acid, 3 hydroxy propionic acid, aspartic acid, glucaric acid, glutamic acid, itaconic acid, levulinic acid, 3-hydroxybutyrolactone, glycerol, sorbitol, xylitol/arabinitol, butanediol, butanol, methane, methanol, ethane, ethene, ethanol, n-propane, 1-propene, 1-propanol, propanal, acetone, propionate, n-butane, 1-butene, 1-butanol, butanal, butanoate, isobutanal, isobutanol, 2-methylbutanal, 2-methylbutanol, 3-methylbutanal, 3 methylbutanol, 2-butene, 2-butanol, 2-butanone, 2,3-butanediol, 3-hydroxy-2-butanone, 2,3 butanedione, ethylbenzene, ethenylbenzene, 2-phenylethanol, phenylacetaldehyde, 1 phenylbutane, 4-phenyl-1-butene, 4-phenyl-2-butene, 1-phenyl-2-butene, 1-phenyl-2-butanol, 4-phenyl-2-butanol, 1-phenyl-2-butanone, 4-phenyl-2-butanone, 1-phenyl-2,3-butandiol, 1 phenyl-3-hydroxy-2-butanone, 4-phenyl-3-hydroxy-2-butanone, 1-phenyl-2,3-butanedione, n-pentane, ethylphenol, ethenylphenol, 2-(4-hydroxyphenyl)ethanol, 4 hydroxyphenylacetaldehyde, 1-(4-hydroxyphenyl) butane, 4-(4-hydroxyphenyl)-1-butene, 4 (4-hydroxyphenyl)-2-butene, 1-(4-hydroxyphenyl)-1-butene, 1-(4-hydroxyphenyl)-2-butanol, 4-(4-hydroxyphenyl)-2-butanol, 1-(4-hydroxyphenyl)-2-butanone, 4-(4-hydroxyphenyl)-2 25 WO 2013/120035 PCT/US2013/025457 butanone, 1-(4-hydroxyphenyl)-2,3-butandiol, 1-(4-hydroxyphenyl)-3-hydroxy-2-butanone, 4-(4-hydroxyphenyl)-3-hydroxy-2-butanone, 1-(4-hydroxyphenyl)-2,3-butanonedione, indolylethane, indolylethene, 2-(indole-3-)ethanol, n-pentane, 1-pentene, 1-pentanol, pentanal, pentanoate, 2-pentene, 2-pentanol, 3-pentanol, 2-pentanone, 3-pentanone, 4 methylpentanal, 4-methylpentanol, 2,3-pentanediol, 2-hydroxy-3-pentanone, 3-hydroxy-2 pentanone, 2,3-pentanedione, 2-methylpentane, 4-methyl-1-pentene, 4-methyl-2-pentene, 4 methyl-3-pentene, 4-methyl-2-pentanol, 2-methyl-3-pentanol, 4-methyl-2-pentanone, 2 methyl-3-pentanone, 4-methyl-2,3-pentanediol, 4-methyl-2-hydroxy-3-pentanone, 4-methyl 3-hydroxy-2-pentanone, 4-methyl-2,3-pentanedione, 1-phenylpentane, 1-phenyl-1-pentene, 1-phenyl-2-pentene, 1-phenyl-3-pentene, 1-phenyl-2-pentanol, 1-phenyl-3-pentanol, 1 phenyl-2-pentanone, 1-phenyl-3-pentanone, 1-phenyl-2,3-pentanediol, 1-phenyl-2-hydroxy 3-pentanone, 1-phenyl-3-hydroxy-2-pentanone, 1-phenyl-2,3-pentanedione, 4-methyl-i phenylpentane, 4-methyl-1-phenyl-1-pentene, 4-methyl-1-phenyl-2-pentene, 4-methyl-i phenyl-3-pentene, 4-methyl-1-phenyl-3-pentanol, 4-methyl-1-phenyl-2-pentanol, 4-methyl-i phenyl-3-pentanone, 4-methyl-1-phenyl-2-pentanone, 4-methyl-1-phenyl-2,3-pentanediol, 4 methyl-1-phenyl-2,3-pentanedione, 4-methyl-1-phenyl-3-hydroxy-2-pentanone, 4-methyl-1 phenyl-2-hydroxy-3-pentanone, 1-(4-hydroxyphenyl) pentane, 1-(4-hydroxyphenyl)-1 pentene, 1-(4-hydroxyphenyl)-2-pentene, 1-(4-hydroxyphenyl)-3-pentene, 1-(4 hydroxyphenyl)-2-pentanol, 1-(4-hydroxyphenyl)-3-pentanol, 1-(4-hydroxyphenyl)-2 pentanone, 1-(4-hydroxyphenyl)-3-pentanone, 1-(4-hydroxyphenyl)-2,3-pentanediol, 1-(4 hydroxyphenyl)-2-hydroxy-3-pentanone, 1-(4-hydroxyphenyl)-3-hydroxy-2-pentanone, 1-(4 hydroxyphenyl)-2,3-pentanedione, 4-methyl-1-(4-hydroxyphenyl) pentane, 4-methyl-1-(4 hydroxyphenyl)-2-pentene, 4-methyl-1-(4-hydroxyphenyl)-3-pentene, 4-methyl-1-(4 hydroxyphenyl)-1-pentene, 4-methyl-1-(4-hydroxyphenyl)-3-pentanol, 4-methyl-1-(4 hydroxyphenyl)-2-pentanol, 4-methyl-1-(4-hydroxyphenyl)-3-pentanone, 4-methyl-1-(4 hydroxyphenyl)-2-pentanone, 4-methyl-1-(4-hydroxyphenyl)-2,3-pentanediol, 4-methyl-1-(4 hydroxyphenyl)-2,3-pentanedione, 4-methyl-1-(4-hydroxyphenyl)-3-hydroxy-2-pentanone, 4 methyl-1-(4-hydroxyphenyl)-2-hydroxy-3-pentanone, 1-indole-3-pentane, 1-(indole-3)-1 pentene, 1-(indole-3)-2-pentene, 1-(indole-3)-3-pentene, 1-(indole-3)-2-pentanol, 1-(indole 3)-3-pentanol, 1-(indole-3)-2-pentanone, 1-(indole-3)-3-pentanone, 1-(indole-3)-2,3 pentanediol, 1-(indole-3)-2-hydroxy-3-pentanone, 1-(indole-3)-3-hydroxy-2-pentanone, 1 (indole-3)-2,3-pentanedione, 4-methyl-1-(indole-3-)pentane, 4-methyl-1-(indole-3)-2 pentene, 4-methyl-1-(indole-3)-3-pentene, 4-methyl-1-(indole-3)-1-pentene, 4-methyl-2 (indole-3)-3-pentanol, 4-methyl-1-(indole-3)-2-pentanol, 4-methyl-1-(indole-3)-3-pentanone, 26 WO 2013/120035 PCT/US2013/025457 4-methyl-1-(indole-3)-2-pentanone, 4-methyl-1-(indole-3)-2,3-pentanediol, 4-methyl-i (indole-3)-2,3-pentanedione, 4-methyl-1-(indole-3)-3-hydroxy-2-pentanone, 4-methyl-i (indole-3)-2-hydroxy-3-pentanone, n-hexane, 1-hexene, 1-hexanol, hexanal, hexanoate, 2 hexene, 3-hexene, 2-hexanol, 3-hexanol, 2-hexanone, 3-hexanone, 2,3-hexanediol, 2,3 hexanedione, 3,4-hexanediol, 3,4-hexanedione, 2-hydroxy-3-hexanone, 3-hydroxy-2 hexanone, 3-hydroxy-4-hexanone, 4-hydroxy-3-hexanone, 2-methylhexane, 3-methylhexane, 2-methyl-2-hexene, 2-methyl-3-hexene, 5-methyl-1-hexene, 5-methyl-2-hexene, 4-methyl-1 hexene, 4-methyl-2-hexene, 3-methyl-3-hexene, 3-methyl-2-hexene, 3-methyl-1-hexene, 2 methyl-3-hexanol, 5-methyl-2-hexanol, 5-methyl-3-hexanol, 2-methyl-3-hexanone, 5-methyl 2-hexanone, 5-methyl-3-hexanone, 2-methyl-3,4-hexanediol, 2-methyl-3,4-hexanedione, 5 methyl-2,3-hexanediol, 5-methyl-2,3-hexanedione, 4-methyl-2,3-hexanediol, 4-methyl-2,3 hexanedione, 2-methyl-3-hydroxy-4-hexanone, 2-methyl-4-hydroxy-3-hexanone, 5-methyl-2 hydroxy-3-hexanone, 5-methyl-3-hydroxy-2-hexanone, 4-methyl-2-hydroxy-3-hexanone, 4 methyl-3-hydroxy-2-hexanone, 2,5-dimethylhexane, 2,5-dimethyl-2-hexene, 2,5-dimethyl-3 hexene, 2,5-dimethyl-3-hexanol, 2,5-dimethyl-3-hexanone, 2,5-dimethyl-3,4-hexanediol, 2,5 dimethyl-3,4-hexanedione, 2,5-dimethyl-3-hydroxy-4-hexanone, 5-methyl-1-phenylhexane, 4-methyl-1-phenylhexane, 5-methyl-1-phenyl-1-hexene, 5-methyl-1-phenyl-2-hexene, 5 methyl-1-phenyl-3-hexene, 4-methyl-1-phenyl-1-hexene, 4-methyl-1-phenyl-2-hexene, 4 methyl-1-phenyl-3-hexene, 5-methyl-1-phenyl-2-hexanol, 5-methyl-1-phenyl-3-hexanol, 4 methyl-1-phenyl-2-hexanol, 4-methyl-1-phenyl-3-hexanol, 5-methyl-1-phenyl-2-hexanone, 5-methyl-1-phenyl-3-hexanone, 4-methyl-1-phenyl-2-hexanone, 4-methyl-1-phenyl-3 hexanone, 5-methyl-1-phenyl-2,3-hexanediol, 4-methyl-1-phenyl-2,3-hexanediol, 5-methyl i-phenyl-3-hydroxy-2-hexanone, 5-methyl-1-phenyl-2-hydroxy-3-hexanone, 4-methyl-1 phenyl-3-hydroxy-2-hexanone, 4-methyl-1-phenyl-2-hydroxy-3-hexanone, 5-methyl-1 phenyl-2,3-hexanedione, 4-methyl-1-phenyl-2,3-hexanedione, 4-methyl-1-(4 hydroxyphenyl)hexane, 5-methyl-1-(4-hydroxyphenyl)-1-hexene, 5-methyl-1-(4 hydroxyphenyl)-2-hexene, 5-methyl-1-(4-hydroxyphenyl)-3-hexene, 4-methyl-1-(4 hydroxyphenyl)-1-hexene, 4-methyl-1-(4-hydroxyphenyl)-2-hexene, 4-methyl-1-(4 hydroxyphenyl)-3-hexene, 5-methyl-1-(4-hydroxyphenyl)-2-hexanol, 5-methyl-1-(4 hydroxyphenyl)-3-hexanol, 4-methyl-1-(4-hydroxyphenyl)-2-hexanol, 4-methyl-1-(4 hydroxyphenyl)-3-hexanol, 5-methyl-1-(4-hydroxyphenyl)-2-hexanone, 5-methyl-1-(4 hydroxyphenyl)-3-hexanone, 4-methyl-1-(4-hydroxyphenyl)-2-hexanone, 4-methyl-1-(4 hydroxyphenyl)-3-hexanone, 5-methyl-1-(4-hydroxyphenyl)-2,3-hexanediol, 4-methyl-1-(4 hydroxyphenyl)-2,3-hexanediol, 5-methyl-1-(4-hydroxyphenyl)-3-hydroxy-2-hexanone, 5 27 WO 2013/120035 PCT/US2013/025457 methyl-1-(4-hydroxyphenyl)-2-hydroxy-3-hexanone, 4-methyl-1-(4-hydroxyphenyl)-3 hydroxy-2-hexanone, 4-methyl-1-(4-hydroxyphenyl)-2-hydroxy-3-hexanone, 5-methyl-1-(4 hydroxyphenyl)-2,3-hexanedione, 4-methyl-1-(4-hydroxyphenyl)-2,3-hexanedione, 4-methyl 1-(indole-3-)hexane, 5-methyl-1-(indole-3)-1-hexene, 5-methyl-1-(indole-3)-2-hexene, 5 methyl-1-(indole-3)-3-hexene, 4-methyl-1-(indole-3)-1-hexene, 4-methyl-1-(indole-3)-2 hexene, 4-methyl-1-(indole-3)-3-hexene, 5-methyl-1-(indole-3)-2-hexanol, 5-methyl-1 (indole-3)-3-hexanol, 4-methyl-1-(indole-3)-2-hexanol, 4-methyl-1-(indole-3)-3-hexanol, 5 methyl-1-(indole-3)-2-hexanone, 5-methyl-1-(indole-3)-3-hexanone, 4-methyl-1-(indole-3) 2-hexanone, 4-methyl-1-(indole-3)-3-hexanone, 5-methyl-1-(indole-3)-2,3-hexanediol, 4 methyl-1-(indole-3)-2,3-hexanediol, 5-methyl-1-(indole-3)-3-hydroxy-2-hexanone, 5-methyl 1-(indole-3)-2-hydroxy-3-hexanone, 4-methyl-1-(indole-3)-3-hydroxy-2-hexanone, 4-methyl 1-(indole-3)-2-hydroxy-3-hexanone, 5-methyl-1-(indole-3)-2,3-hexanedione, 4-methyl-1 (indole-3)-2,3-hexanedione, n-heptane, i-heptene, i-heptanol, heptanal, heptanoate, 2 heptene, 3-heptene, 2-heptanol, 3-heptanol, 4-heptanol, 2-heptanone, 3-heptanone, 4 heptanone, 2,3-heptanediol, 2,3-heptanedione, 3,4-heptanediol, 3,4-heptanedione, 2-hydroxy 3-heptanone, 3-hydroxy-2-heptanone, 3-hydroxy-4-heptanone, 4-hydroxy-3-heptanone, 2 methylheptane, 3-methylheptane, 6-methyl-2-heptene, 6-methyl-3-heptene, 2-methyl-3 heptene, 2-methyl-2-heptene, 5-methyl-2-heptene, 5-methyl-3-heptene, 3-methyl-3-heptene, 2-methyl-3-heptanol, 2-methyl-4-heptanol, 6-methyl-3-heptanol, 5-methyl-3-heptanol, 3 methyl-4-heptanol, 2-methyl-3-heptanone, 2-methyl-4-heptanone, 6-methyl-3-heptanone, 5 methyl-3-heptanone, 3-methyl-4-heptanone, 2-methyl-3,4-heptanediol, 2-methyl-3,4 heptanedione, 6-methyl-3,4-heptanediol, 6-methyl-3,4-heptanedione, 5-methyl-3,4 heptanediol, 5-methyl-3,4-heptanedione, 2-methyl-3-hydroxy-4-heptanone, 2-methyl-4 hydroxy-3-heptanone, 6-methyl-3-hydroxy-4-heptanone, 6-methyl-4-hydroxy-3-heptanone, 5-methyl-3-hydroxy-4-heptanone, 5-methyl-4-hydroxy-3-heptanone, 2,6-dimethylheptane, 2,5-dimethylheptane, 2,6-dimethyl-2-heptene, 2,6-dimethyl-3-heptene, 2,5-dimethyl-2 heptene, 2,5-dimethyl-3-heptene, 3,6-dimethyl-3-heptene, 2,6-dimethyl-3-heptanol, 2,6 dimethyl-4-heptanol, 2,5-dimethyl-3-heptanol, 2,5-dimethyl-4-heptanol, 2,6-dimethyl-3,4 heptanediol, 2,6-dimethyl-3,4-heptanedione, 2,5-dimethyl-3,4-heptanediol, 2,5-dimethyl-3,4 heptanedione, 2,6-dimethyl-3-hydroxy-4-heptanone, 2,6-dimethyl-4-hydroxy-3-heptanone, 2,5-dimethyl-3-hydroxy-4-heptanone, 2,5-dimethyl-4-hydroxy-3-heptanone, n-octane, I octene, 2-octene, i-octanol, octanal, octanoate, 3-octene, 4-octene, 4-octanol, 4-octanone, 4,5-octanediol, 4,5-octanedione, 4-hydroxy-5-octanone, 2-methyloctane, 2-methyl-3-octene, 2-methyl-4-octene, 7-methyl-3-octene, 3-methyl-3-octene, 3-methyl-4-octene, 6-methyl-3 28 WO 2013/120035 PCT/US2013/025457 octene, 2-methyl-4-octanol, 7-methyl-4-octanol, 3-methyl-4-octanol, 6-methyl-4-octanol, 2 methyl-4-octanone, 7-methyl-4-octanone, 3-methyl-4-octanone, 6-methyl-4-octanone, 2 methyl-4,5-octanediol, 2-methyl-4,5-octanedione, 3-methyl-4,5-octanediol, 3-methyl-4,5 octanedione, 2-methyl-4-hydroxy-5-octanone, 2-methyl-5-hydroxy-4-octanone, 3-methyl-4 hydroxy-5-octanone, 3-methyl-5-hydroxy-4-octanone, 2,7-dimethyloctane, 2,7-dimethyl-3 octene, 2,7-dimethyl-4-octene, 2,7-dimethyl-4-octanol, 2,7-dimethyl-4-octanone, 2,7 dimethyl-4,5-octanediol, 2,7-dimethyl-4,5-octanedione, 2,7-dimethyl-4-hydroxy-5-octanone, 2,6-dimethyloctane, 2,6-dimethyl-3-octene, 2,6-dimethyl-4-octene, 3,7-dimethyl-3-octene, 2,6-dimethyl-4-octanol, 3,7-dimethyl-4-octanol, 2,6-dimethyl-4-octanone, 3,7-dimethyl-4 octanone, 2,6-dimethyl-4,5-octanediol, 2,6-dimethyl-4,5-octanedione, 2,6-dimethyl-4 hydroxy-5-octanone, 2,6-dimethyl-5-hydroxy-4-octanone, 3,6-dimethyloctane, 3,6-dimethyl 3-octene, 3,6-dimethyl-4-octene, 3,6-dimethyl-4-octanol, 3,6-dimethyl-4-octanone, 3,6 dimethyl-4,5-octanediol, 3,6-dimethyl-4,5-octanedione, 3,6-dimethyl-4-hydroxy-5-octanone, n-nonane, 1-nonene, 1-nonanol, nonanal, nonanoate, 2-methylnonane, 2-methyl-4-nonene, 2 methyl-5-nonene, 8-methyl-4-nonene, 2-methyl-5-nonanol, 8-methyl-4-nonanol, 2-methyl-5 nonanone, 8-methyl-4-nonanone, 8-methyl-4,5-nonanediol, 8-methyl-4,5-nonanedione, 8 methyl-4-hydroxy-5-nonanone, 8-methyl-5-hydroxy-4-nonanone, 2,8-dimethylnonane, 2,8 dimethyl-3-nonene, 2,8-dimethyl-4-nonene, 2,8-dimethyl-5-nonene, 2,8-dimethyl-4-nonanol, 2,8-dimethyl-5-nonanol, 2,8-dimethyl-4-nonanone, 2,8-dimethyl-5-nonanone, 2,8-dimethyl 4,5-nonanediol, 2,8-dimethyl-4,5-nonanedione, 2,8-dimethyl-4-hydroxy-5-nonanone, 2,8 dimethyl-5-hydroxy-4-nonanone, 2,7-dimethylnonane, 3,8-dimethyl-3-nonene, 3,8-dimethyl 4-nonene, 3,8-dimethyl-5-nonene, 3,8-dimethyl-4-nonanol, 3,8-dimethyl-5-nonanol, 3,8 dimethyl-4-nonanone, 3,8-dimethyl-5-nonanone, 3,8-dimethyl-4,5-nonanediol, 3,8-dimethyl 4,5-nonanedione, 3,8-dimethyl-4-hydroxy-5-nonanone, 3,8-dimethyl-5-hydroxy-4-nonanone, n-decane, 1-decene, 1-decanol, decanoate, 2,9-dimethyldecane, 2,9-dimethyl-3-decene, 2,9 dimethyl-4-decene, 2,9-dimethyl-5-decanol, 2,9-dimethyl-5-decanone, 2,9-dimethyl-5,6 decanediol, 2,9-dimethyl-6-hydroxy-5-decanone, 2,9-dimethyl-5,6-decanedionen-undecane, 1-undecene, 1-undecanol, undecanal. undecanoate, n-dodecane, 1-dodecene, 1-dodecanol, dodecanal, dodecanoate, n-dodecane, 1-decadecene, n-tridecane, 1-tridecene, 1-tridecanol, tridecanal, tridecanoate, n-tetradecane, 1-tetradecene, 1-tetradecanol, tetradecanal, tetradecanoate, n-pentadecane, 1-pentadecene, 1-pentadecanol, pentadecanal, pentadecanoate, n-hexadecane, 1-hexadecene, 1-hexadecanol, hexadecanal, hexadecanoate, n-heptadecane, 1 heptadecene, 1-heptadecanol, heptadecanal, heptadecanoate, n-octadecane, 1-octadecene, 1 octadecanol, octadecanal, octadecanoate, n-nonadecane, 1-nonadecene, 1-nonadecanol, 29 WO 2013/120035 PCT/US2013/025457 nonadecanal, nonadecanoate, eicosane, 1-eicosene, 1-eicosanol, eicosanal, eicosanoate, 3 hydroxy propanal, 1,3-propanediol, 4-hydroxybutanal, 1,4-butanediol, 3-hydroxy-2-butanone, 2,3-butandiol, 1,5-pentane diol, homocitrate, homoisocitorate, b-hydroxy adipate, glutarate, glutarsemialdehyde, glutaraldehyde, 2-hydroxy-1-cyclopentanone, 1,2-cyclopentanediol, cyclopentanone, cyclopentanol, (S)-2-acetolactate, (R)-2,3-Dihydroxy-isovalerate, 2 oxoisovalerate, isobutyryl-CoA, isobutyrate, isobutyraldehyde, 5-amino pentaldehyde, 1,10 diaminodecane, 1,10-diamino-5-decene, 1,10-diamino-5-hydroxydecane, 1,10-diamino-5 decanone, 1,10-diamino-5,6-decanediol, 1,10-diamino-6-hydroxy-5-decanone, phenylacetoaldehyde, 1,4-diphenylbutane, 1,4-diphenyl-1-butene, 1,4-diphenyl-2-butene, 1,4 diphenyl-2-butanol, 1,4-diphenyl-2-butanone, 1,4-diphenyl-2,3-butanediol, 1,4-diphenyl-3 hydroxy-2-butanone, 1-(4-hydeoxyphenyl)-4-phenylbutane, 1-(4-hydeoxyphenyl)-4-phenyl 1-butene, 1-(4-hydeoxyphenyl)-4-phenyl-2-butene, 1-(4-hydeoxyphenyl)-4-phenyl-2-butanol, 1-(4-hydeoxyphenyl)-4-phenyl-2-butanone, 1-(4-hydeoxyphenyl)-4-phenyl-2,3-butanediol, 1 (4-hydeoxyphenyl)-4-phenyl-3-hydroxy-2-butanone, 1-(indole-3)-4-phenylbutane, 1-(indole 3)-4-phenyl-1-butene, 1-(indole-3)-4-phenyl-2-butene, 1-(indole-3)-4-phenyl-2-butanol, 1 (indole-3)-4-phenyl-2-butanone, 1-(indole-3)-4-phenyl-2,3-butanediol, 1-(indole-3)-4 phenyl-3-hydroxy-2-butanone, 4-hydroxyphenylacetoaldehyde, 1,4-di(4 hydroxyphenyl)butane, 1,4-di(4-hydroxyphenyl)-1-butene, 1,4-di(4-hydroxyphenyl)-2 butene, 1,4-di(4-hydroxyphenyl)-2-butanol, 1,4-di(4-hydroxyphenyl)-2-butanone, 1,4-di(4 hydroxyphenyl)-2,3-butanediol, 1,4-di(4-hydroxyphenyl)-3-hydroxy-2-butanone, 1-(4 hydroxyphenyl)-4-(indo le-3 -)butane, 1-(4-hydroxyphenyl)-4-(indole-3)-1-butene, 1-di(4 hydroxyphenyl)-4-(indole-3)-2-butene, 1-(4-hydroxyphenyl)-4-(indole-3)-2-butanol, 1-(4 hydroxyphenyl)-4-(indole-3)-2-butanone, 1-(4-hydroxyphenyl)-4-(indole-3)-2,3-butanediol, 1-(4-hydroxyphenyl-4-(indole-3)-3-hydroxy-2-butanone, indole-3-acetoaldehyde, 1,4 di(indole-3-)butane, 1,4-di(indole-3)-1-butene, 1,4-di(indole-3)-2-butene, 1,4-di(indole-3)-2 butanol, 1,4-di(indole-3)-2-butanone, 1,4-di(indole-3)-2,3-butanediol, 1,4-di(indole-3)-3 hydroxy-2-butanone, succinate semialdehyde, hexane-1,8-dicarboxylic acid, 3-hexene-1,8 dicarboxylic acid, 3-hydroxy-hexane-1,8-dicarboxylic acid, 3-hexanone-1,8-dicarboxylic acid, 3,4-hexanediol-1,8-dicarboxylic acid, 4-hydroxy-3-hexanone-1,8-dicarboxylic acid, glycerol, fucoidan, iodine, chlorophyll, carotenoid, calcium, magnesium, iron, sodium, potassium, phosphate, lactic acid, acetic acid, formic acid, isoprenoids, and polyisoprenes, including rubber. Further, such products can include succinic acid, pyruvic acid, enzymes such as cellulases, polysaccharases, lipases, proteases, ligninases, and hemicellulases and may be present as a pure compound, a mixture, or an impure or diluted form. 30 WO 2013/120035 PCT/US2013/025457 [0047] Fermentation end-products can include polyols or sugar alcohols; for example, methanol, glycol, glycerol, erythritol, threitol, arabitol, xylitol, ribitol, mannitol, sorbitol, dulcitol, fucitol, iditol, inositol, volemitol, isomalt, maltitol, lactitol, and/or polyglycitol. [0048] The term "fatty acid comprising material" as used herein has its ordinary meaning as known to those skilled in the art and can comprise one or more chemical compounds that include one or more fatty acid moieties as well as derivatives of these compounds and materials that comprise one or more of these compounds. Common examples of compounds that include one or more fatty acid moieties include triacylglycerides, diacylglycerides, monoacylglycerides, phospholipids, lysophospholipids, free fatty acids, fatty acid salts, soaps, fatty acid comprising amides, esters of fatty acids and monohydric alcohols, esters of fatty acids and polyhydric alcohols including glycols (e.g. ethylene glycol, propylene glycol, etc.), esters of fatty acids and polyethylene glycol, esters of fatty acids and polyethers, esters of fatty acids and polyglycol, esters of fatty acids and saccharides, esters of fatty acids with other hydroxyl-containing compounds, etc. A fatty acid comprising material can be one or more of these compounds in an isolated or purified form. It can be a material that includes one or more of these compounds that is combined or blended with other similar or different materials. It can be a material where the fatty acid comprising material occurs with or is provided with other similar or different materials, such as vegetable and animal oils; mixtures of vegetable and animal oils; vegetable and animal oil byproducts; mixtures of vegetable and animal oil byproducts; vegetable and animal wax esters; mixtures, derivatives and byproducts of vegetable and animal wax esters; seeds; processed seeds; seed byproducts; nuts; processed nuts; nut byproducts; animal matter; processed animal matter; byproducts of animal matter; corn; processed corn; corn byproducts; distiller's grains; beans; processed beans; bean byproducts; soy products; lipid containing plant, fish or animal matter; processed lipid containing plant or animal matter; byproducts of lipid containing plant, fish or animal matter; lipid containing microbial material; processed lipid containing microbial material; and byproducts of lipid containing microbial matter. Such materials can be utilized in liquid or solid forms. Solid forms include whole forms, such as cells, beans, and seeds; ground, chopped, slurried, extracted, flaked, milled, etc. The fatty acid portion of the fatty acid comprising compound can be a simple fatty acid, such as one that includes a carboxyl group attached to a substituted or un-substituted alkyl group. The substituted or unsubstituted alkyl group can be straight or branched, saturated or unsaturated. Substitutions on the alkyl group can include hydroxyls, phosphates, halogens, alkoxy, or aryl groups. The substituted or unsubstituted alkyl group can have 7 to 29 carbons and preferably 11 to 23 carbons (e.g., 8 to 31 WO 2013/120035 PCT/US2013/025457 30 carbons and preferably 12 to 24 carbons counting the carboxyl group) arranged in a linear chain with or without side chains and/or substitutions. Addition of the fatty acid comprising compound can be by way of adding a material comprising the fatty acid comprising compound. [0049] The term "pH modifier" as used herein has its ordinary meaning as known to those skilled in the art and can include any material that will tend to increase, decrease or hold steady the pH of the broth or medium. A pH modifier can be an acid, a base, a buffer, or a material that reacts with other materials present to serve to raise, lower, or hold steady the pH. In one embodiment, more than one pH modifier can be used, such as more than one acid, more than one base, one or more acid with one or more bases, one or more acids with one or more buffers, one or more bases with one or more buffers, or one or more acids with one or more bases with one or more buffers. In one embodiment, a buffer can be produced in the broth or medium or separately and used as an ingredient by at least partially reacting in acid or base with a base or an acid, respectively. When more than one pH modifiers are utilized, they can be added at the same time or at different times. In one embodiment, one or more acids and one or more bases are combined, resulting in a buffer. In one embodiment, media components, such as a carbon source or a nitrogen source serve as a pH modifier; suitable media components include those with high or low pH or those with buffering capacity. Exemplary media components include acid- or base-hydrolyzed plant polysaccharides having residual acid or base, ammonia fiber explosion (AFEX) treated plant material with residual ammonia, lactic acid, corn steep solids or liquor. [0050] "Growth phase" is used herein to describe the type of cellular growth that occurs after the "Initiation phase" and before the "Stationary phase" and the "Death phase." The growth phase is sometimes referred to as the exponential phase or log phase or logarithmic phase. [0051] The term "plant polysaccharide" as used herein has its ordinary meaning as known to those skilled in the art and can comprise one or more polymers of sugars and sugar derivatives as well as derivatives of sugar polymers and/or other polymeric materials that occur in plant matter. Exemplary plant polysaccharides include lignin, cellulose, starch, pectin, and hemicellulose. Others are chitin, sulfonated polysaccharides such as alginic acid, agarose, carrageenan, porphyran, furcelleran and funoran. Generally, the polysaccharide can have two or more sugar units or derivatives of sugar units. The sugar units and/or derivatives of sugar units can repeat in a regular pattern, or otherwise. The sugar units can be hexose units or pentose units, or combinations of these. The derivatives of sugar units can be sugar alcohols, sugar acids, amino sugars, etc. The polysaccharides can be linear, branched, cross 32 WO 2013/120035 PCT/US2013/025457 linked, or a mixture thereof One type or class of polysaccharide can be cross-linked to another type or class of polysaccharide. The concentration of saccharides in a biomass containing plant polysaccharides such as cellulose, hemicellulose, starch, or pectin can be given in terms of monosaccharide equivalents. A monosaccharide equivalent concentration is the concentration of saccharides assuming complete hydrolysis of polysaccharides to monosaccharides. [0052] The term "saccharification" as used herein has its ordinary meaning as known to those skilled in the art and can include conversion of plant polysaccharides to lower molecular weight species that can be utilized by the organism at hand. For some organisms, this would include conversion to monosaccharides, disaccharides, trisaccharides, and oligosaccharides of up to about seven monomer units, as well as similar sized chains of sugar derivatives and combinations of sugars and sugar derivatives. [0053] The terms "SSF" and "SHF" are known to those skilled in the art; SSF meaning simultaneous saccharification and fermentation, or the conversion from polysaccharides or oligosaccharides into monosaccharides at the same time and in the same fermentation vessel wherein monosaccharides are converted to another chemical product such as ethanol. "SHF" indicates a physical separation of the polymer hydrolysis or saccharification and fermentation processes. [0054] The term "biomass" as used herein has its ordinary meaning as known to those skilled in the art and can include one or more biological materials that can be converted into a biofuel, chemical or other product. Biomass as used herein is synonymous with the term "feedstock" and includes corn syrup, molasses, silage, agricultural residues (corn stalks, grass, straw, grain hulls, bagasse, etc.), animal waste (manure from cattle, poultry, and hogs), Distillers Dried Solubles (DDS), Distillers Dried Grains (DDG), Condensed Distillers Solubles (CDS), Distillers Wet Grains (DWG), Distillers Dried Grains with Solubles (DDGS), woody materials (wood or bark, sawdust, timber slash, and mill scrap), municipal waste (waste paper, recycled toilet papers, yard clippings, etc.), and energy crops (poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, including macroalgae, etc.). One exemplary source of biomass is plant matter. Plant matter can be, for example, woody plant matter, non-woody plant matter, cellulosic material, lignocellulosic material, hemicellulosic material, carbohydrates, pectin, starch, inulin, fructans, glucans, corn, sugar cane, grasses, switchgrass, sorghum, high biomass sorghum, bamboo, algae and material derived from these. Plants can be in their natural state or genetically modified, e.g., to increase the cellulosic or hemicellulosic portion of the cell wall, or to produce additional exogenous or 33 WO 2013/120035 PCT/US2013/025457 endogenous enzymes to increase the separation of cell wall components. Plant matter can also include plant cell culture or plant cell tissue culture. Plant matter can be further described by reference to the chemical species present, such as proteins, polysaccharides and oils. Polysaccharides include polymers of various monosaccharides and derivatives of monosaccharides including glucose, fructose, lactose, galacturonic acid, rhamnose, etc. Plant matter also includes agricultural waste byproducts or side streams such as pomace, corn steep liquor, corn steep solids, distillers grains, peels, pits, fermentation waste, straw, lumber, sewage, garbage and food leftovers. Peels can be citrus which include, but are not limited to, tangerine peel, grapefruit peel, orange peel, tangerine peel, lime peel and lemon peel. These materials can come from farms, forestry, industrial sources, households, etc. Another non limiting example of biomass is animal matter, including, for example milk, meat, fat, animal processing waste, and animal waste. "Feedstock" is frequently used to refer to biomass being used for a process, such as those described herein. [0055] "Broth" is used herein to refer to inoculated medium at any stage of growth, including the point immediately after inoculation and the period after any or all cellular activity has ceased and can include the material after post-fermentation processing. It includes the entire contents of the combination of soluble and insoluble matter, suspended matter, cells and medium, as appropriate. [0056] The term "productivity" as used herein has its ordinary meaning as known to those skilled in the art and can include the mass of a material of interest produced in a given time in a given volume. Units can be, for example, grams per liter-hour, or some other combination of mass, volume, and time. Infermentation, productivity is frequently used to characterize how fast a product can be made within a given fermentation volume. The volume can be referenced to the total volume of the fermentation vessel, the working volume of the fermentation vessel, or the actual volume of broth being fermented. The context of the phrase will indicate the meaning intended to one of skill in the art. Productivity is different from "titer" in that productivity includes a time term, and titer is analogous to concentration. Titer and Productivity can generally be measured at any time during the fermentation, such as at the beginning, the end, or at some intermediate time, with titer relating the amount of a particular material present or produced at the point in time of interest and the productivity relating the amount of a particular material produced per liter in a given amount of time. The amount of time used in the productivity determination can be from the beginning of the fermentation or from some other time, and go to the end of the fermentation, such as when no additional material is produced or when harvest occurs, or some other time as indicated by 34 WO 2013/120035 PCT/US2013/025457 the context of the use of the term. "Overall productivity" refers to the productivity determined by utilizing the final titer and the overall fermentation time. [0057] "Titer" refers to the amount of a particular material present in a fermentation broth. It is similar to concentration and can refer to the amount of material made by the organism in the broth from all fermentation cycles, or the amount of material made in the current fermentation cycle or over a given period of time, or the amount of material present from whatever source, such as produced by the organism or added to the broth. Frequently, the titer of soluble species will be referenced to the liquid portion of the broth, with insolubles removed, and the titer of insoluble species will be referenced to the total amount of broth with insoluble species being present, however, the titer of soluble species can be referenced to the total broth volume and the titer of insoluble species can be referenced to the liquid portion, with the context indicating the which system is used with both reference systems intended in some cases. Frequently, the value determined referenced to one system will be the same or a sufficient approximation of the value referenced to the other. [0058] "Concentration" when referring to material in the broth generally refers to the amount of a material present from all sources, whether made by the organism or added to the broth. Concentration can refer to soluble species or insoluble species, and is referenced to either the liquid portion of the broth or the total volume of the broth, as for "titer." [0059] The term "biocatalyst" as used herein has its ordinary meaning as known to those skilled in the art and can include one or more enzymes and/or microorganisms, including solutions, suspensions, and mixtures of enzymes and microorganisms. In some contexts this word will refer to the possible use of either enzymes or microorganisms to serve a particular function, in other contexts the word will refer to the combined use of the two, and in other contexts the word will refer to only one of the two. The context of the phrase will indicate the meaning intended to one of skill in the art. For example, a biocatalyst can be a fermenting microorganism. The term biocatalyst includes fermenting microorganisms such as yeast, bacteria, or algae. [0060] The terms "conversion efficiency" or "yield" as used herein have their ordinary meaning as known to those skilled in the art and can include the mass of product made from a mass of substrate. The term can be expressed as a percentage yield of the product from a starting mass of substrate. For the production of ethanol from glucose, the net reaction is generally accepted as:

C

6

H

12 0 6 -> 2 C 2

H

5 OH + 2 CO 2 35 WO 2013/120035 PCT/US2013/025457 and the theoretical maximum conversion efficiency, or yield, is 510% (wt.). Frequently, the conversion efficiency will be referenced to the theoretical maximum, for example, "80% of the theoretical maximum." In the case of conversion of glucose to ethanol, this statement would indicate a conversion efficiency of 41% (wt.). The context of the phrase will indicate the substrate and product intended to one of skill in the art. [0061] "Pretreatment" or "pretreated" is used herein to refer to any mechanical, chemical, thermal, biochemical process or combination of these processes whether in a combined step or performed sequentially, that achieves disruption or expansion of the biomass so as to render the biomass more susceptible to attack by enzymes and/or microbes. In one embodiment, pretreatment includes removal or disruption of lignin so as to make the cellulose and hemicellulose polymers in the plant biomass more available to cellulolytic enzymes and/or microbes, for example, by treatment with acid or base. In one embodiment, pretreatment includes disruption or expansion of cellulosic and/or hemicellulosic material. Steam explosion, and ammonia fiber expansion (or explosion) (AFEX) are well known thermal/chemical techniques. Hydrolysis, including methods that utilize acids, bases, and/or enzymes can be used. Other thermal, chemical, biochemical, enzymatic techniques can also be used. [0062] "Fed-batch" or "fed-batch fermentation" is used herein to include methods of culturing microorganisms where nutrients, other medium components, or biocatalysts (including, for example, enzymes, fresh organisms, extracellular broth, genetically modified plants and/or organisms, etc.) are supplied to the fermentor during cultivation, but culture broth is not harvested from the fermentor until the end of the fermentation, although it can also include "self seeding" or "partial harvest" techniques where a portion of the fermentor volume is harvested and then fresh medium is added to the remaining broth in the fermentor, with at least a portion of the inoculum being the broth that was left in the fermentor. During a fed-batch fermentation, the broth volume can increase, at least for a period, by adding medium or nutrients to the broth while fermentation organisms are present. Suitable nutrients which can be utilized include those that are soluble, insoluble, and partially soluble, including gasses, liquids and solids. In one embodiment, a fed-batch process is referred to with a phrase such as, "fed-batch with cell augmentation." This phrase can include an operation where nutrients and cells are added or one where cells with no substantial amount of nutrients are added. The more general phrase "fed-batch" encompasses these operations as well. The context where any of these phrases is used will indicate to one of skill in the art the techniques being considered. 36 WO 2013/120035 PCT/US2013/025457 [0063] "Sugar compounds" or "sugar streams" is used herein to indicate mostly monosaccharide sugars, dissolved, crystallized, evaporated, or partially dissolved, including but not limited to hexoses and pentoses; sugar alcohols; sugar acids; sugar amines; compounds containing two or more of these linked together directly or indirectly through covalent or ionic bonds; and mixtures thereof Included within this description are disaccharides; trisaccharides; oligosaccharides; polysaccharides; and sugar chains, branched and/or linear, of any length. A sugar stream can consist of primarily or substantially C6 sugars (e.g., a C6-rich stream), C5 sugars (e.g., a C5-rich stream), or mixtures of both C6 and C5 sugars in varying ratios of said sugars. C6 sugars have a six-carbon molecular backbone and C5 sugars have a five-carbon molecular backbone. Sugar compounds or sugar streams can be produced from the pretreatment and/or hydrolysis of biomass. The biomass can comprise cellulose, hemicellulose, lignocellulose, starch, or a combination thereof Sugars or sugar streams produced from cellulose, hemicellulose, and/or lignocellulose can be termed "cellulosic-derived saccharides". Sugars or sugar streams produced from starch can be termed "non-cellulosic-derived saccharides" or "non-cellulosic derived saccharide streams. [0064] "C5-rich" composition means that one or more steps have been taken to remove at least some of the C6 sugars originally in the composition. For example, a C5-rich composition can include no more than about 50% C6 sugars, no more than about 40% C6 sugars, no more than about 30% C6 sugars, no more than about 20% C6 sugars, no more than about 10% C6 sugars, no more than about 50% C6 sugars, or it can include from about 2% to about 10% C6 sugars by weight. Likewise, a "C6-rich" composition is one in which at least some of the originally-present C5 sugars have been removed. For example, a C6-rich composition can include no more than about 50% C5 sugars, nor more than about 40% C5 sugars, no more than about 30% C5 sugars, no more than about 20% C5 sugars, no more than about 10% C5 sugars, no more than about 5% C5 sugars, or it can include from about 2% to about 10% C5 sugars by weight. [0065] A "liquid" composition may contain solids and a "solids" composition may contain liquids. A liquid composition refers to a composition in which the material is primarily liquid, and a solids composition is one in which the material is primarily solid. [0066] "Gentle Pretreatment" generally refers to the collection of processes upstream of hydrolysis, which result in composition that, when hydrolyzed, produces a fermentable sugar composition. The fermentable sugar composition can be used to enhance a non-cellulosic fermentation process, such as a corn mash fermentation process. In some embodiments, the gentle pretreatment process provides a fermentable sugar composition having a favorable 37 WO 2013/120035 PCT/US2013/025457 nutrient balance (e.g. plant-derived extracted nutrients, which are part of the composition as a result of the pretreatment process) and/or an amount of toxic compounds (e.g. phenolics and sugar degradation products, organic acids and furans, which inhibit and/or inactivate the performance of enzymes and or fermentation organisms), which is limited such that the resultant fermentable sugar composition can enhance a non-cellulosic fermentation process, such as a corn mash fermentation process. For example, a gentle pretreatment is one that results in a sugar stream that is about 25% (w/v) C6 sugars or more, about 4 g/L hydroxymethyl furfural or less, about 4 g/L furfural or less, about 10 g/L acetic acid or less, about 10 g/L formic acid or less for example as measured by typical HPLC methods referred to herein. ("About X amount of a substance or less" means the same as "no more than about" and includes zero-i.e. includes the possibility that none of that substance is present in the composition.) "Gentle pretreatment" can include one or more of: pre-processing biomass to reduce size and/or create size uniformity; pretreatment itself (process for making cellulose more accessible to hydrolysis); and post-processing steps such as washing steps. [0067] The terms "non-cellulosic" and "sugar- or starch- based" are used interchangeably and have the same meaning. For example "non-cellulosic fermentation process" is used interchangeably and means the same thing as "sugar- and starch-based fermentation process." Starch is a carbohydrate consisting of consisting of a large number of glucose units joined by glycosidic bonds. The glycosidic bonds are typically the easily hydrolysable alpha glycosidic bonds. This polysaccharide can be produced by all green plants as an energy store. There can be two types of starch molecules: the linear and helical amylose and the branched amylopectin, although amylase can also contain branches. [0068] A "first biomass" as used herein includes simple saccharides (e.g., mono and di saccharides, e.g., glucose, sucrose, lactose, etc.) and/or starch-containing materials. For example, a first biomass includes corn, corn mash, sugar cane, sugar beets, sugar palms, sweet sorghum, nypa palm, cassava, rice, milo, sorghum, sweet potatoes, wheat, molasses, tubers, roots, stems, whole grains, barley, rye, milo, sago, cassaya, tapioca, rice peas, beans, potatoes, beets, fruits, or any other sugar or starch containing materials, or combination of sugar or starch containing materials or sugar or starch containing biomasses. The term "simple saccharides and/or starch containing biomass" is also used interchangeably herein with a "first biomass." Description [0069] The following description and examples illustrate some exemplary embodiments of the disclosure in detail. Those of skill in the art will recognize that there are numerous 38 WO 2013/120035 PCT/US2013/025457 variations and modifications of this disclosure that are encompassed by its scope. Accordingly, the description of a certain exemplary embodiment should not be deemed to limit the scope of the present disclosure. [0070] Corn Fermentation [0071] To overcome the cost of corn, and issues of glycerol production and slow fermentation, several entities have tried adding mixed cellulosic-derived sugars either with or without the pretreatment liquor. There has been little or no success using such methods. One reason is that the industrial yeasts used to ferment starch are primarily C6-fermenting species. In fact, almost all yeasts require C6 sugars as a feedstock and cannot ferment pentose (C5) sugar as rapidly as C6 sugar or cannot ferment C5 sugar at all. Those that can ferment C5 sugars do not tolerate high levels of ethanol, thus are not useful in the industrial production of biofuels. [0072] In the production of sugar-derived products through fermentation, it is important to carry out the fermentation as quickly as possible. The risk of contamination increases as the fermentation lengthens. Furthermore, the energy requirements increase the cost of fermentation, thus raising the price of the product. [0073] Feedstock and Pretreatment of Feedstock [0074] In one embodiment, the feedstock (biomass) contains cellulosic, hemicellulosic, and/or lignocellulosic material. The feedstock can be derived from agricultural crops, crop residues, trees, woodchips, sawdust, paper, cardboard, grasses, algae, municipal waste and other sources. [0075] Cellulose is a linear polymer of glucose where the glucose units are connected via 0(1->4) linkages. Hemicellulose is a branched polymer of a number of sugar monomers including glucose, xylose, mannose, galactose, rhamnose and arabinose, and can have sugar acids such as mannuronic acid and galacturonic acid present as well. Lignin is a cross-linked, racemic macromolecule of mostly p-coumaryl alcohol, conferyl alcohol and sinapyl alcohol. These three polymers occur together in lignocellulosic materials in plant biomass. The different characteristics of the three polymers can make hydrolysis of the combination difficult as each polymer tends to shield the others from enzymatic attack. [0076] In one embodiment, methods are provided for the pretreatment of feedstock used in the fermentation and production of the biofuels and chemicals. The pretreatment steps can include mechanical, thermal, pressure, chemical, thermochemical, and/or biochemical tests pretreatment prior to being used in a bioprocess for the production of fuels and chemicals, but untreated biomass material can be used in the process as well. Mechanical processes can 39 WO 2013/120035 PCT/US2013/025457 reduce the particle size of the biomass material so that it can be more conveniently handled in the bioprocess and can increase the surface area of the feedstock to facilitate contact with chemicals/biochemicals/biocatalysts. Mechanical processes can also separate one type of biomass material from another. The biomass material can also be subjected to thermal and/or chemical pretreatments to render plant polymers more accessible. Multiple steps of treatment can also be used. [0077] Mechanical processes include, are not limited to, washing, soaking, milling, size reduction, screening, shearing, size classification and density classification processes. Chemical processes include, but are not limited to, bleaching, oxidation, reduction, acid treatment, base treatment, sulfite treatment, acid sulfite treatment, basic sulfite treatment, ammonia treatment, and hydrolysis. Thermal processes include, but are not limited to, sterilization, ammonia fiber expansion or explosion ("AFEX"), steam explosion, holding at elevated temperatures, pressurized or unpressurized, in the presence or absence of water, and freezing. Biochemical processes include, but are not limited to, treatment with enzymes, including enzymes produced by genetically-modified plants, and treatment with microorganisms. Various enzymes that can be utilized include cellulase, amylase, glucosidase, xylanase, gluconase, and other polysaccharases; lysozyme; laccase, and other lignin-modifying enzymes; lipoxygenase, peroxidase, and other oxidative enzymes; proteases; and lipases. One or more of the mechanical, chemical, thermal, thermochemical, and biochemical processes can be combined or used separately. Such combined processes can also include those used in the production of paper, cellulose products, microcrystalline cellulose, and cellulosics and can include pulping, kraft pulping, acidic sulfite processing. The feedstock can be a side stream or waste stream from a facility that utilizes one or more of these processes on a biomass material, such as cellulosic, hemicellulosic or lignocellulosic material. Examples include paper plants, cellulosics plants, distillation plants, cotton processing plants, and microcrystalline cellulose plants. The feedstock can also include cellulose-containing or cellulosic containing waste materials. The feedstock can also be biomass materials, such as wood, grasses, corn, starch, or sugar, produced or harvested as an intended feedstock for production of ethanol or other products such as by biocatalysts. [0078] In another embodiment, a method can utilize a pretreatment process disclosed in U.S. Patents and Patent Applications US20040152881, US20040171136, US20040168960, US20080121359, US20060069244, US20060188980, US20080176301, 5693296, 6262313, US20060024801, 5969189, 6043392, US20020038058, US5865898, US5865898, 40 WO 2013/120035 PCT/US2013/025457 US6478965, 5986133, or US20080280338, each of which is incorporated by reference herein in its entirety. [0079] In another embodiment, the AFEX process is be used for pretreatment of biomass. In a preferred embodiment, the AFEX process is used in the preparation of cellulosic, hemicellulosic or lignocellulosic materials for fermentation to ethanol or other products. The process generally includes combining the feedstock with ammonia, heating under pressure, and suddenly releasing the pressure. Water can be present in various amounts. The AFEX process has been the subject of numerous patents and publications. [0080] In another embodiment, the pretreatment of biomass comprises the addition of calcium hydroxide to a biomass to render the biomass susceptible to degradation. Pretreatment comprises the addition of calcium hydroxide and water to the biomass to form a mixture, and maintaining the mixture at a relatively high temperature. Alternatively, an oxidizing agent, selected from the group consisting of oxygen and oxygen-containing gasses, can be added under pressure to the mixture. Examples of carbon hydroxide treatments are disclosed in U.S. Patent No. 5865898 to Holtzapple and S. Kim and M. T. Holzapple, Bioresource Technology, 96, (2005) 1994, incorporated by reference herein in its entirety. [0081] In one embodiment, pretreatment of biomass comprises dilute acid hydrolysis. Example of dilute acid hydrolysis treatment are disclosed in T. A. Lloyd and C. E Wyman, Bioresource Technology, (2005) 96, 1967, incorporated by reference herein in its entirety. [0082] In another embodiment, pretreatment of biomass comprises pH controlled liquid hot water treatment. Examples of pH controlled liquid hot water treatments are disclosed in N. Mosier et al., Bioresource Technology, (2005) 96, 1986, incorporated by reference herein in its entirety. [0083] In one embodiment, pretreatment of biomass comprises aqueous ammonia recycle process (ARP). Examples of aqueous ammonia recycle process are described in T. H. Kim and Y. Y. Lee, Bioresource Technology, (2005) 96, 2007, incorporated by reference herein in its entirety. [0084] In one embodiment, the above mentioned methods have two steps: a pretreatment step that leads to a wash stream, and an enzymatic hydrolysis step of pretreated-biomass that produces a hydrolysate stream. In the above methods, the pretreatment step can include acid hydrolysis, hot water pretreatment, steam explosion or alkaline reagent based methods (AFEX, ARP, and lime pretreatments). Dilute acid and hot water treatment methods can be used to solubilize all or a portion of the hemicellulose. Methods employing alkaline reagents can be used remove all, most, or a portion of the lignin during the pretreatment step. As a 41 WO 2013/120035 PCT/US2013/025457 result, the wash stream from the pretreatment step in the former methods contains mostly hemicellulose-based sugars, whereas this stream has mostly lignin for the high-pH methods. The subsequent enzymatic hydrolysis of the residual biomass leads to mixed sugars (C5 and C6) in the alkali based pretreatment methods, while glucose is the major product in the hydrolysate from the low and neutral pH methods. Such a hydrolysate can be referred to as a C6-enriched hydrolysate. In one embodiment, the treated material is additionally treated with catalase or another similar chemical, chelating agents, surfactants, and other compounds to remove impurities or toxic chemicals or further release polysaccharides. [0085] In one embodiment, one or more monosaccharides are produced by pretreating and/or hydrolyzing a biomass comprising cellulose, hemicellulose, lignocellulose and/or starch. The biomass can be pretreated according to any of the methods disclosed herein; for example, by dilute acid, hot water treatment, stream explosion, or an alkaline pretreatment. The biomass can be pretreated using a combination of techniques; for example, the biomass can be pretreated using hot water or stream explosion followed by alkaline treatment. The one or more monosaccharides can include C6 and/or C5 monosaccharides. The one or more monosaccharides can be in a C6-enriched hydrolysate (C6 Saccharide Stream). The one or more monosaccharides can be in a C5-enriched hydrolysate (C5 Saccharide Stream). The one or more monosaccharides can comprise both C5 and C6 saccharides (C5 + C6 Saccharide Stream). The one or more monosaccharides can include cellulosic-derived monosaccharides. The one or more monosaccharides can include non-cellulosic-derived monosaccharides (e.g., starch-derived monosaccharides). The one or more monosaccharides can include glucose, fructose, galactose, xylose, or any other saccharides. [0086] A C6-enriched hydrolysate (C6 Saccharide Stream) is enriched for C6 sugars; however, the C6-enriched hydrolysate can comprise C5 sugars. In one embodiment, less than about 50%, 40%, 30%, 20%, 10%, or 1% of the sugars in the C6-enriched hydrolysate are C5 sugars. In another embodiment, about 0-50%, 0-40%, 0-30%, 0-20%, 0-10%, 0-1%, 0-0.1%, 0.1-50%, 0.1-40%, 0.1-30%, 0.1-20%, 0.1-10%, 0.1-1%, 1-50%, 1-40%, 1-30%, 1-20%, 1 10%, 10-50%, 10-40%, 10-30%, 10-20%, 20-50%, 20-40%, 20-30%, 30-50%, 30-40%, of 40-50% of the sugars in a C6-enriched hydrolysate are C5 sugars. The C6-enriched hydrolysate can comprise one or more cellulosic-derived C6 monosaccharides (e.g., glucose). The C6-enriched hydrolysate can comprise one or more non-cellulosic derived monosaccharides (e.g., starch-derived monosaccharides, e.g., glucose). [0087] A hydrolyzate or saccharide stream comprising one or more cellulosic or non cellulosic derived saccharides can further comprise residual solids (e.g., insoluble or 42 WO 2013/120035 PCT/US2013/025457 suspended solids). The residual solids can include unhydrolyzed cellulose, hemicellulose, lignin, or starch; proteins; fats; oils, or a combination thereof The hydrolyzate or sugar stream can comprise from about 0 % to about 50% w/v residual solids; for example, about 0 50%, 0-25%, 0-15%, 0-10%, 0-5%, 0-1%, 1-50%, 1-25%, 1-15%, 1-10%, 1-5%, 5-50%, 5 25%, 5-15%, 5-10%, 10-50%, 10-25%, 10-15%, 15-50%, 15-25%, 25-50%, 0%, 1%, 2%, 3%, 4%, 5%,6%,7%,8, 9%, 10%, 11%, 12%, 13%, 14%, 15%, 16%, 17%, 18%, 19%, 20%, 21%, 22%, 23%, 24%, 25%, 26%, 27%, 28%, 29%, 30%, 31%, 32%, 33%, 34%, 35%, 36

%

, 37%, 38%, 39%, 40%, 41%, 42%, 43%, 44%, 45%, 46%, 47%, 48%, 49%, or 50% residual solids w/v. [0088] Residual solids (e.g., insoluble or suspended solids) in a hydrolyzate or saccharide stream (e.g., C5 Saccharide Stream, C6 Saccharide Stream, C5 + C6 Saccharide Stream, etc.) can have, for example, particle sizes of from 10 gM to 2.5 mm or larger or smaller. The residual solids can have particles sizes of about 0.01-2.5 mm, 0.01-1 mm, 0.01-0.5 mm, 0.01 0.1 mm, 0.01-0.05 mm, 0.05-2.5 mm, 0.05-1 mm, 0.05-0.5 mm, 0.05-0.1 mm, 0.1-2.5 mm, 0.1-1 mm, 0.1-0.5 mm, 0.5-2.5 mm, 0.5-1 mm, 1-2.5 mm, 0.01 mm, 0.02 mm, 0.03 mm, 0.04 mm, 0.05 mm, 0.06 mm, 0.07 mm, 0.08 mm, 0.09 mm, 0.1 mm, 0.11 mm, 0.12 mm, 0.13 mm, 0.14 mm, 0.15 mm, 0.16 mm, 0.17 mm, 0.18 mm, 0.19 mm, 0.2 mm, 0.25 mm, 0.3 mm, 0.35 mm, 0.4 mm, 0.45 mm, 0.5 mm, 0.55 mm, 0.6 mm, 0.65 mm, 0.7 mm, 0.75 mm, 0.8 mm, 0.85 mm, 0.9 mm, 0.95 mm, 1 mm, 1.05 mm, 1.1 mm, 1.15 mm, 1.2 mm, 1.25 mm, 1.3 mm, 1.35 mm, 1.4 mm, 1.45 mm, 1.5 mm, 1.6 mm, 1.7 mm, 1.8 mm, 1.9 mm, 2 mm, 2.1 mm, 2.2 mm, 2.3 mm, 2.4 mm, 2.5 mm. [0089] Residual solids (e.g., insoluble or suspended solids) in a hydrolyzate or saccharide stream (e.g., C5 Saccharide Stream, C6 Saccharide Stream, C5 + C6 Saccharide Stream, etc.) can have, for example, particle sizes of from 10 gM 3 to 2.5 mm 3 or larger or smaller. The residual solids can have particles sizes of about 0.01-2.5 mm 3 , 0.01-1 mm 3 , 0.01-0.5 mm 3 , 0.01-0.1 mm 3 , 0.01-0.05 mm 3 , 0.05-2.5 mm 3 , 0.05-1 mm 3 , 0.05-0.5 mm 3 , 0.05-0.1 mm 3 , 0.1 2.5 mm 3 , 0.1-1 mm 3 , 0.1-0.5 mm 3 , 0.5-2.5 mm 3 , 0.5-1 mm 3 , 1-2.5 mm 3 , 0.01 mm 3 , 0.02 mm 3 , 0.03 mm 3 , 0.04 mm 3 , 0.05 mm 3 , 0.06 mm 3 , 0.07 mm 3 , 0.08 mm 3 , 0.09 mm 3 , 0.1 mm 3 , 0.11 mm 3 , 0.12 mm 3 , 0.13 mm 3 , 0.14 mm 3 , 0.15 mm 3 , 0.16 mm 3 , 0.17 mm 3 , 0.18 mm 3 , 0.19 mm 3 , 0.2 mm 3 , 0.25 mm 3 , 0.3 mm 3 , 0.35 mm 3 , 0.4 mm 3 , 0.45 mm 3 , 0.5 mm 3 , 0.55 mm 3 , 0.6 mm 3 , 0.65 mm 3 , 0.7 mm 3 , 0.75 mm 3 , 0.8 mm 3 , 0.85 mm 3 , 0.9 mm 3 , 0.95 mm 3 , 1 mm 3 , 1.05 mm 3 , 1.1 mm 3 , 1.15 mm 3 , 1.2 mm 3 , 1.25 mm 3 , 1.3 mm 3 , 1.35 mm 3 , 1.4 mm 3 , 1.45 mm 3 , 1.5 mm 3 , 1.6 mm 3 , 1.7 mm 3 , 1.8 mm 3 , 1.9 mm 3 , 2 mm 3 , 2.1 mm 3 , 2.2 mm 3 , 2.3 mm 3 , 2.4 mm 3 , 2.5 mm4. 43 WO 2013/120035 PCT/US2013/025457 [0090] In some embodiments, all or a portion of the residual solids (e.g., insoluble or suspended solids) are sequestered and removed from a hydrolyzate or saccharide stream (e.g., C5 Saccharide Stream, C6 Saccharide Stream, C5 + C6 Saccharide Stream, etc.). The sequestration and removal can be accomplished, for example, by flocculation, filtration, evaporation, centrifugation, or a combination thereof [0091] The level of residual solids (e.g., insoluble or suspended solids) in a hydrolyzate or saccharide stream (e.g., C5 Saccharide Stream, C6 Saccharide Stream, C5 + C6 Saccharide Stream, etc.) can affect the rate and/or final titer of one or more fermentation end-products in a fermentation reaction. For example, decreasing the level of residual solids can decrease the rate and/or final titer of polyols and/or sugar alcohols. Without being limited by theory, this can be due to decreased osmotic stress upon the microbial biocatalyst(s) used in the fermentation reaction. [0092] The level of residual solids (e.g., insoluble or suspended solids) in a hydrolyzate or saccharide stream (e.g., C5 Saccharide Stream, C6 Saccharide Stream, C5 + C6 Saccharide Stream, etc.) can affect the growth rate of a biocatalyst microorganism in a fermentation reaction. The residual solids can contain nutrients (e.g., proteins, amino acids, fats, oils, etc.) or ions/trace metals that promote microorganism growth. Increased growth rates can decrease production of one or more fermentation end-products such as polyols or sugar alcohols. [0093] In one embodiment, pretreatment of biomass comprises ionic liquid (IL) pretreatment. Biomass can be pretreated by incubation with an ionic liquid, followed by IL extraction with a wash solvent such as alcohol or water. The treated biomass can then be separated from the ionic liquid/wash-solvent solution by centrifugation or filtration, and sent to the saccharification reactor or vessel. Examples of ionic liquid pretreatment are disclosed in US publication No. 2008/0227162, incorporated herein by reference in its entirety. [0094] In another embodiment, a method can utilize a pretreatment process disclosed in U.S. Patent No. 4600590 to Dale, U.S. Patent No. 4644060 to Chou, U.S. Patent No. 5037663 to Dale. U.S. Patent No. 5171592 to Holtzapple, et al., et al., U.S. Patent No. 5939544 to Karstens, et al., U.S. Patent No. 5473061 to Bredereck, et al., U.S. Patent No. 6416621 to Karstens., U.S. Patent No. 6106888 to Dale, et al., U.S. Patent No. 6176176 to Dale, et al., PCT publication W02008/020901 to Dale, et al., Felix, A., et al., Anim. Prod. 51, 47-61 (1990)., Wais, A.C., Jr., et al., Journal of Animal Science, 35, No. 1,109-112 (1972), which are incorporated herein by reference in their entireties. [0095] Alteration of the pH of a pretreated feedstock can be accomplished by washing the feedstock (e.g., with water) one or more times to remove an alkaline or acidic substance, or 44 WO 2013/120035 PCT/US2013/025457 other substance used or produced during pretreatment. Washing can comprise exposing the pretreated feedstock to an equal volume of water 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19, 20, 21, 22, 23, 24, 25 or more times. In another embodiment, a pH modifier can be added. For example, an acid, a buffer, or a material that reacts with other materials present can be added to modulate the pH of the feedstock. In one embodiment, more than one pH modifier can be used, such as one or more bases, one or more bases with one or more buffers, one or more acids, one or more acids with one or more buffers, or one or more buffers. When more than one pH modifiers are utilized, they can be added at the same time or at different times. Other non-limiting exemplary methods for neutralizing feedstocks treated with alkaline substances have been described, for example in U.S. Patent Nos. 4,048,341; 4,182,780; and 5,693,296. [0096] In one embodiment, one or more acids can be combined, resulting in a buffer. Suitable acids and buffers that can be used as pH modifiers include any liquid or gaseous acid that is compatible with the microorganism. Non-limiting examples include peroxyacetic acid, sulfuric acid, sulfurous acid, lactic acid, citric acid, phosphoric acid, and hydrochloric acid. In some instances, the pH can be lowered to neutral pH or acidic pH, for example a pH of 7.0, 6.5, 6.0, 5.5, 5.0, 4.5, 4.0, or lower. In some embodiments, the pH is lowered and/or maintained within a range of about pH 4.5 to about 7.1, or about 4.5 to about 6.9, or about pH 5.0 to about 6.3, or about pH 5.5 to about 6.3, or about pH 6.0 to about 6.5, or about pH 5.5 to about 6.9 or about pH 6.2 to about 6.7. [0097] In another embodiment, biomass can be pre-treated at an elevated temperature and/or pressure. In one embodiment, biomass is pre treated at a temperature range of 20'C to 400'C. In another embodiment, biomass is pretreated at a temperature of about 20'C, 25'C, 30'C, 35'C, 40'C, 45'C, 50'C, 55 0 C, 60'C, 65'C, 80'C, 90'C, 100 0 C, 120'C, 150'C, 200'C, 250'C, 300'C, 350'C, 400'C or higher. In another embodiment, elevated temperatures are provided by the use of steam, hot water, or hot gases. In one embodiment, steam can be injected into a biomass containing vessel. In another embodiment, the steam, hot water, or hot gas can be injected into a vessel jacket such that it heats, but does not directly contact the biomass. [0098] In another embodiment, a biomass can be treated at an elevated pressure. In one embodiment, biomass is pre treated at a pressure range of about Ipsi to about 30psi. In another embodiment, biomass is pre treated at a pressure or about Ipsi, 2psi, 3psi, 4psi, 5psi, 6psi, 7psi, 8psi, 9psi, 10psi, l2psi, l5psi, l8psi, 20psi, 22psi, 24psi, 26psi, 28psi, 30psi or more. In some embodiments, biomass can be treated with elevated pressures by the injection 45 WO 2013/120035 PCT/US2013/025457 of steam into a biomass containing vessel. In one embodiment, the biomass can be treated to vacuum conditions prior or subsequent to alkaline or acid treatment or any other treatment methods provided herein. [0099] In one embodiment, alkaline or acid pretreated biomass is washed (e.g. with water (hot or cold) or other solvent such as alcohol (e.g. ethanol)), pH neutralized with an acid, base, or buffering agent (e.g. phosphate, citrate, borate, or carbonate salt) or dried prior to fermentation. In one embodiment, the drying step can be performed under vacuum to increase the rate of evaporation of water or other solvents. Alternatively, or additionally, the drying step can be performed at elevated temperatures such as about 20'C, 25'C, 30'C, 35'C, 40'C, 45'C, 50'C, 55'C, 60'C, 65'C, 80'C, 90'C, 100 0 C, 120'C, 150'C, 200'C, 250'C, 300'C or more. [00100] In one embodiment, the pretreatment step includes a step of solids recovery. The solids recovery step can be during or after pretreatment (e.g., acid or alkali pretreatment), or before the drying step. In one embodiment, the solids recovery step can include the use of a sieve, filter, screen, or a membrane for separating the liquid and solids fractions. In one embodiment, a suitable sieve pore diameter size ranges from about 0.001 microns to 8mm, such as about 0.005microns to 3mm or about 0.01 microns to 1mm. In one embodiment, a sieve pore size has a pore diameter of about 0.0 microns, 0.02 microns, 0.05 microns, 0.1 microns, 0.5 microns, 1 micron, 2 microns, 4 microns, 5 microns, 10 microns, 20 microns, 25 microns, 50 microns, 75 microns, 100 microns, 125 microns, 150 microns, 200 microns, 250 microns, 300 microns, 400 microns, 500 microns, 750 microns, 1mm or more. In one embodiment, biomass (e.g. corn stover) is processed or pretreated prior to fermentation. In one embodiment, a method of pre-treatment includes but is not limited to, biomass particle size reduction, such as for example shredding, milling, chipping, crushing, grinding, or pulverizing. In one embodiment, biomass particle size reduction can include size separation methods such as sieving, or other suitable methods known in the art to separate materials based on size. In one embodiment, size separation can provide for enhanced yields. In one embodiment, separation of finely shredded biomass (e.g. particles smaller than about 8 mm in diameter, such as, 8, 7.9, 7.7, 7.5, 7.3, 7, 6.9, 6.7, 6.5, 6.3, 6, 5.9, 5.7, 5.5, 5.3, 5, 4.9, 4.7, 4.5, 4.3, 4, 3.9, 3.7, 3.5, 3.3, 3, 2.9, 2.7, 2.5, 2.3, 2, 1.9, 1.7, 1.5, 1.3, 1, 0.9, 0.8, 0.7, 0.6, 0.5, 0.4, 0.3, 0.2, or 0.1 mm) from larger particles allows the recycling of the larger particles back into the size reduction process, thereby increasing the final yield of processed biomass. In one embodiment, a fermentative mixture is provided which comprises a pretreated lignocellulosic feedstock comprising less than about 50% of a lignin component present in the feedstock 46 WO 2013/120035 PCT/US2013/025457 prior to pretreatment and comprising more than about 60% of a hemicellulose component present in the feedstock prior to pretreatment; and a microorganism capable of fermenting a five-carbon sugar, such as xylose, arabinose or a combination thereof, and a six-carbon sugar, such as glucose, galactose, mannose or a combination thereof In some instances, pretreatment of the lignocellulosic feedstock comprises adding an alkaline substance which raises the pH to an alkaline level, for example NaOH. In one embodiment, NaOH is added at a concentration of about 0.50% to about 2% by weight of the feedstock. In one embodiment, pretreatment also comprises addition of a chelating agent. [00101] Hydrolysis [00102] In one embodiment, the biomass hydrolyzing unit provides useful advantages for the conversion of biomass to biofuels and chemical products. One advantage of this unit is its ability to produce monomeric sugars from multiple types of biomass, including mixtures of different biomass materials, and is capable of hydrolyzing polysaccharides and higher molecular weight saccharides to lower molecular weight saccharides. In one embodiment, the hydrolyzing unit utilizes a pretreatment process and a hydrolytic enzyme which facilitates the production of a sugar stream containing a concentration of a monomeric sugar or several monomeric sugars derived from cellulosic and/or hemicellulosic polymers. Examples of biomass material that can be pretreated and hydrolyzed to manufacture sugar monomers include, but are not limited to, cellulosic, hemicellulosic, lignocellulosic materials; pectins; starches; wood; paper; agricultural products; forest waste; tree waste; tree bark; leaves; grasses; sawgrass; woody plant matter; non-woody plant matter; carbohydrates; starch; inulin; fructans; glucans; corn; sugar cane; sorghum, other grasses; bamboo, algae, and material derived from these materials. This ability to use a very wide range of pretreatment methods and hydrolytic enzymes gives distinct advantages in biomass fermentations. Various pretreatment conditions and enzyme hydrolysis can enhance the extraction of sugars from biomass, resulting in higher yields, higher productivity, greater product selectivity, and/or greater conversion efficiency. [00103] In one embodiment, the enzyme treatment is used to hydrolyze various higher saccharides (higher molecular weight) present in biomass to lower saccharides (lower molecular weight), such as in preparation for fermentation by biocatalysts such as yeasts to produce ethanol, hydrogen, or other chemicals such as organic acids including succinic acid, formic acid, acetic acid, and lactic acid. These enzymes and/or the hydrolysate can be used in fermentations to produce various products including fuels, and other chemicals. 47 WO 2013/120035 PCT/US2013/025457 [00104] In one example, the process for converting biomass material into ethanol includes pretreating the biomass material (e.g., "feedstock"), hydrolyzing the pretreated biomass to convert polysaccharides to oligosaccharides, further hydrolyzing the oligosaccharides to monosaccharides, and converting the monosaccharides to biofuels and chemical products. Enzymes such as cellulases, polysaccharases, lipases, proteases, ligninases, and hemicellulases, help produce the monosaccharides can be used in the biosynthesis of fermentation end-products. Biomass material that can be utilized includes woody plant matter, non-woody plant matter, cellulosic material, lignocellulosic material, hemicellulosic material, carbohydrates, pectin, starch, inulin, fructans, glucans, corn, algae, sugarcane, other grasses, switchgrass, bagasse, wheat straw, barley straw, rice straw, corncobs, bamboo, citrus peels, sorghum, high biomass sorghum, seed hulls, and material derived from these. The final product can then be separated and/or purified, as indicated by the properties for the desired final product. In some instances, compounds related to sugars such as sugar alcohols or sugar acids can be utilized as well. [001051 Chemicals that can be used in the methods disclosed herein can be purchased from a commercial supplier, such as Sigma-Aldrich. Additionally, commercial enzyme cocktails (e.g. Accellerase TM 1000, CelluSeb-TL, CelluSeb-TS, Cellic T M ' CTec, STARGEN TM, Maxalig T M , Spezyme.Rf

M

, Distillase.Rf

M

, G-Zyme.Rfm, Fermenzyme.Rfm, Fermgen

TM

, GC 212, or Optimashf m ) or any other commercial enzyme cocktail can be purchased from vendors such as Specialty Enzymes & Biochemicals Co., Genencor, or Novozymes. Alternatively, enzyme cocktails can be prepared by growing one or more organisms such as for example a fungi (e.g. a Trichoderma, a Saccharomyces, a Pichia, a White Rot Fungus etc.), a bacteria (e.g. a Clostridium, or a coliform bacterium, a Zymomonas bacterium, Sacharophagus degradans etc.) in a suitable medium and harvesting enzymes produced therefrom. In some embodiments, the harvesting can include one or more steps of purification of enzymes. [00106] In one embodiment, treatment of biomass comprises enzyme hydrolysis. In one embodiment, a biomass is treated with an enzyme or a mixture of enzymes, e.g., endoglucanases, exoglucanases, cellobiohydro lases, cellulase, beta-glucosidases, glycoside hydrolases, glycosyltransferases, lyases, esterases, amylases, glucoamylases, and proteins containing carbohydrate-binding modules. In one embodiment, the enzyme or mixture of enzymes is one or more individual enzymes with distinct activities. In another embodiment, the enzyme or mixture of enzymes can be enzyme domains with a particular catalytic activity. For example, an enzyme with multiple activities can have multiple enzyme 48 WO 2013/120035 PCT/US2013/025457 domains, including for example glycoside hydrolases, glycosyltransferases, lyases and/or esterases catalytic domains. [001071 In one embodiment, enzymes that degrade polysaccharides are used for the hydrolysis of biomass and can include enzymes that degrade cellulose, namely, cellulases. Examples of some cellulases include endocellulases and exo-cellulases that hydrolyze beta 1,4-glucosidic bonds. [00108] In one embodiment, enzymes that degrade polysaccharides are used for the hydrolysis of biomass and can include enzymes that have the ability to degrade hemicellulose, namely, hemicellulases. Hemicellulose can be a major component of plant biomass and can contain a mixture of pentoses and hexoses, for example, D-xylopyranose, L arabinofuranose, D-mannopyranose, Dglucopyranose, D-galactopyranose, D glucopyranosyluronic acid and other sugars. In one embodiment, enzymes that degrade polysaccharides are used for the hydrolysis of biomass and can include enzymes that have the ability to degrade pectin, namely, pectinases. In plant cell walls, the cross-linked cellulose network can be embedded in a matrix of pectins that can be covalently cross-linked to xyloglucans and certain structural proteins. Pectin can comprise homogalacturonan (HG) or rhamnogalacturonan (RH). [00109] In one embodiment, hydrolysis of biomass includes enzymes that can hydrolyze starch. Enzymes that hydrolyze starch include alpha-amylase, glucoamylase, beta amylase, exo-alpha- 1,4-glucanase, and pullulanase. [00110] In one embodiment, hydrolysis of biomass comprises hydrolases that can include enzymes that hydrolyze chitin. In another embodiment, hydrolases can include enzymes that hydrolyze lichen, namely, lichenase. [00111] In one embodiment, after pretreatment and/or hydrolysis by any of the above methods the feedstock contains cellulose, hemicellulose, soluble oligomers, simple sugars, lignin, volatiles and ash. The parameters of the hydrolysis can be changed to vary the concentration of the components of the pretreated feedstock. For example, a hydrolysis can be chosen so that the concentration of soluble C5 saccharides is high and the concentration of lignin is low after hydrolysis. Examples of parameters of the hydrolysis include temperature, pressure, time, concentration, composition and pH. [00112] In one embodiment, the parameters of the pretreatment and hydrolysis are changed to vary the concentration of the components of the pretreated feedstock such that concentration of the components in the pretreated and hydrolyzed feedstock is optimal for fermentation with a microbe such as a yeast or bacterium microbe. 49 WO 2013/120035 PCT/US2013/025457 [001131 In one embodiment, the parameters of the pretreatment are changed to encourage the release of the components of a genetically modified feedstock such as enzymes stored within a vacuole to increase or complement the enzymes synthesized by biocatalyst to produce optimal release of the fermentable components during hydrolysis and fermentation. [00114] In one embodiment, the parameters of the pretreatment and hydrolysis are changed such that concentration of accessible cellulose in the pretreated feedstock is 1%, 5%, 10%, 12%, 13%, 14%, 15%, 16%, 17%, 19%, 20%, 30%, 40% or 50%. In one embodiment, the parameters of the pretreatment are changed such that concentration of accessible cellulose in the pretreated feedstock is 5% to 30%. In one embodiment, the parameters of the pretreatment are changed such that concentration of accessible cellulose in the pretreated feedstock is 10% to 20%. [001151 In one embodiment, the parameters of the pretreatment are changed such that concentration of hemicellulose in the pretreated feedstock is 1%, 5%, 10%, 12%, 13%, 14%, 15%, 16%, 17%, 19%, 20%, 21%, 22%, 23%, 24%, 25%, 26%, 27%, 28%, 29%, 30%, 40% or 50%. In one embodiment, the parameters of the pretreatment are changed such that concentration of hemicellulose in the pretreated feedstock is 5% to 40%. In one embodiment, the parameters of the pretreatment are changed such that concentration of hemicellulose in the pretreated feedstock is 10% to 30%. [00116] In one embodiment, the parameters of the pretreatment and hydrolysis are changed such that concentration of soluble oligomers in the pretreated feedstock is 1%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 7 0%, 75%, 80%, 85%, 90%, 95%, or 99%. Examples of soluble oligomers include, but are not limited to, cellobiose and xylobiose. In one embodiment, the parameters of the pretreatment are changed such that concentration of soluble oligomers in the pretreated feedstock is 30% to 90%. In one embodiment, the parameters of the pretreatment and/or hydrolysis are changed such that concentration of soluble oligomers in the pretreated feedstock is 45% to 80%. [001171 In one embodiment, the parameters of the pretreatment and hydrolysis are changed such that concentration of simple sugars in the pretreated feedstock is 1%, 5%, 10%, 12%, 13%, 14%, 15%, 16%, 17%, 19%, 20%, 30%, 40% or 50%. In one embodiment, the parameters of the pretreatment and hydrolysis are changed such that concentration of simple sugars in the pretreated feedstock is 0% to 20%. In one embodiment, the parameters of the pretreatment and hydrolysis are changed such that concentration of simple sugars in the pretreated feedstock is 0% to 5%. Examples of simple sugars include, but are not limited to, C5 and C6 monomers and dimers. 50 WO 2013/120035 PCT/US2013/025457 [001181 In one embodiment, the parameters of the pretreatment are changed such that concentration of lignin in the pretreated and/or hydrolyzed feedstock is 1%, 5%, 10%, 12%, 13%, 14%, 15%, 16%, 17%, 1 9 %,20

%

,30

%

,40

%

or5O 0 %. In one embodiment, the parameters of the pretreatment and/or hydrolysis are changed such that concentration of lignin in the pretreated feedstock is 0% to 20%. In one embodiment, the parameters of the pretreatment and/or hydrolysis are changed such that concentration of lignin in the pretreated feedstock is 0% to 5%. In one embodiment, the parameters of the pretreatment and hydrolysis are changed such that concentration of lignin in the pretreated and/or hydrolyzed feedstock is less than 1% to 2%. In one embodiment, the parameters of the pretreatment and/or hydrolysis are changed such that the concentration of phenolics is minimized. [00119] In one embodiment, the parameters of the pretreatment and/or hydrolysis are changed such that concentration of furfural and low molecular weight lignin in the pretreated and/or hydrolyzed feedstock is less than 10%, 9%, 8%, 7%, 6%, 5%, 4%, 3%, 2%, or 1%. In one embodiment, the parameters of the pretreatment and/or hydrolysis are changed such that concentration of furfural and low molecular weight lignin in the pretreated and/or hydrolyzed feedstock is less than 1% to 2%. [00120] In one embodiment, the parameters of the pretreatment and/or hydrolysis are changed such that the concentration of simple sugars is at least 75% to 85%, and the concentration of lignin is 0% to 5% and the concentration of furfural and low molecular weight lignin in the pretreated feedstock is less than 1% to 2%. [00121] In one embodiment, the parameters of the pretreatment and/or hydrolysis are changed to obtain a high concentration of hemicellulose and a low concentration of lignin. In one embodiment, the parameters of the pretreatment and/or hydrolysis are changed to obtain a high concentration of hemicellulose and a low concentration of lignin such that concentration of the components in the pretreated stock is optimal for fermentation with a microbe such as biocatalyst. [00122] In one embodiment, more than one of these steps can occur at any given time. For example, hydrolysis of the pretreated feedstock and hydrolysis of the oligosaccharides can occur simultaneously, and one or more of these can occur simultaneously to the conversion of monosaccharides to a fuel or chemical. [001231 In another embodiment, an enzyme can directly convert the polysaccharide to monosaccharides. In some instances, an enzyme can hydrolyze the polysaccharide to oligosaccharides and the enzyme or another enzyme can hydrolyze the oligosaccharides to monosaccharides. 51 WO 2013/120035 PCT/US2013/025457 [00124] In another embodiment, the enzymes can be added to the fermentation or they can be produced by microorganisms present in the fermentation. In one embodiment, the microorganism present in the fermentation produces some enzymes. In another embodiment, enzymes are produced separately and added to the fermentation. [001251 For the overall conversion of pretreated biomass to final product to occur at high rates, the enzymes for each conversion step can be present with sufficiently high activity. If one of these enzymes is missing or is present in insufficient quantities, the production rate of an end product can be reduced. The production rate can also be reduced if the microorganisms responsible for the conversion of monosaccharides to product only slowly take up monosaccharides and/or have only limited capability for translocation of the monosaccharides and intermediates produced during the conversion to end product. Additions of fractions obtained from pretreatment and/or pretreatment and hydrolysis can increase initial or overall growth rates. In another embodiment, oligomers are taken up slowly by a biocatalyst, necessitating an almost complete conversion of polysaccharides and oligomers to monomeric sugars. [00126] In another embodiment, the enzymes of the method are produced by a biocatalyst, including a range of hydrolytic enzymes suitable for the biomass materials used in the fermentation methods. In one embodiment, a biocatalyst is grown under conditions appropriate to induce and/or promote production of the enzymes needed for the saccharification of the polysaccharide present. The production of these enzymes can occur in a separate vessel, such as a seed fermentation vessel or other fermentation vessel, or in the production fermentation vessel where ethanol production occurs. When the enzymes are produced in a separate vessel, they can, for example, be transferred to the production fermentation vessel along with the cells, or as a relatively cell free solution liquid containing the intercellular medium with the enzymes. When the enzymes are produced in a separate vessel, they can also be dried and/or purified prior to adding them to the hydrolysis or the production fermentation vessel. The conditions appropriate for production of the enzymes are frequently managed by growing the cells in a medium that includes the biomass that the cells will be expected to hydrolyze in subsequent fermentation steps. Additional medium components, such as salt supplements, growth factors, and cofactors including, but not limited to phytate, amino acids, and peptides can also assist in the production of the enzymes utilized by the microorganism in the production of the desired products. [001271 Fermentation 52 WO 2013/120035 PCT/US2013/025457 [00128] Provided herein are methods and compositions for producing one or more fermentation end-products from blended feedstocks. The blended feedstocks can comprise a first biomass and one or more monosaccharides produced by pretreating and/or hydrolyzing a second biomass comprising cellulose, hemicellulose, lignocellulose and/or starch. The one or more monosaccharides can include C6 and/or C5 monosaccharides. The one or more monosaccharides can be in a C6-enriched hydrolysate (C6 Saccharide Stream). The one or more monosaccharides can be in a C5-enriched hydrolysate (C5 Saccharide Stream). The one or more monosaccharides can comprise both C5 and C6 saccharides (C5 + C6 Saccharide Stream). The one or more monosaccharides can include cellulosic-derived monosaccharides. The one or more monosaccharides can include non-cellulosic-derived monosaccharides (e.g., starch-derived monosaccharides). The one or more monosaccharides can include glucose, fructose, galactose, xylose, or any other saccharides. The first biomass can comprise non cellulosic polysaccharides (e.g., starch). [00129] A blended feedstock can comprise from about 1% to about 50% solids from a first biomass. For example, the blended feedstock can comprise about 1-50%, 10-50%, 20 40%, 20-36%, 20-35%, 20-34%, 20-33%, 20-32%, 20-31%, 20-30%, 25-36%, 25-35%, 25 34%, 25-33%, 25-32%, 25-31%, 25-30%, 30-36%, 30-35%, 30-34%, 30-33%, 30-32%, or 30-31% solids from the first biomass. In one embodiment, the first biomass comprises non cellulosic saccharides. In one embodiment, the non-cellulosic saccharides comprise starch. In another embodiment, the non-cellulosic saccharides comprise sucrose. In another embodiment, the non-cellulosic saccharides comprise starch and/or sucrose. [001301 A blended feedstock can be produced by combining a first biomass (e.g., containing non-cellulosic saccharides such as starch or sucrose) with one or more cellulosic derived or non-cellulosic derived monosaccharides (e.g., C6 saccharides, C5 saccharides, or a combination thereof). The one or more cellulosic-derived or non-cellulosic-derived monosaccharides can be at a concentration of from about 1% to about 70% w/v prior to combining with the first biomass. For example, the one or more monosaccharides can be at a concentration of about 1- 7 0% w/v, 1-60% w/v, 1- 55 % w/v, 1-50% w/v, 1-40% w/v, 1-30% w/v, 1-20% w/v, 1-10% w/v, 10-70% w/v, 10-60% w/v, 10-55% w/v, 10-50% w/v, 10-40% w/v, 10-30% w/v, 10-20% w/v, 20-70% w/v, 20-60% w/v, 20-55% w/v, 20-50% w/v, 20 40% w/v, 20-30% w/v, 30-70% w/v, 30-60% w/v, 30-55% w/v, 30-50% w/v, 30-40% w/v, 40-70% w/v, 40-60% w/v, 40-55% w/v, 40-50% w/v, 50-70% w/v, 50-60% w/v, 50-55% w/v, 55-70% w/v, 55-60% w/v, or 60-70% w/v prior to combining with the first biomass. 53 WO 2013/120035 PCT/US2013/025457 [001311 A blended feedstock can be produced by combining a first biomass (e.g., containing non-cellulosic saccharides such as starch) with one or more cellulosic-derived monosaccharides. The one or more cellulosic-derived monosaccharides can be C6 saccharides and/or C5 saccharides. The one or more cellulosic-derived monosaccharides can be in a crude-lysate from the pretreatment and/or hydrolysis of cellulose, hemicellulose, and/or lignocellulosic material. The one or more cellulosic-derived monosaccharides can comprise less than 50%, 45%, 40%, 35%, 30%, 25%, 20%, 15%, 10%, 5%, 4%, 3%, 2%, 1.5%, 1%, 0.9%, 0.8%, 0.7%, 0.6%, 0.5%, 0.4%, 0.3%, 0.2%, 0.l1% or less w/v of one or more inhibitory compounds. The one or more inhibitory compounds can be one or more byproducts of the pretreatment and/or hydrolysis of cellulose, hemicellulose, and/or lignocellulose. The one or more inhibitory compounds can comprise one or more organic acids such as acetic acid, lactic acid, or formic acid, and/or one or more furans such as hydroxy methyl furfural or furfural, or a combination thereof [00132] Enhanced rates of fermentation can be achieved using blended feedstocks comprising a first biomass containing non-cellulosic saccharides (e.g., starch, sucrose, etc.) and one or more cellulosic-derived monosaccharides (e.g., C6 monosaccharide, C5 monosaccharides) in comparison to fermentation of the first biomass without the one or more cellulosic-derived monosaccharides. The enhanced rates of fermentation can be from about 1 % higher to about 100% higher; for example, about 1-100%, 1-75%, 1-50%, 1-25%, 1-10%, 10-100%, 10-75%, 10-50%, 10-25%, 25-100%, 25-75%, 25-50%, 50-100%, 50-75%, 75 100%, 1%, 2%, 3%, 4%, %, 65% , 7%, 8%, 9%, 10, 1 % , 12% , 13% , 14% , 15, 16%, 17

%

, 18%, 19%, 20%, 21%, 22%, 23%, 24%, 25%, 26%, 27%, 28%, 29%, 30%, 31%, 32%, 33%, 34%, 35%, 36%, 37%, 38%, 39%, 40%, 41%, 42%, 43%, 44%, 45%, 46%, 47%, 48%, 49%, 50%, 55%, 60%, 65%, 7 0%, 75%, 80%, 85%, 90%, 95%, or 100% higher. [00133] Increased yields of one or more fermentation end-products can be achieved using blended feedstocks comprising a first biomass containing non-cellulosic saccharides (e.g., starch, sucrose, etc.) and one or more cellulosic-derived monosaccharides (e.g., C6 monosaccharide, C5 monosaccharides) in comparison to fermentation of the first biomass without the one or more cellulosic-derived monosaccharides. The increased yields of one or more fermentation end-products can be from about 1 % higher to about 100% higher; for example, about 1-100%, 1-75%, 1-50%, 1-25%, 1-10%, 1-5%, 5-10%, 10-100%, 10-75%, 10-50%, 10-25%, 25-100%, 25-75%, 25-50%, 50-100%, 50-75%, 75-100%, 1%, 1.1%, 1.2%, 1.3%, 1.4%, 1.5%, 1.6%, 1.

7 %, 1.8%, 1.9%, 2%, 2.1%, 2.2%, 2.3%, 2.4%, 2.5%, 2.6%, 2.7%, 2.8%, 2.9%, 3%, 4%,5%,6%, 7%, 8%, 9%, 10%, 11%, 12%, 13%, 14%, 15%, 16 %, 54 WO 2013/120035 PCT/US2013/025457 17%, 18%, 19%, 20%, 21%, 22%, 23%, 24%, 25%, 26%, 27%, 28%, 29%, 30%, 31%, 32%, 33%, 34%, 35%, 36%, 37%, 38%, 39%, 40%, 41%, 42%, 43%, 44%, 45%, 46%, 47%, 48%, 49%, 50%, 55%, 60%, 65%, 70%, 7 5%, 80%, 85%, 90%, 95%, or 100% higher. [00134] A blended feedstock can be prepared by combining a first biomass with a saccharide stream comprising one or more cellulosic-derived monosaccharides, one or more non-cellulosic derived monosaccharides, or a combination thereof The first biomass can comprise non-cellulosic saccharides such as starch or sucrose. The one or more cellulosic derived monosaccharides or non-cellulosic derived monosaccharides can be produced by the pretreatment and/or hydrolysis of a second biomass. The second biomass can comprise cellulose, hemicellulose, lignocellulose, and/or starch. The pretreatment and/or hydrolysis of the second biomass can produce a C6-enriched hydrolysate (C6 Saccharide Stream). The pretreatment and/or hydrolysis of the second biomass can produce a C5-enriched hydrolysate (C5 Saccharide Stream). The pretreatment and/or hydrolysis of the second biomass can produce a hydrolysate containing both C5 and C6 monosaccharides (C5 + C6 Saccharide Stream). In one embodiment, the one or more cellulosic-derived monosaccharides (e.g., from a C6-enriched hydrolysate) are at a concentration that differs from the concentration of saccharides in the first biomass by less than about +/- 50%, 40%, 30%, 20%, 15%, 10%, 5%, or 1%, wherein the concentration of saccharides in the first biomass assumes complete hydrolysis of the first biomass to monomers (e.g., is in monosaccharide equivalents). [001351 A blended feedstock can be prepared by combining a first biomass with a saccharide stream comprising one or more cellulosic-derived monosaccharides, one or more non-cellulosic derived monosaccharides, or a combination thereof The first biomass can comprise non-cellulosic saccharides such as starch or sucrose. The one or more monosaccharides can be produced by the pretreatment and/or hydrolysis of a second biomass. The second biomass can comprise cellulose, hemicellulose, lignocellulose, and/or starch. The pretreatment and/or hydrolysis of the second biomass can produce a C6-enriched hydrolysate (C6 Saccharide Stream), a C5-enriched hydrolyzate (C5 Saccharide Stream), or a C5 and C6 hydrolyzate (C5 + C6 Saccharide Stream). In one embodiment, the first biomass and the saccharides stream comprising the one or more monosaccharides are combined in about a 50:50, 55:45, 60:40:, 65:35, 70:30, 75:35, 80:20, 85:15, 90:10, 95:5, or 99:1 ratio. The ratio can be a weight to weight ratio, a weight to volume ratio, or a volume to volume ratio. [001361 Exposing microorganisms such as bacteria or yeast to hypertonic solution can cause an efflux of cellular water into the medium. In order to counteract the outflow of water molecules during growth, microorganisms can produce and accumulate one or more 55 WO 2013/120035 PCT/US2013/025457 osmoregulatory molecules such as polyhydroxy compounds. (e.g., see Nevoit and Stahl (1997) FEMS Microbiology Review 21:231-241 and Parekh and Pandey (1985) Biotechnology and Bioengineering 27: 1089-1091, each of which is incorporated by reference in its entirety). During ethanolic fermentation of starch-containing compounds, microorganisms such as yeast can redirect part of the carbon released during enzymatic hydrolysis of starch to one or more other products such as polyols or sugar alcohols (e.g., glycerol) instead of fermentation end-products such as ethanol. This can occur, for example, when glucose is overly abundant during the fermentation reaction, for example, due to the conversion of starch to glucose monomers or the addition of a saccharide stream comprising one or more monosaccharides (e.g., C5 monosaccharides, C6 monosaccharides, or both). Environmental factors affecting these pathways can include oxygen availability, type of nitrogen source, osmotic pressure, heat and pH. For example, when glucose is overly abundant, a high osmotic pressure can shift metabolism to the production of glycerol. Therefore, it may be possible to maintain high ethanol production using fed-batch fermentations. In one embodiment, one or more cellulosic-derived C6 monosaccharides are added over time in a fed-batch fermentation reaction comprising a first biomass containing non-cellulosic saccharides such as starch. [001371 Without being limited by theory, the high level of solids (e.g., insoluble solids or suspended solids) in many fermentation reactions using biomass containing non-cellulosic saccharides (e.g., corn mash) can cause osmotic stress upon the biocatalyst microorganisms in the fermentation reaction (e.g., yeast, bacteria, etc.). The osmotic stress can cause the microorganisms to produce osmoregulatory compounds such as polyols (e.g., glycerol) or sugar alcohols. By utilizing blended feedstocks comprising a first biomass containing non cellulosic saccharides and a saccharide stream comprising one or more monosaccharides (e.g., cellulosic-derived or non-cellulosic derived monosaccharides), the solids of the first biomass can be diluted. This can reduce osmotic stress upon the microorganisms and reduce the production of fermentation end-products such as osmoregulatory compounds (e.g., polyols or sugar alcohols). The reduced production of osmoregulatory compounds can increase the rate and/or yield of alcohols such as ethanol, methoanol, butanol, etc. [00138] Provided herein are methods and compositions for producing one or more fermentation end-products wherein the production of one or more other products (e.g., osmoregulatory molecules) such as polyols or sugar alcohols (e.g., glycerol) is reduced. Reduced production of polyols such as glycerol can be achieved using blended feedstocks comprising a first biomass and a saccharide stream comprising one or more cellulosic-derived 56 WO 2013/120035 PCT/US2013/025457 monosaccharides, one or more non-cellulosic derived monosaccharides, or a combination thereof The first biomass can comprise non-cellulosic saccharides such as starch or sucrose. The saccharide stream comprising the one or more monosaccharides can be produced by the pretreatment and/or hydrolysis of a second biomass. The second biomass can comprise cellulose, hemicellulose, lignocellulose, and/or starch. The saccharide stream can be a C6 enriched hydrolysate (C6 Saccharide Stream), a C5-enriched hydrolysate (C5 Saccharide Stream), or a C5 and C6 containing hydrolyzate (C5 + C6 Saccharide Stream). The amount of one or more other products produced can be from about 1% to about 100% lower; for example, about 1-100%, 1-75%, 1-50%, 1-25%, 1-10%, 1-5%, 5-10%, 10-100%, 10-75%, 10-50%, 10-25%, 25-100%, 25-75%, 25-50%, 50-100%, 50-75%, 75-100%, 1%, 2%, 3%, 4%, 5%, 6%, 7%, 8%, 9%, 10%, 11%, 12%, 13%, 14%, 15%, 16%, 17%, 18%, 19%, 20%, 21%, 22%, 23%, 24%, 25%, 26%, 27%, 28%, 29%, 30%, 31%, 32%, 33%, 34%, 35%, 36%, 37%, 38%, 39%, 40%, 41%, 42%, 43%, 44%, 45%, 46%, 47%, 48%, 49%, 50%, 55%, 60%, 65%, 7 0%, 75%, 80%, 85%, 90%, 95%, or 100% lower. In one embodiment, the saccharide stream comprising the one or more monosaccharides are added in a fed batch manner and the reduced production of the one or more other products is in comparison to a non-fed batch fermentation reaction. In another embodiment, the saccharide stream comprising the one or more monosaccharides are added in a batch fermentation and the reduced production of the one or more other products is in comparison to a fermentation reaction containing the first biomass only. [00139] Disclosed herein are fed-batch fermentation reactions in which a first biomass (e.g., containing non-cellulosic saccharides such as starch and/or sucrose) and a saccharide stream comprising one or more cellulosic-derived monosaccharides, one or more non cellulosic derived monosaccharides, or a combination thereof are combined to produce a blended feed-stock in a broth. In a fed-batch reaction, the saccharide stream comprising the one or more monosaccharides (e.g., cellulosic-derived C6 monosaccharides) can be added at a rate of from about 0.001 mL/min/L of broth to about 50 mL/min/L of broth. For example, the saccharide stream comprising the one or more monosaccharides can be added at a rate of about 0.001-50 mL/min/L, 0.001-25 mL/min/L, 0.001-10 mL/min/L, 0.001-5 mL/min/L, 0.001-1 mL/min/L, 0.001-0.7 mL/min/L, 0.001-0.5 mL/min/L, 0.001-0.1 mL/min/L, 0.001 0.01 mL/min/L, 0.01-50 mL/min/L, 0.01-25 mL/min/L, 0.01-10 mL/min/L, 0.01-5 mL/min/L, 0.01-1 mL/min/L, 0.01-0.7 mL/min/L, 0.01-0.5 mL/min/L, 0.01-0.1 mL/min/L, 0.1-50 mL/min/L, 0.1-25 mL/min/L, 0.1-10 mL/min/L, 0.1-5 mL/min/L, 0.1-1 mL/min/L, 0.1-0.7 mL/min/L, 0.1-0.5 mL/min/L, 0.5-50 mL/min/L, 0.5-25 mL/min/L, 0.5-10 mL/min/L, 57 WO 2013/120035 PCT/US2013/025457 0.5-5 mL/min/L, 0.5-1 mL/min/L, 0.5-0.7 mL/min/L, 0.7-50 mL/min/L, 0.7-25 mL/min/L, 0.7-10 mL/min/L, 0.7-5 mL/min/L, 0.7-1 mL/min/L, 1-50 mL/min/L, 1-25 mL/min/L, 1-10 mL/min/L, 1-5 mL/min/L, 5-50 mL/min/L, 5-25 mL/min/L, 5-10 mL/min/L, 10-50 mL/min/L, 10-25 mL/min/L, 25-50 mL/min/L, 0.001 mL/min/L, 0.002 mL/min/L, 0.003 mL/min/L, 0.004 mL/min/L, 0.005 mL/min/L, 0.006 mL/min/L, 0.007 mL/min/L, 0.008 mL/min/L, 0.009 mL/min/L, 0.01 mL/min/L, 0.02 mL/min/L, 0.03 mL/min/L, 0.04 mL/min/L, 0.05 mL/min/L, 0.06 mL/min/L, 0.07 mL/min/L, 0.08 mL/min/L, 0.09 mL/min/L, 0.1 mL/min/L, 0.2 mL/min/L, 0.3 mL/min/L, 0.4 mL/min/L, 0.5 mL/min/L, 0.6 mL/min/L, 0.7 mL/min/L, 0.8 mL/min/L, 0.9 mL/min/L, 1 mL/min/L, 1.1 mL/min/L, 1.2 mL/min/L, 1.3 mL/min/L, 1.4 mL/min/L, 1.5 mL/min/L, 1.6 mL/min/L, 1.7 mL/min/L, 1.8 mL/min/L, 1.9 mL/min/L, 2 mL/min/L, 2.5 mL/min/L, 3 mL/min/L, 3.5 mL/min/L, 4 mL/min/L, 4.5 mL/min/L, 5 mL/min/L, 5.5 mL/min/L, 6 mL/min/L, 6.5 mL/min/L, 7 mL/min/L, 7.5 mL/min/L, 8 mL/min/L, 8.5 mL/min/L, 9 mL/min/L, 9.5 mL/min/L, 10 mL/min/L, 11 mL/min/L, 12 mL/min/L, 13 mL/min/L, 14 mL/min/L, 15 mL/min/L, 16 mL/min/L, 17 mL/min/L, 18 mL/min/L, 19 mL/min/L, 20 mL/min/L, 21 mL/min/L, 22 mL/min/L, 23 mL/min/L, 24 mL/min/L, 25 mL/min/L, 26 mL/min/L, 27 mL/min/L, 28 mL/min/L, 29 mL/min/L, 30 mL/min/L, 31 mL/min/L, 32 mL/min/L, 33 mL/min/L, 34 mL/min/L, 35 mL/min/L, 36 mL/min/L, 37 mL/min/L, 38 mL/min/L, 39 mL/min/L, 40 mL/min/L, 41 mL/min/L, 42 mL/min/L, 43 mL/min/L, 44 mL/min/L, 45 mL/min/L, 46 mL/min/L, 47 mL/min/L, 48 mL/min/L, 49 mL/min/L, or 50 mL/min/L of broth. [00140] In one embodiment, the concentration of monosaccharides in a blended feedstock prior to contacting with one or more biocatalysts (e.g., at the start of a fermentation or simultaneous saccharification and fermentation reaction) can be less than about 100 g/L; for example, less than about 100 g/L, 90 g/L, 80 g/L, 70 g/L, 60 g/L, 50 g/L, 40 g/L, 30 g/L, 25 g/L, 20 g/L, 15 g/L, 10 g/L, 9 g/L, 8 g/L, 7 g/L, 6 g/L, 5 g/L, 4 g/L, 3 g/L, 2 g/L, or 1 g/L. In another embodiment, the concentration of monosaccharides in a blended feedstock prior to contacting with one or more biocatalysts (e.g., at the start of a fermentation or simultaneous saccharification and fermentation reaction) can be from about 1 g/L to about 100 g/L; for example, about 1-100 g/L, 1-75 g/L, 1-50 g/L, 1-25 g/L, 1-10 g/L, 10-100 g/L, 10-75 g/L, 10 50 g/L, 10-25 g/L, 25-100 g/L, 25-75 g/L, 25-50 g/L, 50-100 g/L, 50-75 g/L, or 75-100 g/L. [00141] The present disclosure also provides a fermentative mixture comprising: a cellulosic feedstock pre-treated with an alkaline or acid substance and at a temperature of from about 80 0 C to about 120 0 C; subsequently hydrolyzed with an enzyme mixture, and a microorganism capable of fermenting a five-carbon sugar and/or a six-carbon sugar. In one 58 WO 2013/120035 PCT/US2013/025457 embodiment, the five-carbon sugar is xylose, arabinose, or a combination thereof In one embodiment, the six-carbon sugar is glucose, galactose, mannose, or a combination thereof In one embodiment, the alkaline substance is NaOH. In some embodiments, NaOH is added at a concentration of about 0.5% to about 2% by weight of the feedstock. In one embodiment, the acid is equal to or less than 2% HCl or H 2

SO

4 . In one embodiment, the microorganism is a Rhodococcus strain, a Clostridium strain, a Trichoderma strain, a Saccharomyces strain, a Zymomonas strain, or another microorganism suitable for fermentation of biomass. In another embodiment, the fermentation process comprises fermentation of the biomass using a microorganism that is Clostridium phytofermentans, Clostridium algidixylanolyticum, Clostridium xylanolyticum, Clostridium cellulovorans, Clostridium cellulolyticum, Clostridium thermocellum, Clostridium josui, Clostridium papyrosolvens, Clostridium cellobioparum, Clostridium hungatei, Clostridium cellulosi, Clostridium stercorarium, Clostridium termitidis, Clostridium thermocopriae, Clostridium celerecrescens, Clostridium polysaccharolyticum, Clostridium populeti, Clostridium lentocellum, Clostridium chartatabidum, Clostridium aldrichii, Clostridium herbivorans, Acetivibrio cellulolyticus, Bacteroides cellulosolvens, Caldicellulosiruptor saccharolyticum, Rhodococcus opacus, Ruminococcus albus, Ruminococcusflavefaciens, Fibrobacter succinogenes, Eubacterium cellulosolvens, Butyrivibrio fibrisolvens, Anaerocellum thermophilum, Halocella cellulolytica, Thermoanaerobacterium thermosaccharolyticum, Sacharophagus degradans, or Thermoanaerobacterium saccharolyticum. In still another embodiment, the microorganism is genetically modified to enhance activity of one or more hydrolytic enzymes, such as a genetically-modified Saccaromyces cerevisae. [00142] In one embodiment, a wild type or a genetically-improved microorganism can be used for chemical production by fermentation. Methods to produce a genetically improved strain can include genetic modification, mutagenesis, and adaptive processes, such as directed evolution. For example, yeasts can be genetically-modified to ferment C5 sugars. Other useful yeasts are species of Candida, Cryptococcus, Debaryomyces, Deddera, Hanseniaspora, Kluyveromyces, Pichia, Schizosaccharomyces, and Zygosaccharomyces. Rhodococus strains, such as Rhodococcus opacus variants are a source of triacylglycerols and other storage lipids. (See, e.g., Waltermann, et al., Microbiology 146:1143-1149 (2000)). Other useful organisms for fermentation include, but are not limited to, yeasts, especially Saccaromyces strains and bacteria such as Clostridium phytofermentans, Thermoanaerobacter ethanolicus, Clostridium thermocellum, Clostridium beijerinickii, Clostridium acetobutylicum, Clostridium tyrobutyricum, Clostridium thermobutyricum, 59 WO 2013/120035 PCT/US2013/025457 Thermoanaerobacterium saccharolyticum, Thermoanaerobacter thermohydrosulfuricus, Clostridium acetobutylicum, Moorella ssp., Carboxydocella ssp., Zymomonas mobilis, recombinant E. Coli, Klebsiella oxytoca, Rhodococcus opacus and Clostridium beijerickii. [00143] An advantage of yeasts are their ability to grow under conditions that include elevated ethanol concentration, high sugar concentration, low sugar concentration, and/or operate under anaerobic conditions. These characteristics, in various combinations, can be used to achieve operation with long or short fermentation cycles and can be used in combination with batch fermentations, fed batch fermentations, self-seeding/partial harvest fermentations, and recycle of cells from the final fermentation as inoculum. [00144] Examples of yeasts that can be used as a biocatalyst or fermentive microorganism in the methods disclosed herein include but are not limited to, species found in the genus Ascoidea, Brettanomyces, Candida, Cephaloascus, Coccidiascus, Dipodascus, Eremothecium, Galactomyces, Kluyveromyces, Pichia, Saccharomyces, Schizosaccharomyces, Sporopachydermia, Torulaspora, Yarrowia, or Zygosaccharomyces; for example, Ascoidea rebescens, Brettanomyces anomalus, Brettanomyces bruxellensis, Brettanomyces claussenii, Brettanomyces custersianus, Brettanomyces lambicus, Brettanomyces naardenensis, Brettanomyces nanus, Candida albicans, Candida ascalaphidarum, Candida amphixiae, Candida antarctica, Candida argentea, Candida atlantica, Candida atmosphaerica, Candida blattae, Candida carpophila, Candida cerambycidarum, Candida chauliodes, Candida corydali, Candida dosseyi, Candida dubliniensis, Candida ergatensis, Candidafructus, Candida glabrata, Candidafermentati, Candida guilliermondii, Candida haemulonii, Candida insectamens, Candida insectorum, Candida intermedia, Candida jeffresii, Candida kefyr, Candida krusei, Candida lusitaniae, Candida lyxosophila, Candida maltosa, Candida marina, Candida membranifaciens, Candida miller, Candida oleophila, Candida oregonensis, Candida parapsilosis, Candida quercitrusa, Candida rugosa, Candida sake, Candida shehatea, Candida temnochilae, Candida tenuis, Candida tropicalis, Candida tsuchiyae, Candida sinolaborantium, Candida sojae, Candida subhashii, Candida viswanathii, Candida utilis, Cephaloascusfragrans, Coccidiascus legeri, Dypodascus albidus, Eremothecium cymbalariae, Galactomyces candidum, Galactomyces geotrichum, Kluyveromyces aestuarii, Kluyveromyces africanus, Kluyveromyces bacillisporus, Kluyveromyces blattae, Kluyveromyces dobzhanskii, Kluyveromyces hubeiensis, Kluyveromyces lactis, Kluyveromyces lodderae, Kluyveromyces marxianus, Kluyveromyces nonfermentans, Kluyveromyces piceae, Kluyveromyces sinensis, Kluyveromyces thermotolerans, Kluyveromyces waltii, Kluyveromyces wickerhamii, 60 WO 2013/120035 PCT/US2013/025457 Kluyveromyces yarrowii, Pichia anomola, Pichia heedii, Pichia guilliermondii, Pichia kluyveri, Pichia membranifaciens, Pichia norvegensis, Pichia ohmeri, Pichia pastoris, Pichia subpelliculosa, Saccharomyces bayanus, Saccharomyces boulardii, Saccharomyces bulderi, Saccharomyces cariocanus, Saccharomyces cariocus, Saccharomyces cerevisiae, Saccharomyces chevalieri, Saccharomyces dairenensis, Saccharomyces ellipsoideus, Saccharomyces eubayanus, Saccharomyces exiguus, Saccharomycesflorentinus, Saccharomyces kluyveri, Saccharomyces martiniae, Saccharomyces monacensis, Saccharomyces norbensis, Saccharomyces paradoxus, Saccharomyces pastorianus, Saccharomyces spencerorum, Saccharomyces turicensis, Saccharomyces unisporus, Saccharomyces uvarum, Saccharomyces zonatus, Schizosaccharomyces cryophilus, Schizosaccharomycesjaponicus, Schizosaccharomyces octosporus, Schizosaccharomyces pombe, Sporopachydermia cereana, Sporopachydermia lactativora, Sporopachydermia quercuum, Torulaspora delbrueckii, Torulasporafranciscae, Torulaspora globosa, Torulaspora pretoriensis, Yarrowia lipolytica, Zygosaccharomyces bailii, Zygosaccharomyces bisporus, Zygosaccharomyces cidri, Zygosaccharomycesfermentati, Zygosaccharomycesflorentinus, Zygosaccharomyces kombuchaensis, Zygosaccharomyces lentus, Zygosaccharomyces mellis, Zygosaccharomyces microellipsoides, Zygosaccharomyces mrakii, Zygosaccharomyces pseudorouxii, or Zygosaccharomyces rouxii, or a variant or genetically modified version thereof [00145] Examples of bacteria that can be used as a biocatalyst or fermentive microorganism in the methods disclosed herein include but are not limited to any bacterium found in the genus of Butyrivibrio, Ruminococcus, Eubacterium, Bacteroides, Acetivibrio, Caldibacillus, Acidothermus, Cellulomonas, Curtobacterium, Micromonospora, Actinoplanes, Streptomyces, Thermobifida, Thermomonospora, Microbispora, Fibrobacter, Sporocytophaga, Cytophaga, Flavobacterium, Achromobacter, Xanthomonas, Cellvibrio, Pseudomonas, Myxobacter, Escherichia, Klebsiella, Thermoanaerobacterium, Thermoanaerobacter, Geobacillus, Saccharococcus, Paenibacillus, Bacillus, Caldicellulosiruptor, Anaerocellum, Anoxybacillus, Zymomonas, Clostridium; for example, Butyrivibrio fibrisolvens, Ruminococcusflavefaciens, Ruminococcus succinogenes, Ruminococcus albus, Eubacterium cellulolyticum, Bacteroides cellulosolvens, Acetivibrio cellulolyticus, Acetivibrio cellulosolvens, Caldibacillus cellulovorans, Bacillus circulans, Acidothermus cellulolyticus, Cellulomonas cartae, Cellulomonas cellasea, Cellulomonas cellulans, Cellulomonasfimi, Cellulomonasflavigena, Cellulomonas gelida, Cellulomonas iranensis, Cellulomonas persica, Cellulomonas uda, Curtobacteriumfalcumfaciens, 61 WO 2013/120035 PCT/US2013/025457 Micromonospora melonosporea, Actinoplanes aurantiaca, Streptomyces reticuli, Streptomyces alboguseolus, Streptomyces aureofaciens, Streptomyces cellulolyticus, Streptomycesflavogriseus, Streptomyces lividans, Streptomyces nitrosporeus, Streptomyces olivochromogenes, Streptomyces rochei, Streptomyces thermovulgaris, Streptomyces viridosporus, Thermobifida alba, Thermobifidafusca, Thermobifida cellulolytica, Thermomonospora curvata, Microbispora bispora, Fibrobacter succinogenes, Sporocytophaga myxococcoides, Cytophaga sp., Flavobacterium johnsoniae, Achromobacter piechaudii, Xanthomonas sp., Cellvibrio vulgaris, Cellvibrio fulvus, Cellvibrio gilvus, Cellvibrio mixtus, Pseudomonasfluorescens, Pseudomonas mendocina, Myxobacter sp. AL 1, Escherichia albertii, Escherichia blattae, Escherichia coli, Escherichia fergusonii, Escherichia hermannii, Escherichia vulneris, Klebsiella granulomatis, Klebsiella oxytoca, Klebsiella pneumonia, Klebsiella terrigena, Thermoanaerobacterium thermosulfurigenes, Thermoanaerobacterium aotearoense, Thermoanaerobacterium polysaccharolyticum, Thermoanaerobacterium zeae, Thermoanaerobacterium xylanolyticum, Thermoanaerobacterium saccharolyticum, Thermoanaerobium brockii, Thermoanaerobacterium thermosaccharolyticum, Thermoanaerobacter thermohydrosulfuricus, Thermoanaerobacter ethanolicus, Thermoanaerobacter brocki, Geobacillus thermoglucosidasius, Geobacillus stearothermophilus, Saccharococcus caldoxylosilyticus, Saccharoccus thermophilus, Paenibacillus campinasensis, Bacillus flavothermus, Anoxybacillus kamchatkensis, Anoxybacillus gonensis, Caldicellulosiruptor acetigenus, Caldicellulosiruptor saccharolyticus, Caldicellulosiruptor kristjanssonii, Caldicellulosiruptor owensensis, Caldicellulosiruptor lactoaceticus, Anaerocellum thermophilum, Clostridium thermocellum, Clostridium cellulolyticum, Clostridium straminosolvens, Clostridium acetobutylicum, Clostridium aerotolerans, Clostridium beijerinckii, Clostridium bifermentans, Clostridium botulinum, Clostridium butyricum, Clostridium cadaveric, Clostridium chauvoei, Clostridium clostridioforme, Clostridium colicanis, Clostridium difficile, Clostridiumfallax, Clostridium formicaceticum, Clostridium histolyticum, Clostridium innocuum, Clostridium jungdahlii, Clostridium laramie, Clostridium lavalense, Clostridium novyi, Clostridium oedematiens, Clostridium paraputrificum, Clostridium perfringens, Clostridium phytofermentans, Clostridium piliforme, Clostridium ramosum, Clostridium scatologenes, Clostridium septicum, Clostridium sordellii, Clostridium sporogenes, Clostridium tertium, Clostridium tetani, Clostridium tyrobutyricum, Clostridium thermobutyricum, Zymomonas mobilis, or a variant or genetically modified version thereof 62 WO 2013/120035 PCT/US2013/025457 [00146] In one embodiment, fed-batch fermentation is performed on the treated biomass to produce a fermentation end-product, such as alcohol, ethanol, organic acid, succinic acid, TAG, or hydrogen. In one embodiment, the fermentation process comprises simultaneous hydrolysis and fermentation (SSF) of the biomass using one or more microorganisms such as a Rhodococcus strain, a Clostridium strain, a Trichoderma strain, a Saccharomyces strain, a Zymomonas strain, or another microorganism suitable for fermentation of biomass. In another embodiment, the fermentation process comprises simultaneous hydrolysis and fermentation of the biomass using a microorganism that is Clostridium algidixylanolyticum, Clostridium xylanolyticum, Clostridium cellulovorans, Clostridium cellulolyticum, Clostridium thermocellum, Clostridium josui, Clostridium papyrosolvens, Clostridium cellobioparum, Clostridium hungatei, Clostridium cellulosi, Clostridium stercorarium, Clostridium termitidis, Clostridium thermocopriae, Clostridium celerecrescens, Clostridium polysaccharolyticum, Clostridium populeti, Clostridium lentocellum, Clostridium chartatabidum, Clostridium aldrichii, Clostridium herbivorans, Clostridium phytofermentans, Acetivibrio cellulolyticus, Bacteroides cellulosolvens, Caldicellulosiruptor saccharolyticum, Ruminococcus albus, Ruminococcusflavefaciens, Fibrobacter succinogenes, Eubacterium cellulosolvens, Butyrivibrio fibrisolvens, Anaerocellum thermophilum, Halocella cellulolytica, Thermoanaerobacterium thermosaccharolyticum, Sacharophagus degradans, or Thermoanaerobacterium saccharolyticum. [00147] In one embodiment, the fermentation process can include separate hydrolysis and fermentation (SHF) of a biomass with one or more enzymes, such as a xylanases, endo 1,4-beta-xylanases, xylosidases, beta-D-xylosidases, cellulases, hemicellulases, carbohydrases, glucanases, endoglucanases, endo-1,4-beta-glucanases, exoglucanases, glucosidases, beta-D-glucosidases, amylases, cellobiohydrolases, exocellobiohydrolases, phytases, proteases, peroxidase, pectate lyases, galacturonases, or laccases. In one embodiment, one or more enzymes used to treat a biomass is thermostable. In another embodiment, a biomass is treated with one or more enzymes, such as those provided herein, prior to fermentation. In another embodiment, a biomass is treated with one or more enzymes, such as those provided herein, during fermentation. In another embodiment, a biomass is treated with one or more enzymes, such as those provided herein, prior to fermentation and during fermentation. In another embodiment, an enzyme used for hydrolysis of a biomass is the same as those added during fermentation. In another embodiment, an enzyme used for hydrolysis of biomass is different from those added during fermentation. 63 WO 2013/120035 PCT/US2013/025457 [00148] In some embodiments, fermentation can be performed in an apparatus such as bioreactor, a fermentation vessel, a stirred tank reactor, or a fluidized bed reactor. In one embodiment, the treated biomass can be supplemented with suitable chemicals to facilitate robust growth of the one or more fermenting organisms. In one embodiment, a useful supplement includes but is not limited to, a source of nitrogen and/or amino acids such as yeast extract, cysteine, or ammonium salts (e.g. nitrate, sulfate, phosphate etc.); a source of simple carbohydrates such as corn steep liquor, and malt syrup; a source of vitamins such as yeast extract; buffering agents such as salts (including but not limited to citrate salts, phosphate salts, or carbonate salts); or mineral nutrients such as salts of magnesium, calcium, or iron. In some embodiments redox modifiers are added to the fermentation mixture including but not limited to cysteine or mercaptoethanol. [00149] In one embodiment, the titer and/or productivity of fermentation end-product production by a microorganism is improved by culturing the microorganism in a medium comprising one or more compounds comprising hexose and/or pentose sugars. In one embodiment, a process comprises conversion of a starting material (such as a biomass) to a biofuel, such as one or more alcohols. In one embodiment, methods can comprise contacting substrate comprising both hexose (e.g. glucose, cellobiose) and pentose (e.g. xylose, arabinose) saccharides with a microorganism that can hydrolyze C5 and C6 saccharides to produce ethanol. In another embodiment, methods can comprise contacting substrate comprising both hexose (e.g. glucose, cellobiose) and pentose (e.g. xylose, arabinose) saccharides with R. opacus to produce TAG. [001501 In some embodiments, batch fermentation with a microorganism of a mixture of hexose and pentose saccharides using the methods disclosed herein can provide uptake rates of about 0.1-8 g/L/h or more of hexose and about 0.1-8 g/L/h or more of pentose (xylose, arabinose, etc.). In some embodiments, batch fermentation with a microorganism of a mixture of hexose and pentose saccharides using the methods disclosed herein can provide uptake rates of about 0.1, 0.2, 0.4, 0.5, 0.6 0.7, 0.8, 1, 2, 3, 4, 5, or 6 g/L/h or more of hexose and about 0.1, 0.2, 0.4, 0.5, 0.6 0.7, 0.8, 1, 2, 3, 4, 5, or 6 g/L/h or more of pentose. [001511 In one embodiment, a method for production of ethanol or another alcohol produces about 10 g/l to 120 gain 40 hours or less. In another embodiment, a method for production of ethanol produces about 10 g/l, 11 g/L, 12 g/L, 13 g/L, 14 g/L, 15 g/L, 16 g/L, 17 g/L, 18 g/L, 19 g/L, 20 g/L, 21 g/L, 22 g/L, 23 g/L, 24 g/L, 25 g/L, 26 g/L, 27 g/L, 28 g/L, 29 g/L, 30 g/L, 31 g/L, 32 g/L, 33 g/L, 34 g/L, 35 g/L, 36 g/L, 37 g/L, 38 g/L, 39 g/L, 40 g/L, 41 g/L, 42 g/L, 43 g/L, 44 g/L, 45 g/L, 46 g/L, 47 g/L, 48 g/L, 49 g/L, 50 g/L, 51 g/L, 52 g/L, 64 WO 2013/120035 PCT/US2013/025457 53 g/L, 54 g/L, 55 g/L, 56 g/L, 57 g/L, 58 g/L, 59 g/L, 60 g/L, 61 g/L, 62 g/L, 63 g/L, 64 g/L, 65 g/L, 66 g/L, 67 g/L, 68 g/L, 69 g/L, 70 g/L, 71 g/L, 72 g/L, 73 g/L, 74 g/L, 75 g/L, 76 g/L, 77 g/L, 78 g/L, 79 g/L, 80 g/L, 81 g/L, 82 g/L, 83 g/L, 84 g/L, 85 g/L, 86 g/L, 87 g/L, 88 g/L, 89 g/L, 90 g/L, 91 g/L, 92 g/L, 93 g/L, 94 g/L, 95 g/L, 96 g/L, 97 g/L, 98 g/L, 99 g/L, 100 g/L, 110 g/l, 120 g/l, or more alcohol in 40 hours by the fermentation of biomass. In another embodiment, alcohol is produced by a method comprising simultaneous fermentation of hexose and pentose saccharides. In another embodiment, alcohol is produced by a microorganism comprising simultaneous fermentation of hexose and pentose saccharides. [00152] In another embodiment, the level of a medium component is maintained at a desired level by adding additional medium component as the component is consumed or taken up by the organism. Examples of medium components included, but are not limited to, carbon substrate, nitrogen substrate, vitamins, minerals, growth factors, cofactors, and biocatalysts. The medium component can be added continuously or at regular or irregular intervals. In one embodiment, additional medium component is added prior to the complete depletion of the medium component in the medium. In one embodiment, complete depletion can effectively be used, for example to initiate different metabolic pathways, to simplify downstream operations, or for other reasons as well. In one embodiment, the medium component level is allowed to vary by about 10% around a midpoint, in one embodiment, it is allowed to vary by about 30% around a midpoint, and in one embodiment, it is allowed to vary by 60% or more around a midpoint. In one embodiment, the medium component level is maintained by allowing the medium component to be depleted to an appropriate level, followed by increasing the medium component level to another appropriate level. In one embodiment, a medium component, such as vitamin, is added at two different time points during fermentation process. For example, one-half of a total amount of vitamin is added at the beginning of fermentation and the other half is added at midpoint of fermentation. [00153] In another embodiment, the nitrogen level is maintained at a desired level by adding additional nitrogen-containing material as nitrogen is consumed or taken up by the organism. The nitrogen-containing material can be added continuously or at regular or irregular intervals. Useful nitrogen levels include levels of about 5 to about 10 g/L. In one embodiment, levels of about I to about 12 g/L can also be usefully employed. In another embodiment, levels, such as about 0.5, 0.1 g/L or even lower, and higher levels, such as about 20, 30 g/L or even higher are used. In another embodiment, a useful nitrogen level is about 0.01, 0.05, 0.1, 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19, 20, 21, 22 23, 24, 25, 26, 27, 28, 29 or 30 g/L. Nitrogen can be supplied as 65 WO 2013/120035 PCT/US2013/025457 a simple nitrogen-containing material, such as an ammonium compounds (e.g. ammonium sulfate, ammonium hydroxide, ammonia, ammonium nitrate, or any other compound or mixture containing an ammonium moiety), nitrate or nitrite compounds (e.g. potassium, sodium, ammonium, calcium, or other compound or mixture containing a nitrate or nitrite moiety), or as a more complex nitrogen-containing material, such as amino acids, proteins, hydrolyzed protein, hydrolyzed yeast, yeast extract, dried brewer's yeast, yeast hydrolysates, distillers' grains, soy protein, hydrolyzed soy protein, fermentation products, and processed or corn steep powder or unprocessed protein-rich vegetable or animal matter, including those derived from bean, seeds, soy, legumes, nuts, milk, pig, cattle, mammal, fish, as well as other parts of plants and other types of animals. Nitrogen-containing materials useful in various embodiments also include materials that contain a nitrogen-containing material, including, but not limited to mixtures of a simple or more complex nitrogen-containing material mixed with a carbon source, another nitrogen-containing material, or other nutrients or non nutrients, and AFEX treated plant matter. [00154] In another embodiment, the carbon level is maintained at a desired level by adding sugar compounds or material containing sugar compounds ("Sugar-Containing Material") as sugar is consumed or taken up by the organism. The sugar-containing material can be added continuously or at regular or irregular intervals. In one embodiment, additional sugar-containing material is added prior to the complete depletion of the sugar compounds available in the medium. In one embodiment, complete depletion can effectively be used, for example to initiate different metabolic pathways, to simplify downstream operations, or for other reasons as well. In one embodiment, the carbon level (as measured by the grams of sugar present in the sugar-containing material per liter of broth) is allowed to vary by about 10% around a midpoint, in one embodiment, it is allowed to vary by about 30% around a midpoint, and in one embodiment, it is allowed to vary by 60% or more around a midpoint. In one embodiment, the carbon level is maintained by allowing the carbon to be depleted to an appropriate level, followed by increasing the carbon level to another appropriate level. In some embodiments, the carbon level can be maintained at a level of about 5 to about 120 g/L. However, levels of about 30 to about 100 g/L can also be usefully employed as well as levels of about 60 to about 80 g/L. In one embodiment, the carbon level is maintained at greater than 25 g/L for a portion of the culturing. In another embodiment, the carbon level is maintained at about 5 g/L, 6 g/L, 7 g/L, 8 g/L, 9 g/L, 10 g/L, 11 g/L, 12 g/L, 13 g/L, 14 g/L, 15 g/L, 16 g/L, 17 g/L, 18 g/L, 19 g/L, 20 g/L, 21 g/L, 22 g/L, 23 g/L, 24 g/L, 25 g/L, 26 g/L, 27 g/L, 28 g/L, 29 g/L, 30 g/L, 31 g/L, 32 g/L, 33 g/L, 34 g/L, 35 g/L, 36 g/L, 37 g/L, 38 g/L, 66 WO 2013/120035 PCT/US2013/025457 39 g/L, 40 g/L, 41 g/L, 42 g/L, 43 g/L, 44 g/L, 45 g/L, 46 g/L, 47 g/L, 48 g/L, 49 g/L, 50 g/L, 51 g/L, 52 g/L, 53 g/L, 54 g/L, 55 g/L, 56 g/L, 57 g/L, 58 g/L, 59 g/L, 60 g/L, 61 g/L, 62 g/L, 63 g/L, 64 g/L, 65 g/L, 66 g/L, 67 g/L, 68 g/L, 69 g/L, 70 g/L, 71 g/L, 72 g/L, 73 g/L, 74 g/L, 75 g/L, 76 g/L, 77 g/L, 78 g/L, 79 g/L, 80 g/L, 81 g/L, 82 g/L, 83 g/L, 84 g/L, 85 g/L, 86 g/L, 87 g/L, 88 g/L, 89 g/L, 90 g/L, 91 g/L, 92 g/L, 93 g/L, 94 g/L, 95 g/L, 96 g/L, 97 g/L, 98 g/L, 99 g/L, 100 g/L, 101 g/L, 102 g/L, 103 g/L, 104 g/L, 105 g/L, 106 g/L, 107 g/L, 108 g/L, 109 g/L, 110 g/L, 111 g/L, 112 g/L, 113 g/L, 114 g/L, 115 g/L, 116 g/L, 117 g/L, 118 g/L, 119 g/L, 120 g/L, 121 g/L, 122 g/L, 123 g/L, 124 g/L, 125 g/L, 126 g/L, 127 g/L, 128 g/L, 129 g/L, 130 g/L, 131 g/L, 132 g/L, 133 g/L, 134 g/L, 135 g/L, 136 g/L, 137 g/L, 138 g/L, 139 g/L, 140 g/L, 141 g/L, 142 g/L, 143 g/L, 144 g/L, 145 g/L, 146 g/L, 147 g/L, 148 g/L, 149 g/L, or 150 g/L. [001551 The carbon substrate, like the nitrogen substrate, can be used for cell production and enzyme production, but unlike the nitrogen substrate, the carbon substrate can serve as the raw material for production of fermentation end-products. Frequently, more carbon substrate can lead to greater production of fermentation end-products. In another embodiment, it can be advantageous to operate with the carbon level and nitrogen level related to each other for at least a portion of the fermentation time. In one embodiment, the ratio of carbon to nitrogen is maintained within a range of about 30:1 to about 10:1. In another embodiment, the ratio of carbon nitrogen is maintained from about 20:1 to about 10:1 or more preferably from about 15:1 to about 10:1. In another embodiment, the ratio of carbon nitrogen is about 30:1, 29:1, 28:1, 27:1, 26:1, 25:1, 24:1, 23:1, 22:1, 21:1, 20:1, 19:1, 18:1, 17:1, 16:1, 15:1, 14:1, 13:1, 12:1, 11:1, 10:1, 9:1, 8:1, 7:1, 6:1, 5:1, 4:1, 3:1, 2:1, or 1:1. [00156] Maintaining the ratio of carbon and nitrogen ratio within particular ranges can result in benefits to the operation such as the rate of metabolism of carbon substrate, which depends on the amount of carbon substrate and the amount and activity of enzymes present, being balanced to the rate of end product production. Balancing the carbon to nitrogen ratio can, for example, facilitate the sustained production of these enzymes such as to replace those which have lost activity. [001571 In another embodiment, the amount and/or timing of carbon, nitrogen, or other medium component addition can be related to measurements taken during the fermentation. For example, the amount of monosaccharides present, the amount of insoluble polysaccharide present, the polysaccharase activity, the amount of product present, the amount of cellular material (for example, packed cell volume, dry cell weight, etc.) and/or the amount of nitrogen (for example, nitrate, nitrite, ammonia, urea, proteins, amino acids, etc.) present can 67 WO 2013/120035 PCT/US2013/025457 be measured. The concentration of the particular species, the total amount of the species present in the fermentor, the number of hours the fermentation has been running, and the volume of the fermentor can be considered. In various embodiments, these measurements can be compared to each other and/or they can be compared to previous measurements of the same parameter previously taken from the same fermentation or another fermentation. Adjustments to the amount of a medium component can be accomplished such as by changing the flow rate of a stream containing that component or by changing the frequency of the additions for that component. For example, the amount of saccharide can be increased when the cell production increases faster than the end product production. In another embodiment, the amount of nitrogen can be increased when the enzyme activity level decreases. [001581 In another embodiment, a fed batch operation can be employed, wherein medium components and/or fresh cells are added during the fermentation without removal of a portion of the broth for harvest prior to the end of the fermentation. In one embodiment, a fed-batch process is based on feeding a growth limiting nutrient medium to a culture of microorganisms. In one embodiment, the feed medium is highly concentrated to avoid dilution of the bioreactor. In another embodiment, the controlled addition of the nutrient directly affects the growth rate of the culture and avoids overflow metabolism such as the formation of side metabolites. In one embodiment, the growth limiting nutrient is a nitrogen source or a saccharide source. [001591 In various embodiments, particular medium components can have beneficial effects on the performance of the fermentation, such as increasing the titer of desired products, or increasing the rate that the desired products are produced. Specific compounds can be supplied as a specific, pure ingredient, such as a particular amino acid, or it can be supplied as a component of a more complex ingredient, such as using a microbial, plant or animal product as a medium ingredient to provide a particular amino acid, promoter, cofactor, or other beneficial compound. In some cases, the particular compound supplied in the medium ingredient can be combined with other compounds by the organism resulting in a fermentation-beneficial compound. One example of this situation would be where a medium ingredient provides a specific amino acid which the organism uses to make an enzyme beneficial to the fermentation. Other examples can include medium components that are used to generate growth or product promoters, etc. In such cases, it can be possible to obtain a fermentation-beneficial result by supplementing the enzyme, promoter, growth factor, etc. or 68 WO 2013/120035 PCT/US2013/025457 by adding the precursor. In some situations, the specific mechanism whereby the medium component benefits the fermentation is not known, only that a beneficial result is achieved. [001601 In one embodiment, a fermentation to produce a fuel is performed by culturing a strain of R. opacus in a medium having a supplement of lignin component and a concentration of one or more carbon sources. The resulting production of end product such as TAG can be up to 1-fold, 2-fold, 3-fold, 4-fold, 5-fold, 6-fold, 7-fold, 8-fold, 9-fold, and in some cases up to 10-fold and higher in volumetric productivity than a process using only the addition of a relatively pure saccharide source, and can achieve a carbon conversion efficiency approaching the theoretical maximum. The theoretical maximum can vary with the substrate and product. For example, the generally accepted maximum efficiency for conversion of glucose to ethanol is 0.51 g ethanol/g glucose. In one embodiment, a biocatalyst can produce about 40-100% of a theoretical maximum yield of ethanol. In another embodiment, a biocatalyst can produce up to about 40%, 50%, 60%, 70%, 80%, 90%, 95% and even 100% of the theoretical maximum yield of ethanol. In one embodiment, abiocatalystcanproduceupto about 1%, 2%,3 %,4 0 %,5 %,6 0 %,7%,8 %,9%, 10 %, 11 %, 12 %, 13 %, 14 %, 15 %, 16 %, 17 %, 18 %, 19 %,20 %,21 %,22 %,23 %,24 %,25 %, 26 %, 27 %, 28 %, 29 %, 30 %, 31 %, 32 %, 33 %, 34 %, 35 %, 36 %, 37 %, 38 %, 39 %, 40 %, 41 %, 42 %, 43 %, 44 %, 45 %, 46 %, 47 %, 48 %, 49 %, 50 %, 51 %, 52 %, 53 %, 54 %, 55 %, 56 %, 57 %, 58 %, 59 %, 60 %, 61 %, 62 %, 63 %, 64 %, 65 %, 66 %, 67 %, 68 %, 69 %, 70 %, 71 %, 72 %, 73 %, 74 %, 75 %, 76 %, 77 %, 78 %, 79 %, 80 %, 81 %, 82 %, 83 %, 84 %, 85 %, 86 %, 87 %, 88 %, 89 %, 90 %, 91 %, 92 %, 93 %, 94 %, 95 %, 96 %, 97 %, 98 %, 99 %, 99.99 %, orlO % of a theoretical maximum yield of a fuel. It can be possible to obtain a fermentation-beneficial result by supplementing the medium with a pretreatment or hydrolysis component. In some situations, the specific mechanism whereby the medium component benefits the fermentation is not known, only that a beneficial result is achieved. [00161] Various embodiments offer benefits relating to improving the titer and/or productivity of fermentation end-product production by a biocatalyst by culturing the organism in a medium comprising one or more compounds comprising particular fatty acid moieties and/or culturing the organism under conditions of controlled pH. [00162] In one embodiment, the pH of the medium is controlled at less than about pH 7.2 for at least a portion of the fermentation. In one embodiment, the pH is controlled within a range of about pH 3.0 to about 7.1 or about pH 4.5 to about 7.1, or about pH 5.0 to about 6.3, or about pH 5.5 to about 6.3, or about pH 6.0 to about 6.5, or about pH 5.5 to about 6.9 or about pH 6.2 to about 6.7. The pH can be controlled by the addition of a pH modifier. In 69 WO 2013/120035 PCT/US2013/025457 one embodiment, a pH modifier is an acid, a base, a buffer, or a material that reacts with other materials present to serve to raise of lower the pH. In one embodiment, more than one pH modifier can be used, such as more than one acid, more than one base, one or more acid with one or more bases, one or more acids with one or more buffers, one or more bases with one or more buffers, or one or more acids with one or more bases with one or more buffers. When more than one pH modifiers are utilized, they can be added at the same time or at different times. In one embodiment, one or more acids and one or more bases can be combined, resulting in a buffer. In one embodiment, media components, such as a carbon source or a nitrogen source can also serve as a pH modifier; suitable media components include those with high or low pH or those with buffering capacity. Exemplary media components include acid- or base-hydrolyzed plant polysaccharides having with residual acid or base, AFEX treated plant material with residual ammonia, lactic acid, corn steep solids or liquor. [001631 In one embodiment, a constant pH can be utilized throughout the fermentation. In one embodiment, the timing and/or amount of pH reduction can be related to the growth conditions of the cells, such as in relation to the cell count, the end product produced, the end product present, or the rate of end product production. In one embodiment, the pH reduction can be made in relation to physical or chemical properties of the fermentation, such as viscosity, medium composition, gas production, off gas composition, etc. [00164] Recovery of Fermentation End Products [001651 In another aspect, methods are provided for the recovery of the fermentive end products, such as an alcohol (e.g. ethanol, propanol, methanol, butanol, etc.) another biofuel or chemical product. In one embodiment, broth will be harvested at some point during of the fermentation, and fermentive end product or products will be recovered. The broth with end product to be recovered will include both end product and impurities. The impurities include materials such as water, cell bodies, cellular debris, excess carbon substrate, excess nitrogen substrate, other remaining nutrients, other metabolites, and other medium components or digested medium components. During the course of processing the broth, the broth can be heated and/or reacted with various reagents, resulting in additional impurities in the broth. [001661 In one embodiment, the processing steps to recover end product frequently includes several separation steps, including, for example, distillation of a high concentration alcohol material from a less pure alcohol-containing material. In one embodiment, the high concentration alcohol material can be further concentrated to achieve very high concentration alcohol, such as 98% or 99% or 99.5% (wt.) or even higher. Other separation steps, such as 70 WO 2013/120035 PCT/US2013/025457 filtration, centrifugation, extraction, adsorption, etc. can also be a part of some recovery processes for alcohol as a product or biofuel, or other biofuels or chemical products. [001671 In one embodiment, a process can be scaled to produce commercially useful biofuels. In another embodiment, biocatalyst is used to produce an alcohol, e.g., ethanol, butanol, propanol, methanol, or a fuel such as hydrocarbons hydrogen, TAG, and hydroxy compounds. In another embodiment, biocatalyst is used to produce a carbonyl compound such as an aldehyde or ketone (e.g. acetone, formaldehyde, 1-propanal, etc.), an organic acid, a derivative of an organic acid such as an ester (e.g. wax ester, glyceride, etc.), 1, 2 propanediol, 1, 3-propanediol, lactic acid, formic acid, acetic acid, succinic acid, pyruvic acid, or an enzyme such as a cellulase, polysaccharase, lipases, protease, ligninase, and hemicellulase. [00168] In one embodiment, useful biochemicals can be produced from non-food plant biomass, with a steam or hot-water extraction technique that is carried out by contacting a charge of non-food plant pretreated biomass material such as corn stover or sorhum with water and/or acid (with or without additional process enhancing compounds or materials), in a pressurized vessel at an elevated temperature up to about 160 -220' C. and at a pH below about 7.0, to yield an aqueous (extract solution) mixture of useful sugars including long chain saccharides (sugars), acetic acid, and lignin, while leaving the structural (cellulose and lignin) portion of the lignocellulosic material largely intact. In combination, these potential inhibitory chemicals especially sugar degradation products are low, and the plant derived nutrients that are naturally occurring lignocellulosic-based components are also recovered that are beneficial to a C5 and/or C6 fermenting organism. Toward this objective, the aqueous extract is concentrated (by centrifugation, filtration, solvent extraction, flocculation, evaporation), by producing a concentrated sugar stream, apart from the other hemicellulose (C5 rich) and cellulosic derived sugars (C6 rich) which are channeled into a fermentable stream. [00169] Biofuel plant and process of producing biofuel: [001701 Large Scale Fuel and Chemical Production from Biomass [001711 Generally, there are several basic approaches to producing fuels and chemical end-products from biomass on a large scale utilizing of microbial cells. In the one method, one first pretreats and hydrolyzes a biomass material that includes high molecular weight carbohydrates to lower molecular weight carbohydrates, and then ferments the lower molecular weight carbohydrates utilizing of microbial cells to produce fuel or other products. In the second method, one treats the biomass material itself using mechanical, chemical 71 WO 2013/120035 PCT/US2013/025457 and/or enzymatic methods. In all methods, depending on the type of biomass and its physical manifestation, one of the processes can comprise a milling of the carbonaceous material, via wet or dry milling, to reduce the material in size and increase the surface to volume ratio (physical modification). [00172] In one embodiment, hydrolysis can be accomplished using acids, e.g., Bronsted acids (e.g., sulfuric or hydrochloric acid), bases, e.g., sodium hydroxide, hydrothermal processes, ammonia fiber explosion processes ("AFEX"), lime processes, enzymes, or combination of these. Hydrogen, and other end products of the fermentation can be captured and purified if desired, or disposed of, e.g., by burning. For example, the hydrogen gas can be flared, or used as an energy source in the process, e.g., to drive a steam boiler, e.g., by burning. Hydrolysis and/or steam treatment of the biomass can, e.g., increase porosity and/or surface area of the biomass, often leaving the cellulosic materials more exposed to the biocatalyst cells, which can increase fermentation rate and yield. Removal of lignin can, e.g., provide a combustible fuel for driving a boiler, and can also, e.g., increase porosity and/or surface area of the biomass, often increasing fermentation rate and yield. Generally, in any of the these embodiments, the initial concentration of the carbohydrates in the medium is greater than 20 mM, e.g., greater than 30 mM, 50 mM, 75 mM, 100 mM, 150 mM, 200 mM, or even greater than 500 mM. [00173] Biomass processing plant and process ofproducing products from biomass [00174] In one aspect, a fuel or chemical plant that includes a pretreatment unit to prepare biomass for improved exposure and biopolymer separation, a hydrolysis unit configured to hydrolyze a biomass material that includes a high molecular weight carbohydrate, and one or more product recovery system(s) to isolate a product or products and associated by-products and co-products is provided. In another aspect, methods of purifying lower molecular weight carbohydrate from solid byproducts and/or toxic impurities is provided. [001751 In another aspect, methods of making a product or products that include combining biocatalyst cells of a microorganism and a biomass feed in a medium wherein the biomass feed contains lower molecular weight carbohydrates and unseparated solids and/or other liquids from pretreatment and hydrolysis, and fermenting the biomass material under conditions and for a time sufficient to produce a biofuel, chemical product or fermentive end products, e.g. ethanol, propanol, hydrogen, succinic acid, lignin, terpenoids, and the like as described above, is provided. 72 WO 2013/120035 PCT/US2013/025457 [00176] In another aspect, products made by any of the processes described herein is also provided herein. [001771 One example is a method for producing chemical products from biomass by first treating biomass with an acid at elevated temperature and pressure in a hydrolysis unit. The biomass may first be heated by addition of hot water or steam. The biomass may be acidified by bubbling gaseous sulfur dioxide through the biomass that is suspended in water, or by adding a strong acid, e.g., sulfuric, hydrochloric, or nitric acid with or without preheating/presteaming/water addition. During the acidification, the pH is maintained at a low level, e.g., below about 5. The temperature and pressure may be elevated after acid addition. In addition to the acid already in the acidification unit, optionally, a metal salt such as ferrous sulfate, ferric sulfate, ferric chloride, aluminum sulfate, aluminum chloride, magnesium sulfate, or mixtures of these can be added to aid in the acid hydrolysis of the biomass. The acid-impregnated biomass is fed into the hydrolysis section of the pretreatment unit. Steam is injected into the hydrolysis portion of the pretreatment unit to directly contact and heat the biomass to the desired temperature. The temperature of the biomass after steam addition is, e.g., between about 1300 C and 220' C. The acid hydrolysate is then discharged into the flash tank portion of the pretreatment unit, and is held in the tank for a period of time to further hydrolyze the biomass, e.g., into oligosaccharides and monomeric sugars. Other methods can also be used to further break down biomass. Alternatively, the biomass can be subject to discharge through a pressure lock for any high-pressure pretreatment process. Hydrolysate is then discharged from the pretreatment reactor, with or without the addition of water, e.g., at solids concentrations between about 10% and 60%. [001781 After pretreatment, the biomass may be dewatered and/or washed with a quantity of water, e.g. by squeezing or by centrifugation, or by filtration using, e.g. a countercurrent extractor, wash press, filter press, pressure filter, a screw conveyor extractor, or a vacuum belt extractor to remove acidified fluid. Wash fluids can be collected to concentrate the C5 saccharides in the wash stream. The acidified fluid, with or without further treatment, e.g. addition of alkali (e.g. lime) and or ammonia (e.g. ammonium phosphate), can be re-used, e.g., in the acidification portion of the pretreatment unit, or added to the fermentation, or collected for other use/treatment. Products may be derived from treatment of the acidified fluid, e.g., gypsum or ammonium phosphate. Enzymes or a mixture of enzymes can be added during pretreatment to hydrolyze, e.g. endoglucanases, exoglucanases, cellobiohydrolases (CBH), beta-glucosidases, glycoside hydrolases, glycosyltransferases, alphyamylases, chitinases, pectinases, lyases, and esterases active 73 WO 2013/120035 PCT/US2013/025457 against components of cellulose, hemicelluloses, pectin, and starch, in the hydrolysis of high molecular weight components. [001791 A fermentor, attached or at a separate site, can be fed with hydrolyzed biomass, any liquid fraction from biomass pretreatment, an active seed culture of a biocatalyst, such as a yeast, if desired a co-fermenting microbe, e.g., another yeast or E. coli, and, if required, nutrients to promote growth of the biocatalyst or other microbes. Alternatively, the pretreated biomass or liquid fraction can be split into multiple fermenters, each containing a different strain of a biocatalyst and/or other microbes, and each operating under specific physical conditions. Fermentation is allowed to proceed for a period of time, e.g., between about 1 and 150 hours, while maintaining a temperature of, e.g., between about 250 C and 50' C. Gas produced during the fermentation is swept from fermentor and is discharged, collected, or flared with or without additional processing, e.g. hydrogen gas may be collected and used as a power source or purified as a co-product. [00180] In another aspect, methods of making a fuel or fuels that include combining one or more biocatalyst and a lignocellulosic material (and/or other biomass material) in a medium, adding a lignin fraction from pretreatment, and fermenting the lignocellulosic material under conditions and for a time sufficient to produce a fuel or fuels, e.g., ethanol, propanol and/or hydrogen or another chemical compound is provided herein. [00181] In another aspect, the products made by any of the processes described herein is provided. EXAMPLES [00182] The following examples serve to illustrate certain embodiments and aspects and are not to be construed as limiting the scope thereof [00183] Example 1. Maintenance of DDGS levels. [00184] To supplement C6 with corn mash, a 20% C6 solution is added to an 80% corn mash for an SSF fermentation. The 80% corn mash slurry contains 30% solids which are comprised of 72% starch, 12-15% glucan, oil and fiber about 7 -10%. The oil and fiber, after the fermentation of the starch and glucan, constitutes what is called DDGS and can be sold as feed, primarily for cattle. The starch fermentation results in 21-22% sugars which can be converted to 10-11% ethanol. [001851 If starch-derived sugar is blended with 26-30% C6 concentration in the ratio described supra (20:80), and then fermented, there can be an increase in sugar yields. The totals are 25-26% sugar which translates into a 12-13% ethanol yield. However, 20% of the 74 WO 2013/120035 PCT/US2013/025457 DDGS can be lost due to the dilution of the corn mash solids. The ethanol yield can be increased but there can be a loss of income from the DDGS yield. [001861 The solution is to add a greater concentration of the solids (36% solids instead of 30% solids) to the 80% corn mash solution. Corn mash cannot normally be fermented at a high solids content (36%). However, because the solids are diluted in a C6-supplemented fermentation, DDGS yields can be maintained. Thus, in a 1000 gallon tank, 800 gallons of corn mash containing 36% solids can be supplemented with 200 gallons of C6 solution containing 26-30% C6 sugar, to prevent loss of DDGS. The corn mash solution, that cannot be fermented as 36% solids can be diluted to 30% solids. Thus there can be an increase of ethanol yield (or sugar yield) and production of the same amount of DDGS. The 3-4% increase in sugar can lead to a 1-2% increase in ethanol [001871 Example 2. Preparation of Cellulosic-Derived C6 Fermentable Sugars (from sorghum and switchgrass) [001881 Non-food cellulosic feedstock is received and pre-processed. First, oversized materials (example large chunks of wood) and contaminates (for example stones, soil, etc.) are selected and removed in a gross screening process. The undersized particles, or fines, including contaminates, such as sand, soil or the like, are separated and removed in a fine screening process. The remaining lignocellulosic material can be triturated (e.g., by chipping, tub grinding, hammer milling, or other available comminuting procedure) to reduce the feedstock to the preferred size and condition for further handling and processing. [001891 In one example, switch grass and ensiled energy sorghum was used. Switch grass was dried and hammer milled to reduce particle size. In the case of ensiled energy sorghum, the material was chopped and ensiled in a bunker. The water content of each biomass feedstock was determined and adjusted to a solids content of about 15% (wt/v) solids and moisture content of about 85% (wt/v) using a 24 hour soaking treatment. [00190] The moisture-adjusted switch grass and energy sorghum feedstocks were separately prepared for an acid-catalyzed steam explosion pretreatment process by impregnating the feedstocks with 1 % H 2

SO

4 (w/w, based on dry weight) and left to soak overnight. The impregnated raw material was then charged to a 60L pressurized steam explosion batch reactor at a temperature of about 200' C and a pH of about 2.9 for 7.5 min, so that an aqueous extract (or liquor) containing solubilized components of the lignocellulosic material was obtained (C5 rich). The remaining lignocellulosic material (e.g., fibrous material) was separated from the liquor or extract, and each was further processed as discussed infra. 75 WO 2013/120035 PCT/US2013/025457 [00191] Upon completion of pretreatment, the post-treated material, comprising about 12% to about 14% solids [wt/v], was subjected to a water washing step to separate solubilized C5 sugar from C6 sugars. The washing was performed in two steps; in the first step, the post treated feedstock was separated by centrifugation filter press which enables the separation of the solids from the liquid stream (the liquid stream being C5 rich, e.g., containing a high proportion of C5 sugars). The solid material was further suspended in water to recover additional C5 sugar that may have remained in the separated solids portion. On removing the soluble hemicellulose sugars, the remaining solids contained the cellulose or hexose rich C6 sugars. However, as a person of skill appreciates, no separation process is perfect and the solids portion may include some amount of C5 sugars, and the liquid stream may include some amount of C6 sugars. The liquid stream was then retained and maintained separate from the C6 stream. The separated solids were placed into a mixing tank. Once inside the mixing tank, the solids were adjusted to a pH of about 5 using 0.1 N NaOH. The solids wee then diluted to a dry solids content of about 8% solids. Enzymes (CELLIC CTech 2, Novozymes North America, Franklinton, NC) were added to the solid slurry at 2% loading (v/wt) based on the dry weight of the solids. [00192] Figure 1 is a sample sugar trajectory that illustrates how the biomass is converted from solids into liquefied stream of C6 sugars. Figure 1 was generated by collecting samples periodically for estimation (by HPLC) of cellulosic C6 sugars released by enzymatic hydrolysis of solids. Once enzymatic hydrolysis was complete, the liquid slurry is separated by centrifugation or microfiltration; or, alternatively, the solids can remain in the broth. For the experiments herein, the solids were separated from the broth using evaporation. Approximately 30 L of the resultant C6-rich liquid slurry was concentrated by simple evaporation at a temperature of from about 70'C to about 80'C until the sugar content of the sorghum or switchgrass hydrolysate was raised from about 5% to about 20% w/v. The resulting composition had a C6 sugar:C5 sugar ratio of about 90:10. [00193] Example 3. Preparation and Fermentation of Corn Mash Glucose Feedstock [00194] Mash was derived from industrial dry milling operations (Western New York Energy). Large debris were removed from the standard corn by hand, and small debris (<4 mm) were removed by passing through a No. 5 sieve before grinding using a Wiley mill fitted with a 2-mm screen. This produced particles of which 95% were smaller than 1.5 mm. The moisture content of the ground corn was 13.98 % (w/w, as received) and was used to 76 WO 2013/120035 PCT/US2013/025457 determine the mass of corn needed to prepare mash at a dry solids concentration of 25 % (w/w). [001951 A 0.13 g/ml working solution of the alpha amylase (Liquozyme SC DS, Novozymes) was added at a dose of 0.025 % (w/w) based on the wet weight of the corn in the slurry. The slurries were sealed and mixed at 50 rpm. Samples were liquefied by incubating at 83 0 C for 90 minutes, after which the samples were cooled to 400 and the mass of mash was calculated. The pH of the mash was adjusted to <5.2 by addition of 10 N sulfuric acid. The samples were shaken at 170 rpm at 32 0 C . Glucoamylase enzyme (starch breakdown process for corn mash) (Spirizyme@ Fuel, Novozymes) was prepared as a 0.25 g/mL solution and added at a dose of 0.66% (w/w, based on the wet weight of corn). Antibiotic, Lactrol (Philbro, Ridgefield Park, NH), was added to each flask to achieve a concentration of 0.5 ppm (w/w). The resulting corn mash had a 30% glucose concentration (wt/vol). [00196] A 0.1 g/ml suspension of yeast (Saccharomyces cerevisiae; Ethanol Red; Fermentis, Marcqen-Baroeul, France) was prepared in a sterile 250-ml flask and incubated at 40 'C for 20 minutes prior to inoculation into the fermentation containers containing saccharified corn mash feedstock. Nitrogen, as a 0.2 g/mL urea solution was added to a total concentration of nutrient nitrogen of 500 mg N/kg. The flasks were incubated at 32'C at 170 rpm for 60-120 hours. A dextrose fermentation was run as a control. [001971 Example 4. Blending of Cellulosic-Derived C6 Fermentable Sugars and Starch C6 [00198] Sugar compositions derived from ensiled energy sorghum and switch grass were prepared in accordance with Example 2. The cellulosic hydrolysate derived from sorghum and switchgrass comprise approximately 20% (wt/v) C6 sugars. Various blending ratios of corn mash (starch C6 with cellulosic C6) were prepared as follows: For every 100 ml of total whole fermentation broth, the amount of corn mash to cellulosic sugar C6 sugars was blended such that the final concentration of the sugars remained close to 20%. Thus, for the ratio of corn mash to sorghum of 90:10, 90 ml of 25% sugar slurry (wt/v) of corn mash was blended with 10 ml of cellulosic sorghum sugar slurry comprising 20% C6 sugars. In accordance with this protocol, several blends of corn mash and sorghum were prepared wherein the final C6 sugars were close to 20% (wt/v) and final volume of the broth was adjusted, resulting in four samples having a ratio of about 80:20, 70:30, 60:40 and 50:50 corn mash:C6 sugar. A similar process was followed to create fermentation feedstock, which was a blend of corn mash and switchgrass sugars. 77 WO 2013/120035 PCT/US2013/025457 [00199] Example 5. Ethanol Yield of Corn Mash blended with Cellulosic C6 sugars [00200] Prior to fermentation, the sorghum sugar streams were characterized for total solids, total dissolved solids and HPLC analysis of sugar content. The concentrations of total dry solids and dissolved dry solids were measured using standard fermentation procedures. The sugar substrate concentration was analyzed by HPLC for cellobiose, glucose, xylose, galactose, arabinose and mannose. The concentrations of sugar and ethanol were also determined during fermentation by HPLC. Ethanol conversion rate was determined by finding the theoretical maximum of ethanol to be produced by a sample (total glucose (g) x0.55 = total ethanol (g)). By using the HPLC, the resulting ethanol after fermentation was compared to the theoretical maximum of ethanol to be generated by the starting glucose level of the sample as fermentation began: (Resulting ethanol)/(Theoretical max Ethanol)= Ethanol Conversion rate. [00201] Table 1 and Figure 2 illustrate the approximate percent gain in ethanol yield over corn mash control in fermentation. The 80:20 corn mash blend with energy sorghum showed a 20.710% increase in ethanol conversion rate, the 70:30 corn mash blend with energy sorghum showed a 12.05% increase in ethanol conversion rate, the 60:40 corn mash blend with energy sorghum showed a 16.72% increase in ethanol conversion rate, and the 50:50 corn mash blend with energy sorghum showed a 11. 99% increase in ethanol conversion rate. [00202] Table 1 % Ethanol Improvement Recovered in Ethanol from Yield over Initial Ethanol Theoretical Corn Mash (g/L) sugar Yield Maximum control (%) 100% Corn Mash - Control 318.4 112.6 68.4 --- 80:20 Corn Mash with Energy 265.7 117.5 82.6 20.7 Sorghum 70:30 Corn Mash with Energy 259.7 108.2 76.7 12.0 Sorghum 60:40 Corn Mash with Energy 238.1 103.5 79.9 16.7 Sorghum 78 WO 2013/120035 PCT/US2013/025457 50:50 Corn Mash with Energy 256.9 107.5 76.6 12.0 Sorghum [00203] The results in Figures 3 and 4 demonstrate that corn mash fermented with energy-sorghum derived sugar compositions produce a higher efficiency of yeast sugar conversion to ethanol (approximately a 10-15% increase) as well as faster conversion of glucose sugars to ethanol (about 8 hours faster). Although the corn mash feedstock initially had more sugar than the corn mash and cellulosic sugar blends, all samples resulted in approximately the same final concentration of ethanol. Further, the fermentation of 100% corn mash took nearly ten hours longer to produce this final concentration. [00204] Switchgrass cellulosic sugar was blended with corn mash to produce 80:20 and 50:50 corn mash:switchgrass ratio samples. Table 2 and Figure 5 illustrate the percent gain in ethanol yield over the corn mash control during yeast fermentation. The 80:20 corn mash/switchgrass blend produced a 3.14% rise in ethanol conversion rate, and the 50:50 corn mash blend with switchgrass demonstrated a 6.95% rise in ethanol conversion rate. [002051 Table 2 Improvement in Ethanol % Ethanol Recovered Yield over Initial Ethanol from Theoretical Corn Mash (g/L) sugars Yield Maximum control (%) 100% Corn Mash Control 229.9 106.6 84.6 --- 80:20 Corn Mash with Switch Grass 224.3 106.2 87.3 3.1 50:50 Corn Mash with Switch Grass 219.3 108.5 90.5 7.0 [00206] Example 6. Impact of Sugar Compositions on Fermentation [002071 Three 20% glucose solutions were prepared for fermentation. The first was used as a control. The second was spiked with 5g Switchgrass dry solids. The third feedstock was spiked with 5g energy sorghum dry solids. The three feedstocks were adjusted to comprise similar total sugar concentrations (see Table 3) and fermented with yeast. The 79 WO 2013/120035 PCT/US2013/025457 Switchgrass and energy sorghum dry solids comprised the lignins, plant proteins and oils remaining after hydrolysis and removal of soluble C5 and C6 saccharides. The dry solids were filtered, washed, dried and weighed prior to mixing with the glucose. [00208] Table 3 % Ethanol Improvement in Recovered from Ethanol Yield over Initial Ethanol Theoretical Corn Mash control (g/L) sugar Yield Maximum (%) Glucose Control 196.3 84.4 78.2 --- Glucose with 5g Switchgrass Solids 191.6 96.8 91.9 17.5 Glucose with 5g Energy Sorghum Solids 208.09 109.26 85.1 8.9 [00209] The results shown in Figures 6 and 7 and Table 3 demonstrate that the addition of cellulosic C6 solids to the fermentation broth or growth media stimulate and enhance the conversion of a C6 glucose carbohydrate and/or cellulosic glucose sugar containing sources to ethanol. [00210] Not wishing to be bound by theory, it is believed that the level of nutrient rich ions present in the cellulosic hydrolysate stream enables the yeast to more efficiently and effectively consume glucose. Other mechanisms may also contribute to the observed beneficial effect: 1) appropriate levels of salt (ash) that alter membrane permeability or transport proteins, allowing more glucose into the cell and therefore more ethanol production; 2) appropriate (low) levels of inhibitors may reduce protons on the exterior of the mitochondria in the yeast cell, stimulating processes that seek to maintain the environmental conditions which impacts cell energy generation (these processes would enhance glucose metabolism resulting in higher ethanol production); 3) appropriate levels of trace ions and salts like Zn, Mg, and K in the feedstock increase the pH environment around and in the cell, stimulating enzyme activity resulting in increased ethanol production. [00211] Example 7: Preparation of Corn Stover used for Corn Mash Blending [00212] Corn stover was processed through a steam pretreatment system using only steam and no additional catalysts to prepare a C6-enriched hydrolysate. The pretreatment temperature was 205'C and the resident time was about 7.5 minutes. Excess C5 sugars and 80 WO 2013/120035 PCT/US2013/025457 acetic acid that were generated during pretreatment were solubilized and removed using a filter press. [00213] The stover was then added to a 55 gallon jacketed reactor and total solids were brought to about 8% (wt/wt) using water. The pH of the corn stover was adjusted to about 5.0 using sodium hydroxide. The 8% slurry of corn stover contained approximately 5 kg of dry biomass. To this, 1 L of enzymes were added to the broth. This represented approximately 4x the standard dosage (20% of total solids (v/wt)) in order to ensure complete hydrolysis. During enzymatic hydrolysis, the temperature was maintained at approximately 50' C for about 72 hours with agitation. The total weight of the corn stover plus water was approximately 62.5 kg. The slurry was then centrifuged following hydrolysis to remove all, or substantially all, of the remaining solids from the hydrolyzed sugars and the sugars were then concentrated through evaporation until the C6 sugar level reached about 300g/L. The sugar solution was sealed and kept at 4' C until fermentation. [00214] Example 8: Corn Mash Blending with Cellulosic Sugar derived from Corn Stover [002151 Corn mash oligosaccharides (e.g., starch) containing between about 25% and 30% sugars was blended with monomeric C6 sugar under various fermentation conditions. The monomeric sugars comprised either a solution of pure glucose or a C6-enriched hydrolysate produced from corn stover (e.g., cellulosic sugars) according to the procedure in Example 7. Both sources of monomeric sugars comprised about 25% sugars. The blended feedstocks were then simultaneously saccharified and fermented using a combination of enzymes and yeast. [00216] The corn mash control, undiluted, was saccharified and fermented as is. For the conditions with blended feedstocks, either 80 or 90 grams of corn mash material was weighed out and funneled into the appropriate flask. Following this step, 20 or 10 mL of either a ~25% sterile solution of glucose or ~25% corn stover hydrolysate was added to the corn mash and mixed. Fermentations comprising only pure glucose or the corn stover hydrolysate, had 1 mL of Yeast Nutrient Media added. 1 mL of 5% Urea and 5% Magnesium sulfate solution was added to all samples prior to fermentation, and the pH of each solution was adjusted to 4.8 - 5.2. [002171 Yeast, propagated beforehand to exponential growth phase, was added to each sample. For each corn mash sample, 50 gL of glucoamylase was added at the same time to initiate the simultaneous saccharification of the corn mash and the yeast fermentation. 81 WO 2013/120035 PCT/US2013/025457 Samples of the fermentation were analyzed at 2.5, 5, 24, and 96 hours for glucose and ethanol. The results are summarized in Table 4. [00218] Control fermentations were carried out with pure glucose solution or the C6 enriched corn stover hydrolysate. The concentration of sugars in the fermentation reactions was approximately 20%. The glucose and the C6 hydrolysate produced similar yields of ethanol. The pure glucose fermentation produced an ethanol titer of 105.54 g/L after 96 hours; the C6-enriched hydrolysate fermentation reaction produced an ethanol titer of 104.03 g/L after 96 hours. This experiment shows that the C6-enriched hydrolysate yields are similar to a pure glucose solution. [00219] Table 4: Summary of fermentation data Time 0 2.5 5 24 96 (hrs) Glucose Glucose 192.9 162.1 130 61.54 0 Control (20%) Ethanol 0 7.98 22.94 72.15 105.54 (g/L) Glucose 191.9 196 187.8 47.43 2.97 Corn Stover (gIL) Hydrolysate (20% C6) Ethanol 0 1.98 8.5 71.33 104.03 (g/L) Glucose 12.7 107.8 151.28 54.91 15.74 SSF Corn (g/L) Mash Control Ethanol 0 10.4 33.15 109.87 142.33 (g/L) SSF Corn Glucose 65.9 125.8 151.49 47 4.32 Mash:Glucose (80:20) Ethanol 0 8.4 32.35 112.82 153.85 (g/L) SSF Corn Glucose 70.1 130.3 131.35 55.04 19.93 Mash:Corn (g/L) Stover Hydrolysate Ethanol 0 9.1 31.23 114.11 137.79 (80:20) (g/L) Glucose 28.1 132.3 153.22 45.76 8.65 SSF Corn (gIL) Mash:Glucose (90:10) Ethanol 0 9.6 32.88 117.46 153 (g/L) 82 WO 2013/120035 PCT/US2013/025457 SSF Corn Glucose 41 118 122.82 48.33 14.87 Mash:Corn (g/L) Stover Hydrolysate Ethanol 0 12 33.37 112.53 150.71 (90:10) (g/L) [00220] Example 9. Fed Batch fermentation using Blended Cellulosic-derived and non-Cellulosic Sugars [00221] Using varying proportions of cellulosic-derived C6 stream, the average ethanol yield of liquefied corn mash was compared to the average ethanol yield of a control containing only water and corn solids. Also, a glucose solution instead of a C6 rich stream was also used as a term of comparison for concentration of products, given the high sugar concentration of the amendments. Fed-batch strategy was also examined to evaluate the performance of the yeast when a C6 sugar rich stream was fed into the fermenter as controlled additions during SSF operations. [00222] Most dry milling operations in the U.S. follow a particular series of steps. They mill the corn, adjust the solids and starch content, cook the corn mash with alpha amylase and, finally, to gain efficiency, carry out SSF with the addition of glucoamylase (GA) and a fermenting yeast in a single vessel. The success of this operation can be determined and driven by several factors such as the starch content in the mash leading to total fermentable sugars (e.g., the higher the sugar content, the higher the amount of ethanol produced); the kind of yeast used (sugar, ethanol and temperature tolerant); the inoculum level of the yeast and fermentation time; the residual sugars at the end of fermentation (most corn ethanol plants prefer to maximize sugar utilization and minimize the presence of residual sugars as it impacts the quality of DDGS on distillation); temperature; the control of the release and presence of monomeric C6 sugars and salts during fermentation; the level of fermentation inhibitors formed (e.g., acetic acid, lactic acid, formic acid, HMF, furfural and lignin produced); the presence of C5 sugars and their concentration in the mash (e.g., xylose can interfere with fermentation as most fermenting yeasts are unable to assimilate this sugar; in this case, addition of a C5 fermenting yeast can be used to achieve complete sugar conversion). [00223] To gain efficiency and lower capital expenditures, most corn dry milling operation currently average about 48 hours of fermentation. A limiting factor, affecting the finishing time, can be the rate of the glucoamylase (GA) addition and the conversion of 83 WO 2013/120035 PCT/US2013/025457 dextrin's to monomeric C6 sugars. Most operators try to keep glucose levels at about 1% or less at just after 18 hours of fermentation because the glucoamylase is expensive, so it is necessary to be as efficient as possible. [00224] Further, in most of these operations, glucose levels are kept low to reduce osmotic stress on the yeast, especially past 18 -24 hours of fermentation when other stressors may begin to impact the yeast (e.g., ethanol, lactic acid, acetic acid, etc.). Dosing GA at a higher concentration typically results 3-5% glucose at 24 hours; however by reducing the GA, a reduction in the glycerol production (presumably from less osmotic stress) is noticed. To achieve optimum availability of monomeric C6 glucose without compromising osmotic stress effects during corn mash fermentation with yeast, a fed-batch operation was carried out wherein cellulosic derived C6 sugar was controlled and 'spoon fed' or fed continuously to the corn mash to insure no excess build up of monomeric C6 sugars in the mash. This strategy enabled the microorganism to get optimum feeding-on-demand monomeric C6 sugar, steering the yeast metabolic pathway away from glycerol while enabling rapid conversion to ethanol. [002251 Corn mash slurry was prepared for the different fermentation treatments (e.g., corn mash only and blended with cellulosic-derived C6 monosaccharides). Briefly, the moisture content of the corn was used to determine the mass of corn needed to prepare mash at a dry-solids concentration of 25 % (w/w). The alpha-amylase enzyme (Liquozyme SC DS, Novozymes, U.S.A.) was diluted to ensure more precise delivery of enzyme to each sample. A 0. 13-g/ml working solution of the alpha amylase was added at a dose of 0.025 % (w/w) based on the wet weight of the corn. The pH was adjusted to 5.7 - 5.85 using IN ammonium hydroxide and the samples agitated while incubating at 830 C for 90 minutes. Following liquidation of the samples, they were cooled to 400 C. [00226] Prior to fermentation, the cellulosic C6 rich stream derived from various feedstocks (e.g., corn stover, wheat straw, energy sorghum, switchgrass, etc.) was prepared using pretreatment procedures that maximize recovery of fermentable saccharides. The fermentations were performed with crude hydrolysates that were characterized for total solids, total dissolved solids and HPLC analysis of sugar content. The concentrations of total dry solids and dissolved dry solids were measured using standard NREL procedures. The sugar substrate concentration was analyzed by HPLC for C5 sugars and glucose as C6. [002271 Characterization of a C6 rich stream [00228] A C6 rich stream was prepared from processing corn stover that was pretreated in a commercial Biogasol unit capable of processing 100MT dry biomass per 84 WO 2013/120035 PCT/US2013/025457 day with dilute H 2

SO

4 (15 minutes at 1700 C with 0.6%, H 2

SO

4 ). The C5 sugars were separated and the C6 /lignin rich solids were enzyme hydrolyzed with Novozyme Cellic Ctec3 cellulase enzymes. Post hydrolysis, the lignin was separated and the C6 rich stream with a residual amount of C5 was further concentrated to 25% solubilized solids. [00229] The contents of the cellulose hydrolysis stream (C6 rich stream) is shown in Table 5 below. [002301 Table 5: Characterization of cellulosic C6 stream pH Dissolved Acetic acid HMF C5 as Glucose solids % % Xylose (%w/v) (%w/w) (%w/v) 5.0 25.44 0 0 2.5 23.48 [00231] The mass of the cooled mash was calculated for each sample. The pH of the mash was adjusted to <5.2 by addition of 1-N sulfuric acid. [00232] All enzymes, nutrients, and other amendments added to the fermentation flasks were freshly prepared before use. The total concentration of nutrient nitrogen as urea was 500 mg N/kg to a final concentration of 500 ppm as nitrogen (w/w, based on the total mass of mash). The glucoamylase enzyme (Spirizyme Fuel, Novozymes) was prepared as a 0.25 g/ml solution and added at a dose of 0.066% (w/w, based on the wet weight of corn). Antibiotic, FermGuard Xtreme (Ferm Solutions, Inc, Danville, KY), was added to each sample as a dose of 0.5 ppm (w/w). Yeast extract (0.16 g) was added to the glucose treatment that fermented with no corn solids. [00233] A 0.1 g/ml suspension of yeast (Saccharomyces cerevisiae; FermaxGreen and FermaxGold Ethanol Red; Fermentis, Marcq-en-Baroeul, France) was prepared in a sterile IL flask having the corn mash with glucoamylase. This suspension was incubated and mixed for 6 hours at 340 C prior to inoculation of a 6.5% volume of the suspension into a sample. [00234] The mass of each sample was recorded after all additions were made, and the samples were incubated at 320 C with agitation for 62 hours. [002351 Table 6: Summary design of cellulosic-C6 rich stream to water ratio per treatment for determination of effects on ethanol yield 85 WO 2013/120035 PCT/US2013/025457 TREATMENT TYPE OF SOLUTION SOLUTION: CORN MASH SLURRY RATIO 10% Cellulosic-C6 rich 10:90 20% Cellulosic-C6 rich. 20:80 Glucose Control Glucose, 250 g/L:O Fed batch Cellulosic-C6 rich (46% 10:90 10 L C6 solution) 1 L fed to 9 L corn mash [002361 Samples were collected at various time intervals and the combined mass of the mash and sample was measured. The samples were analyzed for concentrations of substrates (glucose, subunits, residual xylose) and products (ethanol, glycerol, lactic acid, and acetic acid) by HPLC. The remaining samples were collected at the end of fermentation and analyzed for pH and substrate/product concentrations. The final concentrations of total dry solids and dissolved dry solids were measured after incubation for 62 hours [00237] Fed batch operation [002381 Partially dextrinized corn mash was charged in a 30 L C-30 Sartorius stainless steel Steam In Place (SIP) bioreactor, pH adjusted to 5 with 1 N KOH and the temperature maintained at 320 C. The yeast was propagated separately. Glucoamylase enzyme (Spirizyme Fuel, Novozymes) was prepared as a 0.25 g/ml solution and added at a dose of 0.066% (w/w, based on the wet weight of corn). Antibiotic, FermGuard Xtreme, was added to each tank to achieve a dose of 0.5 ppm (w/w). [00239] The yeast inoculum was prepared by adding 0.15 g of dried matrix green and matrix gold yeast to the corn mash, at pH 5 with KOH and propagated for 6 hr. Seed was inoculated into the fermenter at 6.5% v/w (T=0 hr). The fermenter operating parameters were as follows: temperature 340 C, RPM = 300, feed rate of cellulosic derived C6 rich stream (1 L of 48% w/v sugar as C6 and 4.3% w/v C5 as xylan) was fed continuously and controlled at a feed rate of 0.7 ml/min. During the first 24 -36 h of the operation, IL of the C6 rich solution was drained into the fermenter. Samples were drawn at time intervals and analyzed for residual sugars and progress of ethanol fermentations. In some samples, an engineered yeast that was capable of fermenting C6 glucose and C5 sugar (xylose) was used. The intent was to test and see if mixed cultures of C6 and an engineered C5 fermenting yeast assist in successful fermentation of sugar mixtures of glucose and xylose in the corn mash. 86 WO 2013/120035 PCT/US2013/025457 [00240] Fed batch operation in 2 L (seed propagator) and 30 L automaticfermenters (Sartorius, PA) [00241] Table 7 Sample HPLC DROP RESULTS (w/v) except Ethanol (v/v) T Tot. Lact. Ac. h S DP4S DP3S DP2S Glu Fruc. Acid Glyc. Acid EtOH Cont. 1 48 2.26 1.33 0.47 0.25 0.17 0.04 0.16 1.75 0.03 15.71 Cont. 2 48 2.54 1.52 0.48 0.26 0.24 0.04 0.21 1.75 0.02 15.44 Cont. 3 48 1.96 1.04 0.46 0.23 0.19 0.04 0.18 1.77 0.03 15.7 Test 4 (90:10) 48 2.88 1.15 0.71 0.36 0.25 0.41 0.15 1.45 0.03 16.32 Test 5 (90:10) 48 2.66 1 0.68 0.39 0.17 0.42 0.15 1.45 0.03 16.35 Test 6 (90:10) 48 2.69 1.03 0.69 0.36 0.2 0.41 0.13 1.43 0.04 16.2 Test 1 (80:20) 48 3.24 1.08 0.76 0.5 0.12 0.78 0.15 1.26 0.05 16.84 Test 2 (80:20) 48 3.27 1.1 0.76 0.49 0.14 0.78 0.15 1.25 0.04 16.71 Test 3 (80:20) 48 3.3 1.08 0.77 0.5 0.16 0.79 0.16 1.27 0.05 16.89 Cont.: Control (corn mash only); T (h): Time in hours; Tot. Sug.: Total Sugars; DP4S: saccharides with 4 degrees of polymerization; DP3S: saccharides with 3 degrees of polymerization; DP2S: saccharides with 2 degrees of polymerization; Glu.: Glucose; Fruc.: Fructose; Lact. Acid: Lactic Acid; Glyc.: Glycerol; Ac. Acid: Acetic Acid; EtOH: Ethanol. [00242] As shown in Table 7, fed-batch fermentations blending corn mash with cellulosic-derived C6 monosaccharides resulted in higher yields of ethanol and lower yields of glycerol after 48 hours as compared to control fermentations of corn mash only. [00243] Fed batch fermentations of cellulosic C6 rich sugar from wheat straw (WS) blended with corn mash at an 90:10 or 80:20 ratio (corn mash : wheat straw) were performed in an automated 30L system. The results of the fermentation were compared to control batch process fermentations of blended feedstocks at the same ratio. All fermentations were inoculated with three strains of industrial C6 fermenting yeasts and one genetically engineered yeast that can ferment both C5 and C6 sugars. The results are shown in Table 8 and Figures 10 and 11. 87 WO 2013/120035 PCT/US2013/025457 [00244] Table 8. Fed-batch vs. batch fermentation. Formic Acetic Glucose Xylose Acid Acid Ethanol Treatment (g/L) (g/L) (g/L) (g/L) (g/L) Corn Mash (CM) TO 21.15 4.55 0.4 3.54 3.35 30 L fed batch 90:10 CM:WS T5 172.9 1.55 0.3 8.17 22.8 30 L fed batch 90:10 CM:WS T18 36.65 3.1 0.6 17.82 99.1 30 L fed batch 90:10 CM:WS T36 10.55 5.7 0.85 16.76 124.2 30 L fed batch 90:10 CM:WS T48 3.65 6.4 0.9 18.97 143.85 Control Batch Process 90:10 TO 53.7 4.4 0.4 3.29 1.8 Control Batch Process 90:10 T5 146.65 0.75 0.25 3.06 3 Control Batch Process 90:10 T 18 110.3 3.3 0.45 10.88 51.35 Control Batch Process 90:10 T36 2.15 0.85 0.5 11.92 105.15 Control Batch Process 90:10 T48 2.9 4.65 0.65 13.58 118.25 [002451 The fed batch runs indicated initial significant improvement in ethanol volume productivity in g/l/h. Combining cellulosic derived C6 sugar with corn mash as a fed batch process produces higher ethanol production in a shorter amount of time over the first portion of the fermentation in the 30L and flask samples. The fed batch process not only has shown an increase in ethanol production compared to corn mash on its own, it has also shown to be superior to batch process where all of the cellulosic sugar in the blend is added initially in fermentation. Further optimization with the mixed culture of C6 and C5 fermenting yeast in the 30L reactor resulted in higher ethanol titers (25%) and reduced the amount of residual sugar in solution, especially in the remaining C5 portion. [00246] Figure 8 shows that by feeding a higher concentration of cellulosic sugar over time, higher ethanol production can be achieved when cellulosic sugar is blended with corn mash after 48 hours and in a shorter amount of time. Residual sugar in both fermentations was under 0.13% v/v. The C5 portion of solution remained mostly unfermented due to the lack of C5 fermenting microbe. [002471 Figure 9 shows the amount of ethanol produced in a 90:10 blend of corn mash and cellulosic sugar at the shake flask level vs. the ethanol production in standard corn mash from as is, at an industrial size scale. The addition of cellulosic sugar throughout the 88 WO 2013/120035 PCT/US2013/025457 fermentation can account for the increase in ethanol production at the beginning of the fermentation. [00248] Figure 10 illustrates the results of fed batch replacement of 10% of the corn mash with 10% concentrated cellulosic sugar solution (52% total C5 and C6 sugar). There was an increase of 4

.

7 5 % v/v ethanol by this method than with corn mash without any blending. The standard yeast combined with a C5 and C6 fermenting yeast strain led to a higher ethanol yield. [00249] Figure 11 shows the percent increase in ethanol production between the 90:10 and 80:20 blended flasks of corn mash with cellulosic sugar derived from wheat straw. The 90:10 fed batch run had a 24.63% increase in ethanol production compared to the batch run in a 90:10 ratio. The 80:20 fed batch blend also saw positive improvement, yielding 12% of an ethanol increase compared to the batch run in the same blend. [002501 Example 10 [002511 Summary [00252] In this example, different proportions of a corn stillage hydrolyzate containing starch-derived C6 saccharides (C6 Saccharide Stream) was added (dosed) to corn mash in fermentation reactions. Fermentation reaction progress was measured by mass loss, ethanol concentration, and ethanol yield. The data show statistically significant increases in mass loss, ethanol concentrations and yield for doses above 10% C6 Saccharide Stream. For the higher doses, the total residual sugars concentration may indicate an incomplete fermentation. [002531 Objective [00254] An objective of this example is to determine how different proportions of a C6 Saccharide Stream added to corn mash affect the ethanol yield. The average ethanol yield in flask fermentations of liquefied corn mash, prepared using different proportions of C6 Saccharide Stream, was compared to the average ethanol yield of a quality control (QC) treatment, containing only water and corn solids. A glucose control, utilizing a glucose solution instead of water or C6 Saccharide Stream was also used as a term of comparison for concentration of products, given the high sugars concentration of the amendments. [002551 Preparation of C6 Saccharide Stream [002561 Hot water at about 190 'F was added to corn stillage material until the total solids level was about 12%. The mixture was continuously agitated at about 185 'F for about 90 min, then the pH was adjusted to about 5.8 with sodium hydroxide. The corn stillage material was treated with alpha amylase amylase enzymes and glucoamylase enzymes. Solids 89 WO 2013/120035 PCT/US2013/025457 were sequestered by filter press and the liquid fraction was concentrated to about 25% glucose (w/v) by evaporation. [002571 Preparation of Corn Mash [00258] Mashes were prepared for ten different fermentation treatments shown in Table 9. Large debris were removed from the corn by hand, and small debris (<4 mm) were removed by passing through a No. 5 sieve (Fisher Scientific Company) before grinding using a Wiley mill (Thomas Scientific, NJ) fitted with a 2-mm screen. This produces flour for which 95 % of the particles are smaller than 1.5 mm. [002591 Table 9. Summary of experimental conditions. treatment ID type of solution solution:water ratio in mash 5% C6 Saccharide Stream 5:95 10% C6 Saccharide Stream 10:90 20% C6 Saccharide Stream 20:80 30% C6 Saccharide Stream 30:70 40% C6 Saccharide Stream 40:60 47.5% C6 Saccharide Stream 47.5:52.5 50% C6 Saccharide Stream 50:50 QC/0% QC 0:100 glucose control glucose, 250 g/L:0 [00260] The moisture of the ground corn was determined gravimetrically by drying a subsample of the flour in a forced-air oven at 105 'C for 3 hours. The moisture content for corn used the first week was 14.04 % (w/w, as received) and for week two it was 14.35 % (w/w, as received). The moisture content of the corn was used to determine the mass of corn needed to prepare 160 g of mash at a dry-solids concentration of 25 % (w/w). [00261] The mass of corn, total deionized (DI) water added, and enzyme needed to prepare 160 g of corn slurry at a total dry solids concentration of 25 % (w/w) for each replicate was determined using a mash calculator. For each treatment, nine independent replicate slurries were prepared. The required amount of DI water was transferred into labeled Labomat beakers, followed by addition of the required mass of corn flour. The alpha amylase enzyme (Liquozyme SC DS, Novozymes) was diluted to ensure more precise delivery of enzyme to each flask. A 0.13 g/mL working solution of the alpha amylase was 90 WO 2013/120035 PCT/US2013/025457 used and added at a dose of 0.025 % (w/w) based on the wet weight of the corn. The slurries were hand swirled after all components were in the Labomat beakers. The pH was adjusted to 5.7 - 5.85 using 6N ammonium hydroxide. Sealed beakers were attached to a vertically mounted wheel in the Labomat (Model BFL12 805, Mathis, Switzerland), which rotated at 50 rpm during the incubation. The wheel was programmed to reverse direction every 50 seconds to improve the mixing efficiency. Samples were liquefied by incubating at 83 0 C for 90 minutes, after which the samples were cooled to 40 0 C in the Labomat. Prior to fermentation, the C6 Saccharide Stream was characterized for total solids, total dissolved solids and HPLC analysis of sugar content. The concentrations of total dry solids and dissolved dry solids were measured using standard procedures. The sugar substrate concentration was analyzed with HPLC for oligosaccharides having a degree of polymerization of four or more (DP4+), three (DP3), two (DP2), and one (glucose). [00262] Once the mash was cooled, the entire contents (approximately 160 g) of each Labomat beaker were transferred to a sterile 250-ml Erlenmeyer flask. The masses of the mash and flasks were recorded, and the mass of mash transferred to the fermentation flasks was calculated. The pH of the mash was adjusted to <5.2 by addition of 150 gl of 10-N sulfuric acid. The flasks were shaken at 170 rpm on an incubator/shaker (Sartorius, Certomat BS-1) at 32 0 C until preparation of all mashes was complete. [002631 All enzymes, nutrients, and other amendments added to the fermentation flasks were freshly prepared before use. The total concentration of nutrient nitrogen was 500 mg N/kg, urea was added as a sterile 0.2 g/ml solution to a final concentration of 500 ppm as nitrogen (w/w, based on the total mass of mash). The glucoamylase enzyme (Spirizyme Fuel, Novozymes) was prepared as a 0.25-g/nL solution and added at a dose of 0.066% (w/w, based on the wet weight of corn). Antibiotic, Lactrol (Phibro, Ridgefield Park, NJ), was added to each flask to achieve a dose of 0.5 ppm (w/w). Yeast extract (0.16 g) was added to the glucose treatment which fermented with no corn solids. [00264] A 0. 1-g/mL suspension of yeast (Saccharomyces cerevisiae; Ethanol Red; Fermentis, Marcq-en-Baroeul, France) was prepared in a sterile 250-ml flask. This suspension was incubated and mixed for 20 minutes at 40 'C before inoculation into the fermentation flasks. Each fermentation flask was inoculated with 160 gl of the yeast suspension to attain an initial concentration of 1 x 10 7 yeast cells/mL. [002651 The mass of each flask was recorded after all additions were made, and the sanitized fermentation traps were reinserted into each flask. The flasks were incubated at 32 'C with shaking at 170 rpm in an incubator/shaker (Sartorius, Certomat BS-1) for 62 hours. 91 WO 2013/120035 PCT/US2013/025457 [002661 Samples were collected at 22, 46 and 62 hours. Mass measurements were taken twice a day; the combined mass of the mash and flask was measured for each flask with the traps in place. One-third of the experimental flasks were taken sacrificially at 22 hours and another third harvested at 46 hours, flask material at both of these sample time points were analyzed for pH and the concentrations of substrates (glucose, DP2, DP3, and DP4+, where "DPx" represent glucose oligomers with "x" subunits) and products (ethanol, glycerol, lactic acid, and acetic acid) using HPLC. The remaining flasks were collected at the end of fermentation and analyzed for pH and substrate/product concentrations. Samples were prepared for HPLC by centrifugation to remove large solids, followed by filtration through 0.45 gm syringe filters, and acidification to pH of approximately 2 by addition of sulfuric acid to a final concentration of 0.01 N. The final concentrations of total dry solids and dissolved dry solids were measured after incubation for 62 hours, and the density of the beer filtrate was measured by densitometer (Anton Paar DMA 4500, Anton-Paar GmbH, Graz, Austria). [002671 Results [00268] Characterization of C6 Saccharide Stream [00269] The average composition of four samples of the C6 Saccharide Stream is shown in Table 10. The original pH of the individual samples were: 1.319, 1.17, 1.39, and 1.195. [002701 Table 10. Characterization of C6 Saccharide Stream Average total dissolved pH DP4+ DP3 DP2 Glucose solids solids (4 (%w/w) (%w/w) (%w/v) (%w/v) (%w/v) (%w/v) samples) 1.27 25.08 24.44 6.36 1.51 1.75 21.48 [002711 Reaction Progress (Mass Loss) [00272] Fermentation progress curves are shown in Figure 12 (A&B) and the average mass losses for all treatments at all time points are shown in Table 11. The cumulative mass losses after incubation for 15.67 and 62 hrs are shown in Figure 13. Significant differences in the average reaction progress after 15.67 and 62 hours were identified among the eight treatments using one-way ANOVA at the 95% confidence level. Further analysis by Dunnett's test against the QC shows that at 15.67 hours all treatments were different than the 92 WO 2013/120035 PCT/US2013/025457 QC; the treatments with 5%, 10%, 20%, and 30% C6 Saccharide Stream lost more mass than the QC, while treatments with 40%, 47.5%, and 50% SWE A and the glucose treatment lost less mass than the QC. Further analysis by Dunnett's test shows that at 62 hours the treatments with 5% and 10% of C6 Saccharide Stream were the only two treatments which had statistically identical mass loss to the QC sample. At 62 hours, Tukey's test for paired comparisons shows that the glucose treatment is lower than all other treatments, the break down for mass loss at the end of fermentation is as follows: {5% = 10% = QC} < 20% < {30% = 40% = 47.5% = 50%} [002731 Table 11. Average mass loss in grams during fermentation [00274] fermentation time (hours) treatmen 15.67 22 39 46 62 t 5% 6.82 10.91 13.21 13.72 14.35 10% 6.97 10.90 13.16 13.70 14.52 20% 6.41 11.60 14.49 14.95 15.73 30% 5.75 11.08 15.42 15.94 16.97 40% 3.91 9.40 15.73 16.51 17.69 47.5% 3.26 8.30 15.26 16.14 17.00 50% 3.04 7.85 15.08 16.02 17.28 QC 5.20 10.05 13.24 13.64 14.23 Glucose 0.27 0.46 1.30 1.68 2.56 [002751 The fermentation progress was slower in the glucose control, although that the solution was supplemented with yeast nutrients. The data for the glucose control is reported in Tables 13-16. [00276] Final Concentrations of Residual Sugars and Fermentation Products [002771 Final concentrations of total dissolved sugars (Table 12, Figure 14) were less than 2% (w/v, expressed as glucose equivalents) for treatments QC and C6 Saccharide Stream at 5%, 10%, 20%, and 3 0%; the other treatments dosed with C6 Saccharide Stream at 40%, 45.7%, and 50% had less than 4% (w/v); the glucose treatment had 21.13% (w/v). A concentration of total residual sugars less than 2% is expected for complete fermentations of corn mash. Significant differences among the final total dissolved sugars concentrations among the eight treatments were identified using one-way ANOVA at the 95% confidence 93 WO 2013/120035 PCT/US2013/025457 level. Further analysis by Dunnett's test revealed the C6 Saccharide Stream treatments in proportions of 30%, 40%, 47.5%, and 50% had statistically higher residual sugars concentrations compared to the QC. For treatments that contained the C6 Saccharide Stream, Tukey's test was used to identify statistically equivalent pairs; two groups were found to have statistically the same final total residual sugars concentrations: 5%, 10%, 20%, and 30% was one group and 40% 47.5%, and 50% the other. [00278] Table 12. Average final concentrations and standard deviations of residual sugars, glycerol, ethanol, and final yield Treatment Residual sugars* Glycerol Ethanol Yield (%, w/v) (%, w/v) (%, w/v) (g/g) 5% 0.586 ± 0.010 1.087 ± 0.024 10.426 ± 0.069 0.350 + 0.004 10% 1.001 +0.014 1.188 0.002 10.562 0.111 0.355 + 0.004 20% 1.243 0.002 1.181 0.003 11.613 0.112 0.387 + 0.001 30% 1.814 0.014 1.174 0.011 12.630 0.071 0.417 + 0.004 40% 3.061 ± 0.995 1.257 ± 0.112 13.063 ± 0.150 0.430 + 0.003 47.5% 3.801 ± 1.544 1.325 ± 0.136 12.718 ± 0.326 0.414 + 0.013 50% 3.141 0.154 1.292 0.044 12.888 0.411 0.421 + 0.015 QC 0.294 ± 0.011 0.862 ± 0.009 10.288 ± 0.061 0.350 + 0.003 *concentrations expressed as glucose equivalents [002791 Total glycerol concentrations were also analyzed, as they can be a reflection of osmotic or other stress during fermentation. Yeast stress can affect ethanol production adversely. All treatments receiving the C6 Saccharide Stream had higher final glycerol concentrations than the QC; significant differences were identified using one-way ANOVA and by Dunnett's test against the control (QC). Figure 15 shows the glycerol concentration as a function of dose. [00280] Significant differences among the final ethanol concentrations among the eight treatments were identified using ANOVA. Further analysis by Tukey's test for paired differences identified the data could be sorted into two groups; 50%, 10%, and QC are statistically the same as one another and lower than the group of 20%, 30%, 40%, 45.7% and 50%, which are statistically the same as one another (Figure 14). [00281] The average pH for each treatment throughout fermentation is shown in Figure 16. No correlations based on dose were identified when pairing residual sugars, glycerol, and ethanol concentrations with pH. 94 WO 2013/120035 PCT/US2013/025457 [00282] Ethanol Yield [00283] The ethanol yield showed significant differences among the treatments by one way ANOVA at the 95% confidence level; Dunnett's test against QC shows that only treatments with 5% and 10% SWE A were statistically the same as the control, although in a dose-response plot, the 10% treatment also trends higher than control. Of the treated mashes, C6 Saccharide Stream at 40% had the highest yield overall, but this treatment had statistically the same yield as 30%, 47.5%, and 50%, as analyzed by Tukey's test for paired differences. The normalized dose response graph (Figure 17) shows that overall the mashes treated with 20% or higher C6 Saccharide Stream produced a statistically higher amount of ethanol than the control. In this graph, the y-axis represents the amount in excess of 100% of ethanol yield, compared to the QC samples which are noted as 0% in Figure 17. [00284] Table 13 shows the final product yields and residual sugar levels for each of the replicate samples in the treatment categories. Table 14 shows the final product yields and residual sugar levels averaged over all replicate samples in the treatment categories. Table 15 shows the mass loss at 15.67, 22, 39, 46, and 62 hours of fermentation for each of the replicates within the treatment conditions. Table 16 shows the pH for each of three replicates within each treatment condition at 22, 46, and 62 hours of fermentation. [002851 Table 13. Final substrate and product concentrations substrates (g/100 ml) Total products (g/100 ml) sugars* Treatmen (g gluc. t eq./100 Lactic acetic ID DP4+ DP3 DP2 glucose ml) acid glycerol acid ethanol 0.342 0.049 0.128 0.012 0.574 0.109 1.100 0.003 10.456 5% 0.359 0.047 0.129 0.013 0.594 0.109 1.103 0.004 10.475 0.353 0.052 0.127 0.013 0.590 0.101 1.060 0.004 10.347 0.642 0.066 0.171 0.032 0.988 0.134 1.187 0.006 10.610 10o 0.662 0.056 0.183 0.036 1.016 0.138 1.190 0.009 10.435 0.641 0.060 0.183 0.037 0.999 0.135 1.186 0.008 10.641 0.850 0.069 0.180 0.047 1.244 0.177 1.178 0.010 11.484 20% 0.846 0.072 0.176 0.048 1.241 0.177 1.182 0.012 11.678 0.846 0.072 0.179 0.049 1.244 0.178 1.183 0.011 11.677 30% 1.262 0.103 0.229 0.090 1.828 0.192 1.187 0.050 12.665 95 WO 2013/120035 PCT/US2013/025457 1.253 0.103 0.226 0.089 1.814 0.195 1.167 0.046 12.548 1.242 0.100 0.226 0.089 1.800 0.194 1.169 0.048 12.677 1.762 0.114 0.293 0.136 2.504 0.218 1.198 0.062 13.063 40% 2.827 0.261 0.382 0.420 4.210 0.262 1.386 0.108 13.214 1.727 0.123 0.286 0.138 2.469 0.223 1.187 0.061 12.913 3.484 0.357 0.448 0.894 5.578 0.303 1.480 0.136 12.783 47.50 2.100 0.156 0.323 0.224 3.040 0.240 1.270 0.081 13.008 1.955 0.150 0.303 0.156 2.785 0.252 1.226 0.078 12.365 2.188 0.171 0.331 0.253 3.191 0.250 1.309 0.090 13.021 5000 2.087 0.163 0.309 0.175 2.969 0.259 1.243 0.084 12.427 2.221 0.167 0.347 0.279 3.264 0.254 1.326 0.092 13.218 QC 0.126 0.044 0.098 0.008 0.298 0.077 0.858 0.000 10.319 0.132 0.043 0.098 0.009 0.304 0.075 0.853 0.000 10.316 0.125 0.044 0.094 0.009 0.292 0.078 0.855 0.000 10.244 0.131 0.039 0.091 0.000 0.281 0.068 0.876 0.001 10.380 0.130 0.038 0.093 0.000 0.282 0.064 0.872 0.001 10.258 0.129 0.051 0.104 0.000 0.306 0.068 0.858 0.001 10.214 0.050 0.038 0.167 20.184 20.456 0.023 0.319 0.064 1.680 glucose 0.050 0.038 0.166 21.664 21.934 0.023 0.322 0.067 1.680 0.050 0.038 0.166 20.730 21.000 0.023 0.314 0.063 1.655 values in bold are below detection limits *total sugars = XDP4+*CDP4+ + XDP3*CDP3 + XDP2*CDP2 + Cglucose where: XDP4+ = 1.111 g glucose equivalents/g DP4+ XDP3 = 1.07 g glucose equivalents/g DP3 XDP2 = 1.05 g glucose equivalents/g DP2 Ci = concentration of compound "i" [00286] Table 14. Summary of average final substrate and product concentrations Substrates (g/100 ml) Total Products (g/100 ml) sugars* (g gluc. Treat. glucos eq./100 lactic glycer acetic ethano ID DP4+ DP3 DP2 e ml) acid ol acid 1 500 0.351 0.049 0.128 0.013 0.586 0.106 1.087 0.004 10.426 96 WO 2013/120035 PCT/US2013/025457 0.009 0.002 0.001 0.001 0.01 0.005 0.024 0.0004 0.069 0.648 0.061 0.179 0.035 1.001 0.135 1.188 0.008 10.562 10% 0.012 0.005 0.007 0.003 0.014 0.002 0.002 0.002 0.111 0.847 0.071 0.178 0.048 1.243 0.177 1.181 0.011 11.613 20% 0.002 0.002 0.002 0.001 0.002 0.001 0.003 0.001 0.112 1.252 0.102 0.227 0.089 1.814 0.194 1.174 0.048 12.63 30% 0.01 0.002 0.001 0.001 0.014 0.001 0.011 0.002 0.071 2.105 0.166 0.32 0.231 3.061 0.234 1.257 0.077 13.063 40% 0.625 0.083 0.053 0.163 0.995 0.024 0.112 0.027 0.15 2.513 0.221 0.358 0.425 3.801 0.265 1.325 0.098 12.718 47.5% 0.844 0.118 0.079 0.407 1.544 0.034 0.136 0.032 0.326 2.165 0.167 0.329 0.236 3.141 0.254 1.292 0.088 12.888 50% 0.07 0.004 0.019 0.054 0.154 0.005 0.044 0.004 0.411 0.129 0.043 0.097 0.004 0.294 0.072 0.862 0.001 10.288 QC 0.003 0.005 0.005 0.005 0.011 0.006 0.009 0.001 0.061 0.05 t 0.038 0.166 20.86 21.13 0.023 0.319 0.065 1.671 glucose 0.000 1 0.0003 0.001 0.748 0.747 0.0002 0.004 0.002 0.015 *total sugars = XDP4+*CDP4+ + XDP3*CDP3 + XDP2*CDP2 + Cglucose where: XDP4+ = 1.111 g glucose equivalents/g DP4+ XDP3 = 1.07 g glucose equivalents/g DP3 XDP2 = 1.05 g glucose equivalents/g DP2 Ci = concentration of compound "i" [002871 Table 15. Mass loss (g) throughout fermentation 97 WO 2013/120035 PCT/US2013/025457 Fermentation time (hrs) Treatment ID 15.67 22 39 46 62 6.36 10.77 6.74 10.90 6.90 10.93 7.04 10.95 13.18 13.64 5% 6.85 10.96 13.17 13.63 6.92 10.94 13.26 13.77 6.91 10.99 13.25 13.80 14.34 6.98 11.01 13.28 13.82 14.43 6.64 10.76 13.10 13.66 14.27 6.68 10.91 6.99 10.78 7.20 11.00 6.94 10.65 12.75 13.28 10% 6.99 11.01 13.27 13.77 7.03 11.08 13.39 13.86 7.16 11.04 13.36 13.87 14.54 6.91 10.64 12.89 13.48 14.34 6.86 11.00 13.32 13.94 14.67 6.07 11.40 6.59 11.76 6.42 11.60 6.31 11.52 14.55 14.98 20% 6.49 11.64 14.36 14.79 6.58 11.72 14.45 14.82 6.45 11.62 14.40 14.90 15.56 6.41 11.62 14.63 15.15 15.85 6.37 11.54 14.52 15.04 15.78 5.44 10.91 30% 5.65 11.00 5.70 11.07 98 WO 2013/120035 PCT/US2013/025457 5.85 11.17 15.51 16.00 6.03 11.28 15.21 15.72 5.80 11.07 14.78 15.18 5.76 11.13 15.77 16.36 17.06 5.69 11.00 15.58 16.13 16.86 5.83 11.12 15.68 16.25 16.98 3.96 9.58 4.36 10.17 4.14 9.68 3.19 8.18 15.45 16.6 40% 4.18 9.80 16.14 16.72 4.26 10.01 16.0 15.58 4.10 9.66 16.25 16.87 17.73 3.11 7.95 15.26 16.59 17.74 3.93 9.58 16.11 16.72 17.59 3.27 8.63 3.47 8.65 2.45 6.59 3.59 8.83 16.03 17.14 47.5% 3.80 9.30 14.93 15.33 3.55 8.70 15.75 16.75 2.37 6.47 13.73 15.25 17.02 3.43 8.71 15.92 16.69 17.54 3.41 8.86 15.21 15.70 16.45 3.28 8.48 2.11 5.87 3.33 8.43 3.43 8.73 15.10 15.55 3.28 8.25 15.65 16.73 2.17 5.90 13.02 14.57 3.39 8.49 15.92 16.76 17.63 3.26 8.40 15.11 15.59 16.34 99 WO 2013/120035 PCT/US2013/025457 3.14 8.14 15.69 16.9 17.87 5.02 10.03 5.26 10.11 5.19 10.15 5.38 10.04 13.08 13.48 5.27 10.23 13.09 13.49 5.29 10.18 13.15 13.56 5.38 10.25 13.15 13.64 14.17 5.38 10.24 13.11 13.59 14.18 5.32 10.20 12.99 13.48 14.07 QC 5.30 10.06 5.00 9.91 5.40 10.15 13.24 13.59 5.08 9.91 13.48 13.84 5.15 9.95 13.43 13.77 5.12 9.95 13.42 13.78 14.39 5.35 10.22 13.44 13.81 14.41 4.79 9.67 13.30 13.61 14.14 0.24 0.43 0.25 0.44 0.26 0.44 0.30 0.48 1.30 1.67 glucose 0 control 0.27 0.45 1.28 1.65 0.30 0.49 1.35 1.73 2.60 0.29 0.48 1.33 1.72 2.56 0.28 0.46 1.28 1.64 2.52 100 WO 2013/120035 PCT/US2013/025457 [002881 Table 16 pH throughout fermentation fermentation time (hrs) Treatment ID 22 46 62 3.36 3.50 3.60 5% 3.31 3.47 3.55 3.29 3.38 3.46 2.92 3.18 3.39 10% 2.93 3.18 3.30 2.91 3.21 3.35 3.60 3.94 4.00 20% 3.59 3.90 4.06 3.51 3.91 4.04 4.11 4.41 4.49 30% 4.02 4.40 4.50 4.08 4.33 4.49 3.84 3.74 3.95 40% 3.76 3.81 3.91 3.75 3.80 3.93 3.73 3.85 3.80 47.5% 3.65 3.78 3.85 3.61 3.73 3.85 4.07 4.58 4.46 50% 4.05 4.41 4.59 4.04 4.37 4.41 4.15 4.51 4.64 4.20 4.45 4.44 4.53 4.38 4.45 QC 4.23 4.51 4.49 4.57 4.45 4.49 4.22 4.63 4.46 glucose 3.81 3.54 3.69 control 3.80 3.60 3.76 101 WO 2013/120035 PCT/US2013/025457 3.85 3.68 3.76 [002891 Conclusions [00290] This example tested the effect of adding different proportions of C6 Saccharide Stream to corn mash on ethanol production. The criteria evaluated to determine the effect of these additions were mass loss, ethanol concentration, and ethanol yield. Residual sugars and glycerol were also evaluated for each treatment in order to get a clearer picture of the overall process, especially in regards to optimization of the C6 Saccharide Stream amendment dose for corn-to-ethanol fermentations. [00291] Statistically significant increases in mass loss, ethanol concentrations and yield were found for doses above 10% C6 Saccharide Stream. For the higher doses of C6 Saccharide Stream (40%, 47.5% and 50%), the total residual sugars concentration may indicate an incomplete fermentation. In practical applications, a value much above 2% of total residual sugars can create processing problems during distillation. Given the increase ethanol yield however, it may be desirable to find an optimum dose whereby the addition of C6 Saccharide Stream would maximize the benefits (increased yield) and minimize the residual sugars. [00292] Figure 9 shows a dose response plot of the increase in ethanol yield and the residual sugar levels for the treatment conditions tested. Taking into consideration the uncertainty on the measurements, these data suggest that a dose between 35% and 45% of C6 Saccharide Stream may perform the best in a fuel ethanol fermentation. [002931 If it is desirable to have a concentration of residual sugars below 2%, a lower dose may also be useful. These results were achieved by fermenting a mash that contained 25% solids. An increase in ethanol yield of 5

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2 0 % is a major improvement over ethanol fermentations with no amendments. [00294] Example 11 [002951 In this example, three different saccharide streams and two different lignin streams were subjected to free amino acids profiling (Table 17), trace metals analysis (Table 18), and fatty acid profiling (Table 19). All of the samples were produced from the hydrolysis of pretreated corn stover. [00296] C5 + C6 Saccharides Stream & C5 +C6 Lignin Stream [002971 Pretreated corn stover containing about 30% solids was used to produce the 'C5 + C6 Saccharide Stream' and the 'C5 + C6 Lignin Stream'. The solids were placed into a jacketed kettle with an agitator. Water was added to the pretreated solids to create an about 102 WO 2013/120035 PCT/US2013/025457 10% solids solution (wt/v). The temperature of the pretreated corn stover was then brought up to about 50'C. The pH was adjusted using ammonium hydroxide to about 5.0. Once pH and temperature are both set, cellulase enzymes were added to the solids at a dosing of about 5% of total dry solids (wt/wt). The solution was kept at about 50'C, a pH of about 5.0 and at constant agitation for about 72 hours. The solids were then separated via filtration from the liquid stream to produce the C5 + C6 Lignin Stream at about 20% solids (w/w). The liquid stream at this point contains C5 and C6 monosaccharides . The liquid stream was then concentrated via evaporation to the desired monosaccharide levels to produce the C5 + C6 Saccharides Stream. The C5 + C6 Saccharides stream contained about 18.7% C6 and about 6.8% C5 saccharides. [00298] C5 Saccharides Stream [00299] Pretreated corn stover containing about 30% solids was used to create the C5 saccharides stream. To extract the monomeric C5 saccharides, hot water (at about 50'C) was mixed with the pretreated solids at a rate of about IL of water for every 1 kg of wet solids. Once the water was mixed with the pretreated solids, the biomass and hot water solution was mixed for about 15 minutes at about 50'C. The solids were then filtered out and the liquid fraction was collected. The liquid fraction was then sequestered. The solids were then re collected and re-washed with the same ratio of hot water (at about 50'C) and mixed for about 15 minutes at about 50'C. The solids were then once again filtered out and the liquid fraction was collected and sequestered. The liquid fraction from the second wash was then combined with the liquid fraction from the first wash and the entire liquid fraction was concentrated via evaporation to the desired saccharide levels, yielding the C5 Saccharides Stream. The C5 Saccharides Stream contained about 12.9% C5 saccharides and about 1.3 % C6 saccharides. [003001 C6 Saccharides Stream & C6 Lignin Stream [003011 The C6 Saccharides Stream and C6 Lignin Stream are produced from the solids sequestered during production of the C5 Saccharide Stream. The solids were placed into a jacketed kettle with an agitator. Water was added to the pretreated solids to create an about 10% solids solution (w/v). The temperature of the pretreated corn stover was then brought up to about 50'C. The pH was adjusted using ammonium hydroxide to about 5.0. Once pH and temperature were both set, cellulase enzymes (Celtech 3 cellulase from Novozyme) were added to the solids at a dosing of about 5% of total dry solids (wt/wt). The solution was kept at about 50'C, a pH of about 5.0 and at constant agitation for about 72 hours. The solids were then separated from the liquid stream via filtration to produce the C6 Lignin Stream at about 20% solids. The liquid stream at this point is enriched for C6 103 WO 2013/120035 PCT/US2013/025457 monosaccharides. The liquid stream was then concentrated via evaporation and vacuum to the desired saccharide levels to produce the C6 Saccharide Stream. The C6 Saccharide Stream contained about 25.10% C6 saccharides and about 2.6% C5 Sugars. [00302] Table 17. Amino acids profiling (% w/v) C5 +6+LC6inCC6LgCi Amino Acid Saccharides Saicchairides Sacchairides C+6Lgi 6Lgi Stream Stream Stream Stream Stream Aprtic < 0.01%o < 0.01%o < 0.01%o < 0.01%o < 0.01%0 Threonine < 0.01%o < 0.01%o < 0.01%o < 0.01%o < 0.01%o Serine < 0.01%o < 0.01%o < 0.01%o < 0.01%o < 0.01%o Glutamic Acid < 0.01%o < 0.01%o < 0.01%o < 0.01%o < 0.01%o Proline < 0.01%o < 0.01%o < 0.01%o < 0.01%o < 0.01%o Glycine < 0.01%o < 0.01%o < 0.01%o < 0.01%o < 0.01%o Alanine < 0.01%o < 0.01%o < 0.01%o < 0.01%o < 0.01%o Cystine, free < 0.0100 < 0.0100 < 0.0100 < 0.0100 < 0.0100 Valine < 0.0100 < 0.0100 < 0.0100 < 0.0100 < 0.0100 Methionine < 0.0100 < 0.0100 < 0.0100 < 0.0100 < 0.0100 Isoleucine < 0.0100 < 0.0100 < 0.0100 < 0.0100 < 0.0100 Leucine < 0.0100 < 0.0100 < 0.0100 < 0.0100 < 0.0100 Tyrosine < 0.0100 < 0.0100 < 0.0100 < 0.0100 < 0.0100 Phenylalanine < 0.0100 < 0.0100 < 0.0100 < 0.0100 < 0.0100 Lysine 0.0100 0.0100 0.0100 <0.0100 <0.0100 Histidine < 0.0100 < 0.0100 < 0.0100 < 0.0100 < 0.0100 Arginine < 0.0100 < 0.0100 < 0.0100 < 0.0100 0.0500 [003031 Table 18. Trace metal analysis (PPM; Parts Per Million) C5 + C6ininCC6LgCi Metal Saecharides Saccharides Saecharides C+6Lgi 6Lgi Streamn Streaim Stream Stream Stream Aluminum 6.4 < 4.9 36 25 180 Antimony <0.50 <0.49 <0.49 <0.50 <0.50 Arsenic < 0.25 < 0.24 < 0.24 <0.25 <0.25 104 WO 2013/120035 PCT/US2013/025457 Barium 0.26 0.15 0.10 5.4 6.2 Cadmium < 0.099 < 0.097 < 0.097 <0.10 <0.099 Calcium 330 86 340 210 1100 Chromium 1.7 0.15 5.4 6.9 15 Cobalt < 0.099 < 0.097 0.29 <0.10 0.15 Copper 1.3 0.77 4.7 6.3 10 Iron 21 < 1.2 170 89 260 Lead < 0.19 < 0.18 < 0.18 0.34 0.45 Magnesium 71 25 180 32 48 Manganese 2.0 0.26 5.1 1.0 1.2 Nickel 1.2 < 0.24 4.9 2.0 3.6 Phosphorus 150 95 170 57 34 Potassium 570 97 1500 200 420 Selenium <0.74 <0.73 <0.73 <0.75 <0.74 Silver < 0.25 < 0.24 <0.24 <0.25 0.29 Sodium 3000 480 460 1100 61 Tin < 0.50 < 0.49 <0.49 0.79 1.0 Vanadium <0.30 <0.49 <0.49 <0.50 0.51 Zinc 1.8 < 0.49 8.2 2.3 1.7 [00304] Table 19. Fatty acid profiling (% w/w) C5 +C6 C6 CS C5 +C6 C6 Lignin FattyAcidSacchairides Saccharides Saiccharides Lignin Stream Srm temStream Stream C40Btrc0.00 0.00 0.00 0.00 0.00 C6:0 Hexanoic 0.00 0.00 0.00 0.00 0.00 C8:0 Octanoic 0.00 0.00 0.00 0.00 0.00 C 10:0 Decanoic 0.00 0.00 0.00 0.00 0.00 C 12:0 Lauric 0.00 0.00 0.00 0.00 0.00 C 13:0 Tridecanoic 0.00 0.00 0.00 0.00 0.00 C 14:0 Myristic 0.00 0.00 0.00 0.00 0.00 C15:0 Pentadecanoic 0.00 0.00 0.00 0.00 0.00 105 WO 2013/120035 PCT/US2013/025457 C16:0 Palmitic 0.00 0.00 0.00 0.00 0.04 C17:0 Heptadecanoic 0.00 0.00 0.00 0.00 0.00 C18:0 Stearic 0.00 0.00 0.00 0.02 0.02 C20:0 Arachidic 0.00 0.00 0.00 0.00 0.01 C21:0 Heneicosanoic 0.00 0.00 0.00 0.00 0.00 C22:0 Behenic 0.00 0.00 0.00 0.01 0.01 C23:0 Tricosanoic 0.00 0.00 0.00 0.00 0.00 C24:0 Lignoceric 0.00 0.00 0.00 0.01 0.01 C14:1 (cis-9) Myristoleic 0.00 0.00 0.00 0.00 0.00 C15:1 (cis-10) Pentadecinoic 0.00 0.00 0.00 0.00 0.04 C16:1 (cis-9) Palmitoleic 0.00 0.00 0.00 0.00 0.00 C17:1 (cis-lO) 0.00 0.00 0.00 0.00 0.00 Heptadecenoate C18:1 (cis-9) Oleic 0.00 0.00 0.00 0.05 0.06 C20:1 (cis-11) Eicosenoic 0.00 0.00 0.00 0.00 0.00 C22:1 (cis-13) Erucic 0.00 0.00 0.00 0.00 0.00 C24:1 (cis-15) Nervonic 0.00 0.00 0.00 0.00 0.00 C18:2 (cis-9, 12) Lonoleic 0.00 0.00 0.00 0.07 0.05 C18:3 (cis-6, 9, 12) y 0.00 0.00 0.00 0.00 0.00 linolenic C18:3 (cis-9, 12,15) 0.00 0.00 0.00 0.00.00.00.02 0.00 Linolenic C20:2 (cis-11, 14) 0.00 0.00 0.00 0.00 0.00 Eicosadienoic C20:3 (cis-8, 11,14) 0.00 0.00 0.00 0.00 0.00 Eicosatrienoic C20:3 (cis-li, 14, 17) 0.00 0.00 0.00 0.00 0.00 Eicosatrienoic C20:4 (cis-5, 8, 11, 14) 0.00 0.00 0.00 0.00 0.00 Arachidonic C20:5 (cis-5, 8, 11, 14, 17) 0.00 0.00 0.00 0.00 0.00 Eicosapentanoic 106 WO 2013/120035 PCT/US2013/025457 C22:2 (cis-13, 16) 0.00 0.00 0.00 0.00 0.01 Docosadienoic C22:6 (cis-4, 7, 10, 13, 16, 19) 0.00 0.00 0.00 0.00 0.00 Docosahexaenoic C18:1 (trans-9) Methyl 0.00 0.00 0.00 0.01 0.00 Elaidate C 18:2 (trans-9, 12) Methyl 0.00 0.00 0.00 0.00 0.00 Linoelaidate [00305] Example 12 [00306] In this example, yeast fermentations are performed using 80:20 blends of corn mash and a C6 Saccharide Stream produced from corn stover or an equivalent amount of pure sugars. The corn mash was prepared according as in Example 10 and had a glucose concentration of about 30% (w/v). [003071 Preparation of C6 Saccharide Stream containing cellulosic-derived saccharides [00308] Upon completion of pretreatment, the post-treated material, which comprised about 25% to about 30% solids [wt/v], was subjected to a water washing step to separate solubilized C5 saccharides from C6 Saccharides (the C5 saccharide stream includes some amount of C6 from glycan hydrolysis "impurity"). The washing was performed in two steps; in the first step, the post- treated feedstock was separated by filter press to separate the solids from the liquid stream containing the C5 saccharides. The solid material was further suspended in water to recover additional C5 saccharides which may have remained in the separated solids portion. On removing the soluble hemicellulose sugars (C5 saccharides), the remaining solids contained the cellulose (C6 saccharides). The liquid stream was then retained and kept separate from the solids. [00309] The separated solids were placed into a mixing tank. Once inside the mixing tank, the solids were adjusted to a pH of about 5 using 0.1 N Sodium Hydroxide. The solids were then diluted with water to about 10% solids. An enzyme cocktail (CELLIC CTech 2, Novozymes) was then added to the solid slurry. The amount of the enzyme added to the mixture was 2% loading (v/wt) based on the dry weight of the solids. The slurry was mixed at 50'C continuously for 72 hours. 107 WO 2013/120035 PCT/US2013/025457 [003101 Once enzymatic hydrolysis was complete, the liquid slurry was separated by centrifugation or microfiltration; or, alternatively, the solids can remain in the broth. For the experiments herein, the solids were separated from the broth using evaporation. A lab-scale evaporation set up in Buchi R220SE evaporator was used. About 30 L of the resultant C6 rich liquid slurry was concentrated by simple evaporation at a temperature of 60 degrees C until the sugar content of the Corn Stover hydrolysate (C6 Saccharide Stream) was raised from about 5% to about 25% w/v. The resulting composition had a C6 saccharide: C5 saccharide ratio of about 90:10. [003111 Fermentation Reaction [00312] Six bench top fermentation flasks were set up for each condition. Each flask contained a total of 275 g of fermentation substrate made up of 220 g of corn mash and 55 g of the C6 Saccharide Stream containing 25.4% glucose & 4.3% xylose or a stock solution of the same sugar concentrations. Additional fermentation additives included 0.5 mL of a 40% urea solution, 0.305 mL of a 1:10 dilution of Spirozym Ultra XHS delivered at 0.036% w/w, 0.245 mL of a 1:100 dilution of protease, 0.1 mL of a 1:100 dilution of phytase, and a scoop of V50. [00313] Fermentation progress was monitored by weighing the flasks at 6 hour intervals for a total of 66 hours. The mass loss for each flask containing an 80:20 blend of corn mash and the C6 Saccharide Stream (Exp. 1-6) or an 80:20 blend of corn mash and stock sugars (Cont. 1-6) is shown in Table 20. The average mass loss for each condition is graphed in Figure 19. [00314] Table 20. Fermentation progress Total Weight Loss (g) 6hr 12hr 18hr 24hr 30hr 36hr 42hr 48hr 54hr 60hr 66hr Cont. 1 2.99 12.93 21.10 25.13 28.00 29.88 31.47 Cont. 2 -0.60 9.59 17.43 22.26 25.78 27.74 29.97 29.03 29.72 28.98 29.63 Cont. 3 1.96 12.13 20.01 25.01 28.19 30.24 31.15 31.35 31.28 31.53 31.64 Cont. 4 1.63 12.49 20.21 23.79 27.75 30.12 30.86 Cont. 5 2.11 11.03 19.56 23.34 27.91 29.26 29.53 28.88 29.43 30.15 29.25 Cont. 6 2.76 11.96 19.63 23.59 27.80 29.65 29.71 29.60 29.98 30.06 30.78 Cont. 1.81 11.69 19.66 23.85 27.57 29.48 30.45 29.72 30.10 30.18 30.33 Avg. 108 WO 2013/120035 PCT/US2013/025457 Exp. 1 1.27 12.43 19.36 22.86 25.64 27.13 28.14 Exp. 2 2.00 11.43 19.62 23.71 26.81 28.34 30.36 30.00 31.40 30.61 31.83 Exp. 3 1.45 11.82 19.64 24.11 27.44 29.52 30.36 30.69 30.69 30.85 31.44 Exp. 4 1.97 13.57 20.20 24.73 28.81 30.09 30.82 Exp. 5 0.66 11.19 18.70 23.17 26.81 28.55 29.62 29.69 29.72 30.39 29.87 Exp. 6 2.72 13.78 20.49 24.81 29.52 30.13 30.60 31.33 31.44 31.82 32.56 Exp. 1.68 12.37 19.67 23.90 27.51 28.96 29.98 30.43 30.81 30.92 31.43 Avg [003151 Residual sugars (DP4, DP3, Maltose, and Glucose), and fermentation products (lactic acid, glycerol, acetic acid, and ethanol) were analyzed by HPLC. Two flasks from each condition were analyzed after 42 hours; the remaining four flasks for each condition were analyzed after 66 hours of fermentation. Tested flasks were discarded due to exposure to air and interruption of fermentation. The results are shown in Table 21. [00316] Table 21. Residual sugars and total products Residual Sugars (% /v Final Products (% w/v) Lactic Acetic [003171 DP4 DP3 Maltose Glucose Acid Gl cerol Acid Ethanol Cont. 1 (42 hr) 0.456 0 049 0.772 0A054 0 135 1L675 0 097 131129 Cont. 2 (66 hr) 0.448 0.045 0.706 0.057 0.131 1.617 0.112 13.293 Cont. 3 (66hr 0.446 0.045 0.736 0.056 0.144 1.665 0.108 13.239 Cont. 4 (4 h)0.445 0 047 0.726 0 055 0,144 1.646 0.097 13.184 Cont. 5 (66hr 0.436 0.047 0.753 0.054 0.145 1.664 0.109 13.17 Cont. 6 (6h)0.45 0.047 0.772 0.058 0.145 1.678 0.112 13.093 Cont. Avg (66 hr) 0.445 0.046 0.742 0.0563 0.141 1.656 0.110 13.199 Exp. 1 (42 hr) 0.599 0,177 0.849 0 439 0 3 1 522 0 102 13.251 Exp. 2 (66 hr) 0.572 0.17 0.831 0.09 0.129_ 1.541 0.113 13.522 Exp. 3 (66hr 0.568 0.168 0.825 0.086 0.131 1.53 0.11 13.596 Exp. 4 (42 hr) 8 7 81I2 (1124 0 31 1528 0 105 13496 109 WO 2013/120035 PCT/US2013/025457 Exp. 5 (66 hr) 0.565 0.169 0.804 0.081 0.132 1.539 0.113 13.481 Exp. 6 (66 hr) 0.565 0.167 0.815 0.067 0.132 1.532 0.11 13.628 Exp. Avg (66 hr) 0.568 0.169 0.819 0.081 0.131 1.536 0.112 13.557 [003181 The fermentations dosed with the C6 Saccharide Stream showed a 2.7% increase in ethanol yield and a 7.2% decrease in glycerol production in comparison to the fermentations dosed with stock sugars. [003191 Example 13 [00320] In this example, yeast fermentations are performed using 80:20 blends of corn mash C6 Saccharide Stream produced from corn stover or an equivalent amount of pure sugars. The corn mash and C6 Saccharide Streams were prepared as in Example 12. [00321] Six bench top fermentation flasks were set up for each condition. Each flask contained a total of 275 g of fermentation substrate made up of 220 g of corn mash and 55 g of the C6 Saccharide Stream containing 25.4% glucose & 4.3% xylose or a stock solution of the same sugar concentrations. Additional fermentation additives included 0.5 mL of a 40% urea solution, 0.305 mL of a 1:10 dilution of Spirozym Ultra XHS delivered at 0.036% w/w, 0.245 mL of a 1:100 dilution of protease, 0.1 mL of a 1:100 dilution of phytase, and a scoop of V50. [00322] Fermentation progress was monitored by weighing the flasks at 6 hour intervals for a total of 60 hours. The mass loss for each flask containing an 80:20 blend of corn mash and the C6 Saccharide Stream (Exp. 1-6) or an 80:20 blend of corn mash and stock sugars (Cont. 1-6) is shown in Table 22. The average mass loss for each condition is graphed in Figure 20. [00323] Table 22. Fermentation progress Total Weight Loss (g) 6hr 12hr 18hr 24hr 30hr 36hr 42hr 48hr 54hr 60hr Cont. 1 3.50 14.34 21.05 25.25 28.85 29.97 30.41 31.05 31.28 31.66 Cont. 2 2.88 13.74 21.00 26.85 30.16 30.53 30.08 31.26 30.10 31.20 Cont. 3 2.96 13.17 20.55 24.39 28.46 29.97 31.56 31.33 31.78 32.63 Cont. 4 3.90 14.78 21.35 24.94 28.50 30.50 31.17 31.06 32.77 31.04 Cont. 5 5.42 15.26 23.03 27.06 29.80 31.03 31.13 31.43 31.93 31.35 Cont. 6 1.96 13.11 19.48 23.12 27.20 28.37 29.16 29.01 29.11 29.16 110 WO 2013/120035 PCT/US2013/025457 Cont. 3.44 14.07 21.08 25.27 28.83 30.06 30.59 30.86 31.16 31.17 Avg. Exp. 1 3.08 13.91 20.26 23.78 26.54 28.75 30.29 29.92 30.41 30.17 Exp. 2 4.07 15.25 21.13 25.50 28.34 31.13 32.12 32.09 31.70 31.95 Exp. 3 2.64 14.09 21.51 25.49 28.48 29.98 30.04 31.23 30.91 31.33 Exp. 4 3.29 15.69 22.82 26.16 30.59 33.07 33.24 34.53 35.70 35.34 Exp. 5 3.35 14.48 21.21 25.55 29.58 30.79 31.21 31.29 31.28 33.14 Exp. 6 2.59 14.01 20.64 24.92 28.46 29.56 29.83 30.65 30.58 31.48 Exp. 3.17 14.57 21.26 25.23 28.67 30.55 31.12 31.62 31.76 32.24 Avg [00324] Residual sugars (DP4, DP3, Maltose, and Glucose), and fermentation products (lactic acid, glycerol, acetic acid, and ethanol) were analyzed by HPLC after 60 hours. The results are shown in Table 21. [003251 Table 21. Residual sugars and total products (% w/v) Residual Sugars Final Products Lactic Acetic DP4 DP3 Maltose Glucose Acid Glycerol Acid Ethanol Cont. 1 0.469 0.062 0.772 0.07 0.1 1.713 0.091 13.765 Cont. 2 0.458 0.064 0.78 0.069 0.102 1.737 0.089 13.649 Cont. 3 0.461 0.062 0.77 0.067 0.1 1.695 0.087 13.6 Cont. 4 0.459 0.064 0.818 0.066 0.102 1.762 0.085 13.702 Cont. 5 0.453 0.064 0.804 0.069 0.104 1.752 0.085 13.595 Cont. 6 0.459 0.064 0.822 0.068 0.136 1.894 13.503 Cont. 0.460 0.063 0.794 0.068 0.107 1.759 0.087 13.636 Avg Exp. 1 0.657 0.171 0.9 0.098 1.588 0.096 13.602 Exp. 2 0.64 0.172 0.869 0.102 0.1 1.608 0.095 13.944 Exp. 3 0.666 0.174 0.888 0.101 0.104 1.634 0.099 13.85 Exp. 4 0.66 0.172 0.895 0.175 0.102 1.603 0.104 13.875 Exp. 5 0.638 0.169 0.849 0.085 0.102 1.603 0.1 14.009 111 WO 2013/120035 PCT/US2013/025457 Exp. 6 0.667 0.173 0.916 0.103 1.616 0.096 13.81 Exp. 0.655 0.172 0.886 0.116 0.102 1.609 0.098 13.848 Avg Blank cells represent machine errors and are excluded from the average values. [003261 The fermentations dosed with the C6 Saccharide Stream showed a 1.6% increase in ethanol yield and an 8.5% decrease in glycerol production in comparison to the fermentations dosed with stock sugars at the same concentration. [003271 Example 14 [003281 In this example, yeast fermentations are performed to compare a corn mash only fermentation with a 70:30 blend of corn mash and a C6 Saccharide Stream produced from corn stover. The corn mash and C6 Saccharide Stream were produced as in Example 12. [00329] Fermentation Reaction [003301 215 mL of corn mash was propagated in a 1 L flask. In addition, 65 mL of distilled water, 16 mL of city water, 1 mL of a 40% urea solution and 0.03 g antibiotic was also added to the propagation flask. Solutions were warmed to 32 'C before propagation was started. Once heated to 32 'C, 0.15 g of yeast and 38 gL of glucoamylase was added to the flask and agitated at 150 RPM for 10 hours. [003311 Fermentation was carried out in 750 mL solutions in IL flasks for 96 hours. The fermentation conditions are detailed in Table 22. [00332] Table 22. Fermentation substrate and additives C6 Corn Mash Yeast prop Sample Urea Glucoamylase Saccharide (ferm feed) Stream drop Corn mash 675 mL 0.975 mL 0.1725 mL 0 ML 75 mL control 70:30 Corn Mash: C6 450 mL 0.975 mL 0.1095 mL 225 mL 75 mL Saccharide Stream [003331 The rate of ethanol production during fermentation of corn mash only (diamonds) and (70:30) corn mash: C6 Saccharide Stream (squares) is shown in Figure 21. The final ethanol titers were similar between the two conditions; however, the 70:30 blend 112 WO 2013/120035 PCT/US2013/025457 fermentation reaction reached the plateau level earlier. These data indicate that the ethanol production rate kinetics is improved by use of the blended feedstock. [00334] The rate of glycerol production during fermentation of corn mash only (diamonds) and (70:30) corn mash: C6 Saccharide Stream (squares) is shown in Figure 22. The final glycerol levels and the rates of production of glycerol were both higher in the corn mash only fermentation. [003351 The conversion efficiency of fermentation of corn mash only and the 70:30 blend of corn mash and the C6 Saccharide Stream is shown in Table 23. [003361 Table 23. Sample Initial sugar Residual Sugar Ethanol % Sugar to (g/L) sugar (g/L) utilization produced ethanol (g/L) conversion efficiency Corn mash 231.5 9.25 96% 134.35 114% control 70:30 blend 229.8 9.3 95.9% 130 115.6% [003371 While preferred embodiments of the present invention have been shown and described herein, it will be obvious to those skilled in the art that such embodiments are provided by way of example only. Numerous variations, changes, and substitutions will now occur to those skilled in the art without departing from the invention. It should be understood that various alternatives to the embodiments of the invention described herein may be employed in practicing the invention. It is intended that the following claims define the scope of the invention and that methods and structures within the scope of these claims and their equivalents be covered thereby. 113

Claims (256)

1. A method of producing one or more fermentation end-products comprising: (a) combining a first biomass comprising non-cellulosic saccharides with a saccharide stream comprising C6 monosaccharides to produce a blended feedstock in a broth; (b) contacting the blended feedstock with one or more biocatalysts; (c) fermenting the non-cellulosic saccharides of the first biomass and the C6 monosaccharides of the saccharides stream to produce one or more fermentation end-products comprising an alcohol and a polyol, wherein an alcohol yield is increased and a polyol yield is decreased in comparison to fermentation of the first biomass without the saccharide stream.

2. The method of claim 1, wherein the alcohol is ethanol.

3. The method of claim 1, wherein the polyol is glycerol.

4. The method of claim 1, wherein the broth comprising the blended feedstock has a lower osmolarity than a broth containing only the first biomass at an equivalent total saccharide level in monosaccharide equivalents.

5. The method of claim 1, wherein the saccharide stream further comprises C5 monosaccharides.

6. The method of claim 1, wherein the C6 monosaccharides comprise cellulosic-derived C6 monosaccharides, non-cellulosic derived C6 monosaccharides, or a combination thereof.

7. The method of claim 1, wherein the alcohol yield is increased by about 1% to about 100% relative to fermentation of the first biomass without the saccharide stream.

8. The method of claim 1, wherein the alcohol is produced at a rate that is faster relative to fermentation of the first biomass without the saccharide stream.

9. The method of claim 1, wherein the alcohol is produced at a rate that is about 1% to about 100% faster relative to fermentation of the first biomass without the saccharide stream.

10. The method of claim 1, wherein the C6 monosaccharides of the saccharide stream are at a concentration that differs from a concentration of the non-cellulosic saccharides in the first biomass by less than +/- 50%, wherein the concentration of non-cellulosic saccharides in the first biomass is in monosaccharide equivalents.

11. The method of claim 1, wherein the C6 monosaccharides of the saccharide stream are at a concentration that differs from a concentration of the non-cellulosic saccharides in the first biomass by less than +/- 25%, wherein the concentration of non-cellulosic saccharides in the first biomass is in monosaccharide equivalents. -114- WO 2013/120035 PCT/US2013/025457

12. The method of claim 1, wherein the method is a fed-batch fermentation wherein the saccharide stream is added over time.

13. The method of claim 12, wherein the saccharide stream is added at a rate of from about 0.01 mL/min/L of broth to about 5 mL/min/L of broth during the fermenting.

14. The method of claim 1, wherein the polyols yield is decreased by about 1% to about 100% relative to the non-fed batch fermentation.

15. The method of claim 1, wherein the first biomass comprises starch, sucrose, or a combination thereof

16. The method of claim 1, wherein the first biomass comprises corn, corn mash, sugar cane, sugar beets, sugar palms, sweet sorghum, nypa palm, cassava, rice, milo, sorghum, sweet potatoes, wheat, molasses, tubers, roots, stems, whole grains, barley, rye, milo, sago, cassaya, tapioca, rice peas, beans, potatoes, beets, fruits, or a combination thereof

17. The method of claim 1, wherein the saccharide stream is produced from the pretreatment and/or hydrolysis of cellulose, hemicellulose, lignocellulose material, starch, or a combination thereof

18. The method of claim 1, wherein the saccharide stream is produced by the pretreatment and/or hydrolysis of a second biomass comprising cellulose, hemicellulose, and/or lignocellulose.

19. The method of claim 18, wherein the second biomass comprises corn, corn syrup, corn stover, corn cobs, molasses, silage, grass, straw, grain hulls, bagasse, distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof

20. The method of claim 1, wherein the one or more biocatalysts comprise one or more fermenting microorganisms.

21. The method of claim 1, wherein the one or more biocatalysts comprise one or more yeasts and/or one or more bacteria.

22. The method of claim 1, wherein the one or more biocatalysts comprise one or more yeasts.

23. The method of claim 1, wherein the one or more biocatalysts comprise one or more strains of Saccharomyces cerevisiae. -115- WO 2013/120035 PCT/US2013/025457

24. The method of claim 1, wherein at least one of the one or more biocatalysts is a genetically-modified yeast that ferments C5 and C6 saccharides.

25. The method of claim 1, wherein at least one of the one or more biocatalysts is a bacteria that hydrolyzes and/or ferments C5 and C6 saccharides.

26. The method of claim 1, wherein at least one of the one or more biocatalysts is a hydrolytic enzyme.

27. The method of claim 1, wherein the one or more biocatalysts comprise an endoglucanase, an exoglucanase, a cellobiohydrolase, a cellulase, a beta-glucosidase, a glycoside hydrolase, a glycosyltransferase, a lyase, an esterase, a glucamylase, or a combination thereof.

28. The method of claim 1, wherein at least one of the one or more biocatalysts is an enzyme that hydrolyzes starch.

29. The method of claim 1, wherein at least one of the one or more biocatalysts is an alpha-amylase, glucoamylase, beta-amylase, exo-alpha- 1,4-glucanase, or pullulanase.

30. The method of claim 1, wherein the one or more biocatalysts comprise at least one fermenting microorganism and at least one hydrolytic enzyme.

31. The method of claim 1, wherein the one or more biocatalysts comprise at least one fermenting microorganism that is a yeast or bacteria and at least one enzyme that hydrolyzes starch.

32. The method of claim 1, wherein the blended feedstock comprises less than 100 g/L monosaccharides prior to contacting with the one or more biocatalysts.

33. The method of claim 1, wherein the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides prior to contacting with the one or more biocatalysts.

34. The method of claim 1, wherein the first biomass and the saccharide stream are combined in a ratio of from about 50:50 to 99:1 (first biomass: saccharide stream) by volume or by weight:volume.

35. The method of claim 1, wherein the first biomass and the saccharide stream are combined in a ratio of about 80:20 (first biomass: saccharide stream) by volume or by weight:volume.

36. The method of claim 1, wherein the first biomass and the saccharide stream are combined in a ratio of about 90:10 (first biomass: saccharide stream) by volume or by weight:volume.

37. The method of claim 1, wherein the blended feedstock comprises from about 10% to about 50% solids from the first biomass. -116- WO 2013/120035 PCT/US2013/025457

38. The method of claim 1, wherein the blended feedstock comprises from about 20% to about 40% solids from the first biomass.

39. The method of claim 1, wherein the blended feedstock comprises from about 30% to about 36% solids from the first biomass.

40. The method of claim 1, wherein the C6 monosaccharides of the saccharide stream are at a concentration of from about 10% to about 70% w/v prior to combining with the first biomass.

41. The method of claim 1, wherein the C6 monosaccharides of the saccharide stream are at a concentration of from about 20% to about 50% w/v prior to combining with the first biomass.

42. A fermentation end-product produced by the method of claim 1.

43. The fermentation end-product of claim 42, wherein the fermentation end-product is ethanol.

44. A method of producing one or more fermentation end-products comprising: (a) combining a first biomass with one or more cellulosic-derived C6 monosaccharides to produce a blended feedstock in a broth; (b) contacting the blended feedstock with one or more biocatalysts; and (c) fermenting the first biomass and the one or more cellulosic-derived C6 monosaccharides for a sufficient time to produce one or more fermentation end-products from the blended feedstock, wherein a yield of at least one of the one or more fermentation end products is increased relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides.

45. The method of claim 44, wherein the yield of the at least one of the one or more fermentation end-products is increased by about 1% to about 100% relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides.

46. The method of claim 44, wherein at least one of the one or more fermentation end products is produced at a rate that is faster relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides.

47. The method of claim 44, wherein at least one of the one or more fermentation end products is produced at a rate that is about 1% to about 100% faster relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides.

48. The method of claim 44, wherein the one or more cellulosic-derived C6 monosaccharides are at a concentration that differs from a concentration of saccharides in the -117- WO 2013/120035 PCT/US2013/025457 first biomass by less than +/- 50%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents.

49. The method of claim 44, wherein the one or more cellulosic-derived C6 monosaccharides are at a concentration that differs from a concentration of saccharides in the first biomass by less than +/- 25%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents.

50. The method of claim 44, wherein the one or more fermentation end-products comprise one or more alcohols.

51. The method of claim 44, wherein the one or more fermentation end-products comprise ethanol.

52. The method of claim 44, wherein the method is a fed-batch fermentation wherein the one or more cellulosic-derived C6 monosaccharides are added over time.

53. The method of claim 52, wherein the one or more cellulosic-derived C6 monosaccharides are added at a rate of from about 0.01 mL/min/L of broth to about 5 mL/min/L of broth during the fermenting.

54. The method of claim 44 or 52, wherein a yield of one or more other products is decreased relative to a non-fed batch fermentation.

55. The method of claim 54, wherein the yield of the one or more other products is decreased by about 1% to about 100% relative to the non-fed batch fermentation.

56. The method of claim 54, wherein the one or more other products comprise one or more polyols or sugar alcohols.

57. The method of claim 54, wherein the one or more other products comprise methanol, glycol, glycerol, erythritol, threitol, arabitol, xylitol, ribitol, mannitol, sorbitol, dulcitol, fucitol, iditol, inositol, volemitol, isomalt, maltitol, lactitol, polyglycitol, or a combination thereof.

58. The method of claim 54, wherein the one or more other products comprise glycerol.

59. The method of claim 44, wherein the first biomass comprises non-cellulosic sugars.

60. The method of claim 44, wherein the first biomass comprises non-cellulosic oligosaccharides.

61. The method of claim 44, wherein the first biomass comprises starch.

62. The method of claim 44, wherein the first biomass comprises corn, corn mash, sugar cane, sugar beets, sugar palms, sweet sorghum, nypa palm, cassava, rice, milo, sorghum, sweet potatoes, wheat, molasses, tubers, roots, stems, whole grains, barley, rye, milo, sago, cassaya, tapioca, rice peas, beans, potatoes, beets, fruits, or a combination thereof. -118- WO 2013/120035 PCT/US2013/025457

63. The method of claim 44, wherein the one or more cellulosic-derived C6 monosaccharides are produced from the pretreatment and/or hydrolysis of cellulose, hemicellulose, or lignocellulose material.

64. The method of claim 44, wherein the one or more cellulosic-derived C6 monosaccharides are produced by the pretreatment and/or hydrolysis of a second biomass comprising cellulose, hemicellulose, or lignocellulose.

65. The method of claim 64, wherein the second biomass comprises corn, corn syrup, corn stover, corn cobs, molasses, silage, grass, straw, grain hulls, bagasse, distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof.

66. The method of claim 44, wherein the one or more biocatalysts comprise one or more fermenting microorganisms.

67. The method of claim 44, wherein the one or more biocatalysts comprise one or more yeasts and/or one or more bacteria.

68. The method of claim 44, wherein the one or more biocatalysts comprise one or more yeasts.

69. The method of claim 44, wherein the one or more biocatalysts comprise one or more strains of Saccharomyces cerevisiae.

70. The method of claim 44, wherein at least one of the one or more biocatalysts is a genetically-modified yeast that ferments C5 and C6 saccharides.

71. The method of claim 44, wherein at least one of the one or more biocatalysts is a bacteria that hydrolyzes and/or ferments C5 and C6 saccharides.

72. The method of claim 44, wherein at least one of the one or more biocatalysts is a hydrolytic enzyme.

73. The method of claim 44, wherein the one or more biocatalysts comprise an endoglucanase, an exoglucanase, a cellobiohydrolase, a cellulase, a beta-glucosidase, a glycoside hydrolase, a glycosyltransferase, a lyase, an esterase, a glucamylase, or a combination thereof.

74. The method of claim 44, wherein at least one of the one or more biocatalysts is an enzyme that hydrolyzes starch.

75. The method of claim 44, wherein at least one of the one or more biocatalysts is an alpha-amylase, glucoamylase, beta-amylase, exo-alpha- 1,4-glucanase, or pullulanase. -119- WO 2013/120035 PCT/US2013/025457

76. The method of claim 44, wherein the one or more biocatalysts comprise at least one fermenting microorganism and at least one hydrolytic enzyme.

77. The method of claim 44, wherein the one or more biocatalysts comprise at least one fermenting microorganism that is a yeast or bacteria and at least one enzyme that hydrolyzes starch.

78. The method of claim 44, wherein the blended feedstock comprises less than 100 g/L monosaccharides prior to contacting with the one or more biocatalysts.

79. The method of claim 44, wherein the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides prior to contacting with the one or more biocatalysts.

80. The method of claim 44, wherein the first biomass and the one or more cellulosic derived C6 monosaccharides are combined in a ratio of from about 50:50 to 99:1 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume.

81. The method of claim 44, wherein the first biomass and the one or more cellulosic derived C6 monosaccharides are combined in a ratio of about 80:20 (first biomass: cellulosic derived C6 monosaccharides) by volume or by weight:volume.

82. The method of claim 44, wherein the first biomass and the one or more cellulosic derived C6 monosaccharides are combined in a ratio of about 90:10 (first biomass: cellulosic derived C6 monosaccharides) by volume or by weight:volume.

83. The method of claim 44, wherein the blended feedstock comprises from about 10% to about 50% solids from the first biomass.

84. The method of claim 44, wherein the blended feedstock comprises from about 20% to about 40% solids from the first biomass.

85. The method of claim 44, wherein the blended feedstock comprises from about 30% to about 36% solids from the first biomass.

86. The method of claim 44, wherein the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 10% to about 70% w/v prior to combining with the first biomass.

87. The method of claim 44, wherein the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 20% to about 50% w/v prior to combining with the first biomass.

88. A fermentation end-product produced by the method of claim 44.

89. The fermentation end-product of claim 88, wherein the fermentation end-product is ethanol.

90. A method of producing one or more fermentation end-products comprising: -120- WO 2013/120035 PCT/US2013/025457 (a) combining a first biomass with one or more cellulosic-derived C6 monosaccharides to produce a blended feedstock in a broth; (b) contacting the blended feedstock with one or more biocatalysts; and (c) fermenting the first biomass and the one or more cellulosic-derived C6 monosaccharides for sufficient time to produce one or more fermentation end-products from the blended feedstock, wherein at least one of the one or more fermentation end-products is produced at a rate that is faster relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides.

91. The method of claim 90, wherein a yield of at least one of the one or more fermentation end-products is increased relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides.

92. The method of claim 90, wherein a yield of at least one of the one or more fermentation end-products is increased by about 1% to about 100% relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides.

93. The method of claim 90, wherein the rate that the at least one of the one or more fermentation end-products is produced is about 1% to about 100% faster relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides.

94. The method of claim 90, wherein the one or more cellulosic-derived C6 monosaccharides are at a concentration that differs from a concentration of saccharides in the first biomass by less than +/- 50%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents.

95. The method of claim 90, wherein the one or more cellulosic-derived C6 monosaccharides are at a concentration that differs from a concentration of saccharides in the first biomass by less than +/- 25%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents.

96. The method of claim 90, wherein the one or more fermentation end-products comprise one or more alcohols.

97. The method of claim 90, wherein the one or more fermentation end-products comprise ethanol.

98. The method of claim 90, wherein the method is a fed-batch fermentation wherein the one or more cellulosic-derived C6 monosaccharides are added over time.

99. The method of claim 98, wherein the one or more cellulosic-derived C6 monosaccharides are added at a rate of from about 0.01 mL/min/L of broth to about 5 mL/min/L of broth during the fermenting. -121- WO 2013/120035 PCT/US2013/025457

100. The method of claim 90 or 98, wherein a yield of one or more other products is decreased relative to a non-fed batch fermentation.

101. The method of claim 100, wherein the yield of the one or more other products is decreased by about 1% to about 100% relative to the non-fed batch fermentation.

102. The method of claim 100, wherein the one or more other products comprise one or more polyols or sugar alcohols.

103. The method of claim 100, wherein the one or more other products comprise methanol, glycol, glycerol, erythritol, threitol, arabitol, xylitol, ribitol, mannitol, sorbitol, dulcitol, fucitol, iditol, inositol, volemitol, isomalt, maltitol, lactitol, polyglycitol, or a combination thereof.

104. The method of claim 100, wherein the one or more other products comprise glycerol.

105. The method of claim 90, wherein the first biomass comprises non-cellulosic sugars.

106. The method of claim 90, wherein the first biomass comprises non-cellulosic oligosaccharides.

107. The method of claim 90, wherein the first biomass comprises starch.

108. The method of claim 90, wherein the first biomass comprises corn, corn mash, sugar cane, sugar beets, sugar palms, sweet sorghum, nypa palm, cassava, rice, milo, sorghum, sweet potatoes, wheat, molasses, tubers, roots, stems, whole grains, barley, rye, milo, sago, cassaya, tapioca, rice peas, beans, potatoes, beets, fruits, or a combination thereof.

109. The method of claim 90, wherein the one or more cellulosic-derived C6 monosaccharides are produced from the pretreatment and/or hydrolysis of cellulose, hemicellulose, or lignocellulose material.

110. The method of claim 90, wherein the one or more cellulosic-derived C6 monosaccharides are produced by the pretreatment and/or hydrolysis of a second biomass comprising cellulose, hemicellulose, or lignocellulose.

111. The method of claim 110, wherein the second biomass comprises corn, corn syrup, corn stover, corn cobs, molasses, silage, grass, straw, grain hulls, bagasse, distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof. -122- WO 2013/120035 PCT/US2013/025457

112. The method of claim 90, wherein the one or more biocatalysts comprise one or more fermenting microorganisms.

113. The method of claim 90, wherein the one or more biocatalysts comprise one or more yeasts and/or one or more bacteria.

114. The method of claim 90, wherein the one or more biocatalysts comprise one or more yeasts.

115. The method of claim 90, wherein the one or more biocatalysts comprise one or more strains of Saccharomyces cerevisiae.

116. The method of claim 90, wherein at least one of the one or more biocatalysts is a genetically-modified yeast that ferments C5 and C6 saccharides.

117. The method of claim 90, wherein at least one of the one or more biocatalysts is a bacteria that hydrolyzes and/or ferments C5 and C6 saccharides.

118. The method of claim 90, wherein at least one of the one or more biocatalysts is a hydrolytic enzyme.

119. The method of claim 90, wherein the one or more biocatalysts comprise an endoglucanase, an exoglucanase, a cellobiohydrolase, a cellulase, a beta-glucosidase, a glycoside hydrolase, a glycosyltransferase, a lyase, an esterase, a glucamylase, or a combination thereof.

120. The method of claim 90, wherein at least one of the one or more biocatalysts is an enzyme that hydrolyzes starch.

121. The method of claim 90, wherein at least one of the one or more biocatalysts is an alpha-amylase, glucoamylase, beta-amylase, exo-alpha- 1,4-glucanase, or pullulanase.

122. The method of claim 90, wherein the one or more biocatalysts comprise at least one fermenting microorganism and at least one hydrolytic enzyme.

123. The method of claim 90, wherein the one or more biocatalysts comprise at least one fermenting microorganism that is a yeast or bacteria and at least one enzyme that hydrolyzes starch.

124. The method of claim 90, wherein the blended feedstock comprises less than 100 g/L monosaccharides prior to contacting with the one or more biocatalysts.

125. The method of claim 90, wherein the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides prior to contacting with the one or more biocatalysts.

126. The method of claim 90, wherein the first biomass and the one or more cellulosic derived C6 monosaccharides are combined in a ratio of from about 50:50 to 99:1 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume. -123- WO 2013/120035 PCT/US2013/025457

127. The method of claim 90, wherein the first biomass and the one or more cellulosic derived C6 monosaccharides are combined in a ratio of about 80:20 (first biomass: cellulosic derived C6 monosaccharides) by volume or by weight:volume.

128. The method of claim 90, wherein the first biomass and the one or more cellulosic derived C6 monosaccharides are combined in a ratio of about 90:10 (first biomass: cellulosic derived C6 monosaccharides) by volume or by weight:volume.

129. The method of claim 90, wherein the blended feedstock comprises from about 10% to about 50% solids from the first biomass.

130. The method of claim 90, wherein the blended feedstock comprises from about 20% to about 40% solids from the first biomass.

131. The method of claim 90, wherein the blended feedstock comprises from about 30% to about 36% solids from the first biomass.

132. The method of claim 90, wherein the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 10% to about 70% w/v prior to combining with the first biomass.

133. The method of claim 90, wherein the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 20% to about 50% w/v prior to combining with the first biomass.

134. A fermentation end-product produced by the method of claim 90.

135. The fermentation end-product of claim 134, wherein the fermentation end-product is ethanol.

136. A method of producing one or more fermentation end-products comprising: (a) combining a first biomass with one or more cellulosic-derived C6 monosaccharides to produce a blended feedstock in a broth; (b) contacting the blended feedstock with one or more biocatalysts; and (c) fermenting the first biomass and the one or more cellulosic-derived C6 monosaccharides for sufficient time to produce one or more fermentation end-products from the blended feedstock, wherein the one or more cellulosic-derived C6 monosaccharides are at a concentration that differs from a concentration of saccharides in the first biomass by less than +/ 50%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents.

137. The method of claim 136, wherein a yield of at least one of the one or more fermentation end-products is increased relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides. -124- WO 2013/120035 PCT/US2013/025457

138. The method of claim 136, wherein a yield of at least one of the one or more fermentation end-products is increased by about 1% to about 100% relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides.

139. The method of claim 136, wherein at least one of the one or more fermentation end-products is produced at a rate that is faster relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides.

140. The method of claim 136, wherein at least one of the one or more fermentation end-products is produced at a rate that is about 1% to about 100% faster relative to fermentation of the first biomass without the one or more cellulosic-derived C6 monosaccharides.

141. The method of claim 136, wherein the concentration of the one or more cellulosic-derived C6 monosaccharides differs from the concentration of saccharides in the first biomass by less than +/- 25%, wherein the concentration of saccharides in the first biomass is in monosaccharide equivalents.

142. The method of claim 136, wherein the one or more fermentation end-products comprise one or more alcohols.

143. The method of claim 136, wherein the one or more fermentation end-products comprise ethanol.

144. The method of claim 136, wherein the method is a fed-batch fermentation wherein the one or more cellulosic-derived C6 monosaccharides are added over time.

145. The method of claim 144, wherein the one or more cellulosic-derived C6 monosaccharides are added at a rate of from about 0.01 mL/min/L of broth to about 5 mL/min/L of broth during the fermenting.

146. The method of claim 136 or 144, wherein a yield of one or more other products is decreased relative to a non-fed batch fermentation.

147. The method of claim 146, wherein the yield of the one or more other products is decreased by about 1% to about 100% relative to the non-fed batch fermentation.

148. The method of claim 146, wherein the one or more other products comprise one or more polyols or sugar alcohols.

149. The method of claim 146, wherein the one or more other products comprise methanol, glycol, glycerol, erythritol, threitol, arabitol, xylitol, ribitol, mannitol, sorbitol, dulcitol, fucitol, iditol, inositol, volemitol, isomalt, maltitol, lactitol, polyglycitol, or a combination thereof.

150. The method of claim 146, wherein the one or more other products comprise glycerol. -125- WO 2013/120035 PCT/US2013/025457

151. The method of claim 136, wherein the first biomass comprises non-cellulosic sugars.

152. The method of claim 136, wherein the first biomass comprises non-cellulosic oligosaccharides.

153. The method of claim 136, wherein the first biomass comprises starch.

154. The method of claim 136, wherein the first biomass comprises corn, corn mash, sugar cane, sugar beets, sugar palms, sweet sorghum, nypa palm, cassava, rice, milo, sorghum, sweet potatoes, wheat, molasses, tubers, roots, stems, whole grains, barley, rye, milo, sago, cassaya, tapioca, rice peas, beans, potatoes, beets, fruits, or a combination thereof.

155. The method of claim 136, wherein the one or more cellulosic-derived C6 monosaccharides are produced from the pretreatment and/or hydrolysis of cellulose, hemicellulose, or lignocellulose material.

156. The method of claim 136, wherein the one or more cellulosic-derived C6 monosaccharides are produced by the pretreatment and/or hydrolysis of a second biomass comprising cellulose, hemicellulose, or lignocellulose.

157. The method of claim 156, wherein the second biomass comprises corn, corn syrup, corn stover, corn cobs, molasses, silage, grass, straw, grain hulls, bagasse, distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof.

158. The method of claim 136, wherein the one or more biocatalysts comprise one or more fermenting microorganisms.

159. The method of claim 136, wherein the one or more biocatalysts comprise one or more yeasts and/or one or more bacteria.

160. The method of claim 136, wherein the one or more biocatalysts comprise one or more yeasts.

161. The method of claim 136, wherein the one or more biocatalysts comprise one or more strains of Saccharomyces cerevisiae.

162. The method of claim 136, wherein at least one of the one or more biocatalysts is a genetically-modified yeast that ferments C5 and C6 saccharides.

163. The method of claim 136, wherein at least one of the one or more biocatalysts is a bacteria that hydrolyzes and/or ferments C5 and C6 saccharides. -126- WO 2013/120035 PCT/US2013/025457

164. The method of claim 136, wherein at least one of the one or more biocatalysts is a hydrolytic enzyme.

165. The method of claim 136, wherein the one or more biocatalysts comprise an endoglucanase, an exoglucanase, a cellobiohydrolase, a cellulase, a beta-glucosidase, a glycoside hydrolase, a glycosyltransferase, a lyase, an esterase, a glucamylase, or a combination thereof.

166. The method of claim 136, wherein at least one of the one or more biocatalysts is an enzyme that hydrolyzes starch.

167. The method of claim 136, wherein at least one of the one or more biocatalysts is an alpha-amylase, glucoamylase, beta-amylase, exo-alpha-1,4-glucanase, or pullulanase.

168. The method of claim 136, wherein the one or more biocatalysts comprise at least one fermenting microorganism and at least one hydrolytic enzyme.

169. The method of claim 136, wherein the one or more biocatalysts comprise at least one fermenting microorganism that is a yeast or bacteria and at least one enzyme that hydrolyzes starch.

170. The method of claim 136, wherein the blended feedstock comprises less than 100 g/L monosaccharides prior to contacting with the one or more biocatalysts.

171. The method of claim 136, wherein the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides prior to contacting with the one or more biocatalysts.

172. The method of claim 136, wherein the first biomass and the one or more cellulosic-derived C6 monosaccharides are combined in a ratio of from about 50:50 to 99:1 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume.

173. The method of claim 136, wherein the first biomass and the one or more cellulosic-derived C6 monosaccharides are combined in a ratio of about 80:20 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume.

174. The method of claim 136, wherein the first biomass and the one or more cellulosic-derived C6 monosaccharides are combined in a ratio of about 90:10 (first biomass: cellulosic-derived C6 monosaccharides) by volume or by weight:volume.

175. The method of claim 136, wherein the blended feedstock comprises from about 10% to about 50% solids from the first biomass.

176. The method of claim 136, wherein the blended feedstock comprises from about 20% to about 40% solids from the first biomass.

177. The method of claim 136, wherein the blended feedstock comprises from about 30% to about 36% solids from the first biomass. -127- WO 2013/120035 PCT/US2013/025457

178. The method of claim 136, wherein the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 10% to about 70% w/v prior to combining with the first biomass.

179. The method of claim 136, wherein the one or more cellulosic-derived C6 monosaccharides are at a concentration of from about 20% to about 50% w/v prior to combining with the first biomass.

180. A fermentation end-product produced by the method of claim 136.

181. The fermentation end-product of claim 180, wherein the fermentation end-product is ethanol.

182. A method of producing one or more fermentation end-products comprising: combining a first biomass with a C6-enriched hydrolysate to produce a blended feedstock; contacting the blended feedstock with one or more hydrolytic enzymes and/or one or more fermenting microorganisms; and fermenting the first biomass and the C6-enriched hydrolysate for a time sufficient to produce one or more fermentation end-products from the blended feedstock.

183. The method of claim 182, wherein the C6-enriched hydrolysate comprises monosaccharides produced from the pretreatment and/or hydrolysis of a second biomass.

184. The method of claim 182, wherein a yield of at least one of the one or more fermentation end-products is increased relative to fermentation of the first biomass without the C6-enriched hydrolysate.

185. The method of claim 182, wherein a yield of at least one of the one or more fermentation end-products is increased by about l% to about 100% relative to fermentation of the first biomass without the C6-enriched hydrolysate.

186. The method of claim 182, wherein a rate of production for at least one of the one or more fermentation end-products is increased relative to fermentation of the first biomass without the C6-enriched hydrolysate.

187. The method of claim 182, wherein a rate of production for at least one of the one or more fermentation end-products is increased by about l% to about 100% relative to fermentation of the first biomass without the C6-enriched hydrolysate.

188. The method of claim 182, 184, 185, 186, or 187, wherein the one or more fermentation end-products comprise one or more alcohols.

189. The method of claim 182, 184, 185, 186, or 187, wherein the one or more fermentation end-products comprise ethanol. -128- WO 2013/120035 PCT/US2013/025457

190. The method of claim 182, wherein a yield of one or more other products is decreased relative to fermentation of the C6-enriched hydrolysate without the first biomass.

191. The method of claim 182, wherein a yield of one or more other products is decreased by about 1% to about 100% relative to fermentation of the C6-enriched hydrolysate without the first biomass.

192. The method of claim 182, 184, 185, 186, 187, 190, or 191, wherein the one or more other products comprise one or more polyols or sugar alcohols.

193. The method of claim 182, 184, 185, 186, 187, 190, or 191, wherein the one or more other products comprise methanol, glycol, glycerol, erythritol, threitol, arabitol, xylitol, ribitol, mannitol, sorbitol, dulcitol, fucitol, iditol, inositol, volemitol, isomalt, maltitol, lactitol, polyglycitol, or a combination thereof.

194. The method of claim 182, 184, 185, 186, 187, 190, or 191, wherein the one or more other products comprise glycerol.

195. The method of claim 182, wherein the first biomass comprises non-cellulosic sugars.

196. The method of claim 182, wherein the first biomass comprises non-cellulosic oligosaccharides.

197. The method of claim 182, wherein the first biomass comprises starch.

198. The method of claim 182, wherein the first biomass comprises corn or corn mash, sugar cane, sugar beet, sugar palm, sweet sorghum, nypa palm, cassava, rice, milo, sorghum, sweet potato, wheat, molasses, or a combination thereof.

199. The method of claim 183, wherein the second biomass comprises cellulose, hemicellulose, or lignocellulose.

200. The method of claim 183, wherein the second biomass comprises corn, corn syrup, corn stover, corn cobs, molasses, silage, grass, straw, grain hulls, bagasse, distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof.

201. The method of claim 182, wherein the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 50%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers. -129- WO 2013/120035 PCT/US2013/025457

202. The method of claim 182, wherein the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 40%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers.

203. The method of claim 182, wherein the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 30%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers.

204. The method of claim 182, wherein the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 20%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers.

205. The method of claim 182, wherein the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 15%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers.

206. The method of claim 182, wherein the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 10%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers.

207. The method of claim 182, wherein the C6-enriched hydrolysate comprises less than about 50% C5 sugars.

208. The method of claim 182, wherein the C6-enriched hydrolysate comprises less than about 40% C5 sugars.

209. The method of claim 182, wherein the C6-enriched hydrolysate comprises less than about 30% C5 sugars.

210. The method of claim 182, wherein the C6-enriched hydrolysate comprises less than about 20% C5 sugars.

211. The method of claim 182, wherein the C6-enriched hydrolysate comprises less than about 10% C5 sugars.

212. The method of claim 182, wherein the C6-enriched hydrolysate comprises from about 0.1% to about 10% C5 sugars.

213. The method of claim 182, wherein the one or more fermenting microorganisms comprise one or more yeast strains, one or more bacterial strains, or a combination thereof. -130- WO 2013/120035 PCT/US2013/025457

214. The method of claim 182, wherein at least one of the one or more fermenting microorganisms is Saccharomyces cerevisiae.

215. The method of claim 182, wherein the one or more hydrolytic enzymes comprise an endoglucanase, an exoglucanase, a cellobiohydrolase, a cellulase, a beta-glucosidase, a glycoside hydrolase, a glycosyltransferase, a lyase, an esterase, a glucamylase, or a combination thereof.

216. The method of claim 182, wherein the blended feedstock comprises less than about 100 g/L monosaccharides prior to contacting with the one or more fermenting microorganisms and the one or more hydrolytic enzymes.

217. The method of claim 182, wherein the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides prior to contacting with the one or more fermenting microorganisms and the one or more hydrolytic enzymes.

218. The method of claim 182, wherein the first biomass and the C6-enriched hydrolysate are combined in a ratio of from about 50:50 to 99:1 by volume or by weight:volume.

219. The method of claim 182, wherein the first biomass and the C6-enriched hydrolysate are combined in a ratio of about 80:20 by volume or by weight:volume.

220. The method of claim 182, wherein the first biomass and the C6-enriched hydrolysate are combined in a ratio of about 90:10 by volume or by weight:volume.

221. A method of producing a C6-enriched hydrolysate comprising: treating a biomass comprising cellulose and hemicellulose and/or lignin to solubilize the hemicellulose and/or lignin; separating the solubilized hemicellulose and/or lignin from the cellulose; and hydrolyzing the cellulose, thereby producing the C6-enriched hydrolysate.

222. The method of claim 221, wherein the biomass comprising cellulose and hemicellulose and/or lignin comprises corn, corn syrup, corn stover, corn cobs, molasses, silage, grass, straw, grain hulls, bagasse, distiller's grains, distiller's dried solubles, distiller's dried grains, condensed distiller's solubles, distiller's wet grains, distiller's dried grains with solubles, wood, bark, sawdust, paper, poplars, willows, switchgrass, alfalfa, prairie bluestem, algae, fruit peels, pits, sorghum, sweet sorghum, sugar cane, switch grass, rice, rice straw, rice hulls, wheat, wheat straw, barley, barley straw, bamboo, seeds, seed hulls, oats, oat hulls, food waste, municipal sewage waste, or a combination thereof.

223. The method of claim 221, wherein the biomass comprises corn stover. -131- WO 2013/120035 PCT/US2013/025457

224. The method of claim 221, wherein the treating comprises stream treatment, hot water treatment, dilute acid treatment, dilute base treatment, steam explosion, acid-catalyzed steam explosion, or a combination thereof.

225. The method of claim 221, wherein the treatment comprises steam treatment.

226. The method of claim 221, wherein the treating is performed at a temperature of from about 175 to about 250 'C.

227. The method of claim 221, wherein the treating is performed at a temperature of about 205 'C.

228. The method of claim 221, wherein the treating is performed from about 1 minute to about 30 minutes.

229. The method of claim 221, wherein the treating is performed for about 7.5 minutes.

230. The method of claim 221, wherein the separating is performed using a filter press.

231. The method of claim 221, wherein the separating step comprises washing the biomass with water.

232. The method of claim 231, wherein the water is from about 25 to about 100 'C.

233. The method of claim 231, wherein the water is about 50 'C.

234. The method of claim 231, wherein the water is added in an amount from about 1 to about 5 L/kg of biomass (dry weight).

235. The method of claim 231, wherein the water is added in an amount of about 3 L/kg of biomass (dry weight).

236. The method of claim 221, wherein the hydrolyzing step comprises enzymatic hydrolysis with one or more enzymes.

237. The method of claim 221, wherein the hydrolyzing step is performed at a pH of from about 3 to about 7.

238. The method of claim 221, wherein the hydrolyzing step is performed at a pH of about 5.

239. The method of claim 221, wherein the hydrolyzing step is performed in a slurry of from about 1 % to about 20% wt/wt biomass/water.

240. The method of claim 221, wherein the hydrolyzing step is performed in a slurry of about 8% wt/wt biomass/water.

241. The method of claim 221, wherein the hydrolyzing step is performed in a jacketed reactor. -132- WO 2013/120035 PCT/US2013/025457

242. The method of claim 221, further comprising concentrating the C6-enriched hydrolysate.

243. The method of claim 242, wherein the C6-enriched hydrolysate is concentrated by evaporation.

244. The method of claim 242, wherein the C6-enriched hydrolysate is concentrated using a roto-evaporator.

245. The method of claim 242, wherein the C6-enriched hydrolysate is concentrated to a C6 sugar concentration of from about 100 g/L to about 500 g/L.

246. The method of claim 242, wherein the C6-enriched hydrolysate is concentrated to a C6 sugar concentration of about 300 g/L.

247. The method of claim 221, wherein the C6-enriched hydrolysate comprises less than about 50% C5 sugars.

248. The method of claim 221, wherein the C6-enriched hydrolysate comprises less than about 40% C5 sugars.

249. The method of claim 221, wherein the C6-enriched hydrolysate comprises less than about 30% C5 sugars.

250. The method of claim 221, wherein the C6-enriched hydrolysate comprises less than about 20% C5 sugars.

251. The method of claim 221, wherein the C6-enriched hydrolysate comprises less than about 10% C5 sugars.

252. The method of claim 221, wherein the C6-enriched hydrolysate comprises from about 0.1% to about 10% C5 sugars.

253. A C6-enriched hydrolysate produced by the method of any one of claims 221 252.

254. A method of producing ethanol comprising: combining a first biomass comprising starch with a C6-enriched hydrolysate to produce a blended feedstock, (i) wherein the C6-enriched hydrolysate comprises monosaccharides produced from the pretreatment and/or hydrolysis of a second biomass, (ii) wherein the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 20%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers, and -133- WO 2013/120035 PCT/US2013/025457 (iii) wherein the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides; contacting the blended feedstock with one or more fermenting microorganisms and one or more hydrolytic enzymes; and fermenting the first biomass and the C6-enriched hydrolysate to produce ethanol from the blended feedstock, wherein an increase rate of production and/or yield of the ethanol is achieved relative to the hydrolysis and fermentation of the first biomass without the C6-enriched hydrolysate.

255. A method of producing ethanol comprising: combining a first biomass comprising starch with a C6-enriched hydrolysate to produce a blended feedstock, (i) wherein the C6-enriched hydrolysate comprises monosaccharides produced from the pretreatment and/or hydrolysis of a second biomass, (ii) wherein the C6-enriched hydrolysate comprises monosaccharides at a concentration that differs from a concentration of sugars in the first biomass by less than about +/- 20%, wherein the concentration of sugars in the first biomass assumes complete hydrolysis to monomers, and (iii) wherein the blended feedstock comprises from about 1 g/L to about 100 g/L monosaccharides; contacting the blended feedstock with one or more fermenting microorganisms and one or more hydrolytic enzymes; and fermenting the first biomass and the C6-enriched hydrolysate to produce ethanol from the blended feedstock, wherein a yield of one or more polyols or sugar alcohols is decreased relative to fermentation of the C6-enriched hydrolysate alone.

256. The ethanol produced by the method of claims 254 or 255. -134-