Abstract:
A process is defined for the continuous steam pretreatment and fractionation of bagasse to produce a concentrated cellulose solid stream that is sensitive to enzymatic hydrolysis. Valuable chemicals are recovered by fractionating the liquid and vapor stream composed of hydrolysis and degradation products of the hemicellulose. Cellulosic derived glucose is produced for fermentation to biofuels. A hemicellulose concentrate is recovered that can be converted to value added products including ethanol.

Description:
CROSS REFERENCE TO RELATED APPLICATIONS 
     This application claims the benefit of priority of U.S. Provisional Patent Application No. 61/410,701 filed Nov. 5, 2010, the contents of which is incorporated herein by reference. 
    
    
     FIELD OF THE INVENTION 
     The present invention generally relates to the production of ethanol from lignocellulosic biomass and in particular to a process for extracting cellulose and hemicellulose from sugarcane bagasse. 
     BACKGROUND OF THE INVENTION 
     Concerns over high oil prices, security of supply and global warming have raised the demand for renewable energy. Renewable energy is energy produced from plant derived biomass. Renewable energy applications such as fuel ethanol are seen as a valuable contribution to the reduction in fossil fuel consumption. Public policies have supported the creation of a fuel ethanol industry largely based on the use of corn as a feedstock. The production of fuel ethanol helps to stabilize farm income and reduces farm subsidies. However, as demand increases for fuel ethanol, additional feedstocks such as lignocellulosic biomass are under consideration (1-3). 
     Fuel ethanol is created by the fermentation of starch derived sugars. The ethanol is distilled and dehydrated to create a high-octane, water-free gasoline substitute. Fuel ethanol is blended with gasoline to produce a hybrid fuel, which has environmental advantages when compared to gasoline alone, and can be used in gasoline-powered vehicles manufactured since the 1980&#39;s. Most gasoline-powered vehicles can run on a blend consisting of gasoline and up to 10 percent ethanol, known as “E-10” (4-10). 
     While corn is the major raw material for producing ethanol in North America, the dominant ethanol feedstock in warmer regions is sugarcane. It is already apparent that large-scale use of ethanol for fuel will require new technologies that will allow the industry to expand its feedstock options to include cellulose (4-10). 
     Cellulosic ethanol is manufactured from lignocellulosic biomass. Lignocellulosic biomass may be grouped into four main categories: (1) wood residues (including sawmill and paper mill discards), (2) municipal paper waste, (3) agricultural wastes (including corn stover, corn cobs and sugarcane bagasse), and (4) dedicated energy crops which are mostly composed of fast growing tall, woody grasses such as switch grass and Miscanthus (8-11). 
     Lignocellulosic biomass is composed of three primary polymers that make up plant cell walls: Cellulose, hemicellulose and lignin. Cellulose is a polymer of D-glucose. Hemicellulose contains two different polymers i.e. xylan, a polymer of xylose and glucomannan, a polymer of glucose and mannose. Lignin is a polymer of guaiacylpropane- and syringylpropane units (12-14). 
     Cellulose fibers are locked into a rigid structure of hemicellulose and lignin. Lignin and hemicelluloses form chemically linked complexes that bind water soluble hemicelluloses into a three dimensional array, cemented together by lignin. Lignin covers the cellulose microfibrils and protects them from enzymatic and chemical degradation. These polymers provide plant cell walls with strength and resistance to degradation, which makes lignocellulosic biomass a challenge to use as a substrate for biofuel production. Variation in the content or organization of these polymers significantly affects the overall steps of cellulosic ethanol production (12-14). 
     Cellulose or β-1-4-glucan is a linear polysaccharide polymer of glucose made of cellobiose units (12, 13). The cellulose chains are packed by hydrogen bonds in microfibrils (14). These fibrils are attached to each other by hemicelluloses, amorphous polymers of different sugars and covered by lignin. 
     Hemicellulose is a physical barrier which surrounds the cellulose fibers and protects cellulose against degradation. There is evidence that hemicellulose, containing xylose polymers (xylan), limits the activity of cellulolytic enzymes, thereby lowering cellulose to glucose conversion rates. (11-14). Thus for the production of fermentable sugars and ethanol, it is desirable to submit to the enzymatic hydrolysis a highly reactive cellulose low in xylan. 
     Lignin is a very complex molecule constructed of phenylpropane units linked in a three dimensional structure which is particularly difficult to biodegrade. Lignin is the most recalcitrant component of the plant cell wall. There are chemical bonds between lignin, hemicellulose and cellulose polymers. There is evidence that the higher the proportion of lignin, the higher the resistance to chemical and biological hydrolysis. Lignin and some soluble lignin derivatives inhibit enzymatic hydrolysis and fermentation processes (14, 15). Thus, it is desirable to use a lignocellulosic feedstock which is low in lignin. 
     The lignin content of bagasse is variable and ranges from low (10%) to high (25% by weight on a dry matter basis). The low lignin content of some bagasse residues makes this waste product a good biomass feedstock for the production of ethanol whereas high lignin bagasse is more suitable for cogeneration applications, in which bagasse is used as a fuel source to provide both heat energy, used in the mill, and electricity, which is typically sold on to the consumer electricity grid. 
     Published work on the various processes for the production of fermentable sugars from cellulosic biomass shows the existence of an inverse relationship between lignin content and the efficiency of enzymatic hydrolysis of sugar based polymers (16). Lignocellulosic microfibrils are associated in the form of macrofibrils. This complicated structure and the presence of lignin provides plant cell walls with strength and resistance to degradation, which also makes these materials a challenge to use as substrates for the production of biofuel and bioproducts. Thus, pretreatment is necessary to produce highly reactive cellulose that reacts well with catalysts such as enzymes (17). 
     Purified cellulose and lignin-free xylo-oligosaccharides are valuable for many purposes. Specifically, reactive cellulose extracted from biomass with low lignin content may be easily hydrolyzed to fermentable sugar monomers and then fermented to ethanol and other biofuels. Lignin-free xylo-oligosaccharides extracted from the hemicellulose fraction are valuable and may be easily used in the preparation of prebiotic substances for food and pharmaceutical applications. 
     The best method and conditions of pretreatment will vary and depend greatly on the type of lignocellulosic starting material used (18, 19). Pretreatment configuration and operating conditions must be adjusted with respect to the content or organization of lignocellulosic polymers in the starting material, to attain optimal conversion of cellulose to fermentable sugars (11). The cellulose-to-lignin ratio is the main factor. Other parameters to consider are the content of hemicellulose, degree of acetylation of hemicellulose, cellulose-accessible surface area, degree of polymerization and crystallinity (11). 
     An effective pretreatment should meet the following requirements: (a) production of reactive cellulosic fiber for enzymatic attack, (b) avoidance of cellulose and hemicelluloses destruction, and (c) avoidance of the formation of possible inhibitors for hydrolytic enzymes and fermenting microorganisms (17-20). 
     Several methods have been investigated for the pretreatment of lignocellulosic materials to produce reactive cellulose. These methods are classified into physical pretreatments, biological pretreatments and physicochemical pretreatments (21-22). 
     The prior art teaches that physical and biological pretreatments are not suitable for industrial applications. Physical methods such as milling, irradiation and extrusion are highly energy demanding and produce low grade cellulose. Also, the rates of known biological treatments are very low (11, 23-25). 
     Pretreatments that combine both chemical and physical processes are referred to as physicochemical processes (26). These methods are among the most effective and include the most promising processes for industrial applications. Hemicellulose hydrolysis is often nearly complete. As cellulose surface area increases, a decrease in cellulose degree of polymerization and crystallinity occurs. These changes greatly increase overall cellulose reactivity. Treatment rates are usually rapid (16-26). These pretreatment methods usually employ hydrolytic techniques using acids (hemicellulose hydrolysis) and alkalis for lignin removal (27-39). 
     The steam explosion process is well documented. Batch and continuous processes have been tested at laboratory and pilot scale by several research groups and companies (40-44). In steam explosion pretreatment, biomass is treated at high pressure, and high temperatures under acidic conditions i.e. 160° C. to 260° C. for 1 min to 20 min, at pH values&lt;pH 4.0 (21, 17-23). The pressure of the pretreated biomass is suddenly reduced, which makes the materials undergo an explosive decompression leading to defibrization of the lignocellulosic fibers (45-47). 
     Steam explosion pretreatment is not very effective in dissolving lignin, but it does disrupt the lignin structure and increases the cellulose susceptibility to enzymatic hydrolysis. Steam explosion pretreatment generally results in extensive hemicellulose breakdown and, to a certain extent, to the degradation of xylose and glucose (40-44). 
     Steam explosion pretreatment has been successfully applied to a wide range of lignocellulosic biomasses. Acetic acid, sulfuric acid or sulfur dioxide are the most commonly used catalysts (40-44). Dilute acid- or sulfur dioxide-catalyzed steam explosion pretreatments refer to the use of 0.1-1.0% diluted sulfuric acid or 0.5-4.0% sulfur dioxide (45-47). 
     In acid catalyzed pretreatment processes catalysts must be recycled or the prehydrolysate stream obtained must be diluted in order to reduce the concentrations of toxic and inhibitory compounds to an acceptable level with respect to cellulolytic enzymes and fermenting organisms. As a result, large amounts of water are required prior to the enzymatic hydrolysis step. This results not only in increased capital equipment cost (tankage) but also in increased operating cost by limiting the final ethanol titer, due to the dilution factor applied to the stream of biomass prehydrolysate, which then dramatically increases energy requirements and cost of distillation (11, 20, 45-47). 
     In the autohydrolysis process, no added acid is required to reach pH values below 4.0. Acetic acid is released during the breakdown of acetylated hemicellulose resulting from the high pressure steam applied to the biomass during the cooking stage. The degree of hemicellulose acetylation is variable among different sources of biomass (11, 41, 48). The hemicellulose content of bagasse is high. Much of the hemicellulose is acetylated, which means the breakdown and solubilization of the hemicellulose, which occurs during pretreatment, leads to the formation of acetic acid. 
     The presence of acetic acid reduces the need for acid catalysts, which is beneficial to the pretreatment process and resulting downstream processing. However, acetic acid is a powerful inhibitor of both the hydrolysis and the glucose fermentation process. Acetic acid remains in the pretreated biomass and carries through to the hydrolysis and fermentation steps. A process is desired that includes a pretreatment step carried out at a pH values &lt;pH 4.0 to maximize hemicellulose solubilization. However, after steam pretreatment, acetic acid and pre-treatment degradation products must be removed to enhance the digestibility of the cellulose in the enzymatic hydrolysis step and to enable a more rapid and complete conversion of glucose to ethanol in the fermentation step. 
     Pretreatment of lignocellulosic biomass is projected to be the single, most expensive processing step, representing about 20% of the total cost. Capital-intensiveness of lignocellulosic biomass pretreatment is a problem (49). Thus, a process is desired for efficient fractionation of lignocellulosic biomass into multiple streams that (i) contain value-added compounds and (ii) may significantly improve the overall economics of a biofuel production facility. 
     The growing commercial importance of xylo-oligosaccharides, non digestible sugar oligomers made up of xylose units, is based on their beneficial health properties; particularly the prebiotic activity and makes them good candidates as high value added bioproducts. Xylo-oligosaccharide mixtures from auto-hydrolysis of various agricultural residues exhibit a great prebiotic potential similar to commercially available xylo-oligosaccharide products (50-52). 
     As is apparent from the above discussion of known approaches, improving the overall ethanol yield and reducing enzyme usage or hydrolysis time are generally linked to increased operating costs. The increased costs may outweigh the value of the increased ethanol yield, rendering existing methods economically unacceptable. 
     SUMMARY OF THE INVENTION 
     It is now an object of the present invention to provide a process which overcomes at least one of the above disadvantages. 
     Compared to other biomass such as corncobs, the lower content of acetyl groups in bagasse, coupled with higher lignin content, make bagasse more difficult to pre-treat. For example, corncobs typically have acetyl groups in a concentration of about 4.6-5.5%, on a dry matter basis. Corncobs typically have a lignin content in the range of 4 to 7% on a dry matter basis. This is a lower lignin content than that of bagasse. Because of the concentration of acetyl groups and lignin, autohydrolysis can be achieved in corncobs without the addition of acid. 
     In contrast to corncobs, the concentration of acetyl groups in bagasse is typically in a range of about 3.2-3.5%, on a dry matter basis. Typically, bagasse has a lignin content of between 17 and 20%, which is up to five times the amount of lignin found in corncobs. Since bagasse has a lower content of acetyl groups and a higher content of lignin than that of corncobs, conventional processes to pretreat bagasse require the use of added mineral acid to assist with hydrolysis. However, the addition of mineral acid is disadvantageous as it catalyses the condensation of lignin which makes the cellulose less accessible to enzymatic hydrolysis. 
     The inventors have now surprisingly found that the use of mineral acid can be completely avoided during pretreatment of bagasse by carefully selecting treatment conditions that result in auto-hydrolysis pre-treatment. This was surprising and unexpected in view of the relatively lower content of acetyl groups and higher content of lignin in bagasse. In particular, the inventors surprisingly discovered that by controlling the conditions of temperature, pressure and treatment time an efficient pretreatment of bagasse biomass can be achieved without the need for acid addition. The inventors have further discovered that the amount of acetic acid in the prehydrolysate obtained can be reduced by closely controlling the treatment conditions during the pretreatment step. In particular, the inventors have unexpectedly found conditions of temperature, pressure and treatment time at which sufficient acetic acid is produced to pretreat the bagasse biomass by the process of autohydrolysis, while at the same time limiting the acetic acid content in the prehydrolysate to a level which does not cause any significant delays in the downstream fermentation process. 
     The inventors have also discovered that the catalytic activities of cellulolytic enzymes are specifically inhibited by soluble forms of hemicellulose i.e. soluble xylo-oligosaccharides and xylose. Products of hemicellulose decomposition released during bagasse pretreatment which remain in the pretreated biomass, and carry through to the hydrolysis and fermentation steps, can negatively affect enzymatic conversion of cellulose to glucose. 
     Thus, a novel process is described for the continuous steam explosion pretreatment of sugarcane bagasse wherein no mineral acid is added and the amount of acetic acid released in the pretreatment step is controlled to maximize the efficiency of the steam exposure step. 
     A sufficient residence time is provided to ensure proper breakdown/hydrolysis of the hemicellulose and activation of the cellulose fraction. 
     The steam explosion pretreated bagasse fibers are extracted under pressure prior to exiting the pretreatment reactor. Minimal water is used as an eluent to remove water soluble hemicellulose and cellulose degradation products such as, xylose, xylo-oligosaccharides, furans, fatty acids, sterols, ester, ethers and acetic acid. 
     The inventors have discovered that complete removal of the inhibitory compounds is neither required nor desirable for the achievement of the most economically viable pretreatment process. The inventors have identified a narrow range of extraction conditions for the removal of inhibitory compounds in which hemicelluloses and hemicellulose hydrolysis and degradation products and other inhibitors are still present, but reduced to a level where they have a much reduced inhibitory effect on the enzymes. In addition, the fractionation of the biomass still provides an economical amount of valuable hemicellulose. The extraction is achieved with a lower volume of eluent and level of dilution making the process much more cost effective. In effect, the extraction cost is significantly less than the value of the increased ethanol yield, lower enzyme dosages, and the reduced processing times achieved. When combined with the ideal pretreatment temperature, time and purging of impurities, an economical process to convert bagasse to fermentable sugar is achieved. 
     A further important feature of our new process is the continual extraction of a liquid purge from the pretreatment process. This purge increases hemicellulose recovery by minimizing the formation of furfural from monomeric sugars released during pretreatment. The liquid purge from the pretreatment system is combined with the extracted hemicellulose. Extraction refers in general to a single or multiple step process of removing liquid portions from the fibers with or without addition or utilization of an eluent, (the diluting step) Typically the extraction is enhanced by use of a mechanical compressing device such as a modular screw device. The eluent can be recycled to increase the economy of its use or used for example in the known process of counter current washing as an example. Liquefied components in the steam treated lignocellulosic biomass and the dissolved components are subsequently removed from the fibrous solids. Generally this removes most of the dissolved compounds, the wash water, primarily consisting of hemicellulose hydrolysis and degradation products that are inhibitory to downstream hydrolysis and fermentation steps. 
     The extracting system in general uses a device that employs a mechanical pressing or other means to separate solids from liquid or air from solids. This can be accomplished under pressure as described above and/or under atmospheric pressure accomplished with several different types of machines that vary and the detail of which is not essential to this invention. 
     The extract stream containing the xylo-oligosaccharide fraction is combined with the liquid purge from the pretreatment system. The combined stream is collected and concentrated to the desired dryness for further applications. A final refining step is required for producing xylo-oligosaccharides with a degree of purity suitable for pharmaceuticals, food and feed, and agricultural applications. Vacuum evaporation can be applied in order to increase the concentration and simultaneously remove volatile compounds such as acetic acid and flavors or their precursors. Solvent extraction, adsorption and ion-exchange precipitation have been proposed by those skilled in the art. 
     A balance is preferably maintained between the removal of the water soluble components (xylo-oligosaccharide fraction) and the need to minimize the amount of washing/eluent water added. It is desirable to minimize water use, as the xylo-oligosaccharide fraction must be concentrated for its eventual use, which requires equipment and energy, both of which must be minimized. 
     In addition, the economics of ethanol production demand the maximization of the value in all the byproduct streams from the process. As an example, acetic acid may be recovered for sale as an industrial chemical. Also, xylo-oligosaccharides, (non digestible sugar oligomers made up of xylose units), have beneficial health properties; particularly their prebiotic activity. This makes them good candidates as high value added bioproducts. 
     In the new process, pressurized activated cellulose is flashed into a cyclone by rapidly releasing the pressure to ensure an explosive decompression of the pretreated bagasse into fibrous solids and vapors. This opens up the fibers to increase accessibility for the enzymes. Purified cellulose with a low level of residual hemicellulose can be sent to the hydrolysis and fermentation stages. 
     In one aspect, the invention provides a continuous process for fractionation of sugarcane bagasse biomass, comprising the steps of: a) subjecting the bagasse biomass to auto-hydrolysis treatment without the addition of acid by exposing the bagasse biomass to steam at a preselected temperature of between 170 and 220° C. and a preselected reaction pressure of between 100 and 322 psig, for a preselected exposure time of between 5 to 90 minutes, to remove a desired amount of a hemicellulose fraction from the bagasse biomass and activate a cellulose fraction of the bagasse biomass to obtain a pre-hydrolyzed bagasse biomass; and during the exposing step at the preselected temperature and reaction pressure i) continually purging liquid condensate and vapor formed to remove and collect a first liquid stream including water soluble compounds and a first vapor stream including volatile chemicals; b) selectively extracting at the preseleted reaction pressure from the pre-hydrolysed bagasse biomass containing hemicellulose hydrolysis and degradation components; c) rapidly releasing the preselected reaction pressure after the extracting step for explosive decompression of the pre-hydrolyzed bagasse into pretreated fibrous solids, vapor and condensate; and d) collecting the vapor and condensate from the explosive decompression for separation and recovery of byproducts. 
     Preferably, the bagasse biomass has a moisture content of 50% to 70%, and is pre-heated to a temperature of about 100° C. for a minimum of about 10 minutes prior to pretreatment. 
     More preferably, the moisture content is 70%. 
     A further feature of this new process is the removal of toxic compounds prior to pretreatment by the addition of a mechanical squeezing step prior to pretreatment which improves fermentation by removing extractives found in the biomass. Preferably, the pre-heated bagasse is squeezed from atmospheric pressure to a selected pressure required for pre-treatment while removing a stream of extractives. 
     Preferably, the liquid from the pretreatment purge stream is blended with the liquid extracted from the prehydrolysed bagasse biomass. 
     Preferably, the preselected exposure time and preselected temperature are selected to achieve a severity index of 3.88 to 4.11. More preferably, the severity index is 4.0. Preferably, the preselected temperature is between 190 and 210° C., the preselected pressure is between 165 and 260 psig, and the preselected exposure time is between 7 and 10 minutes. More preferably, the preselected temperature is about 205° C., the preselected pressure is about 235 psig and the preselected exposure time is about 8 minutes. 
     Preferably, the bagasse biomass is washed and subsequently separated from the dissolved hemicellulose and lignin free xylo-oligosaccharides and remaining inhibitory chemicals prior to explosive decompression. 
     Preferably, the bagasse biomass is washed under a steam pressure that ranges from 100 psig to 290 psig prior to the step of explosive decompression. Preferably, the pretreated fibrous solids are washed with water. 
     Preferably, the washed fibrous solids are separated from the wash water by a separation process selected from the group consisting of compressing, filtering, centrifuging, and combinations thereof. Preferably, the washing is counter current washing. The wash water is preferably recycled wash water. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
       Other objects and advantages of the invention will become apparent upon reading the detailed description and upon referring to the drawings in which: 
         FIG. 1  shows a process diagram of the continuous pretreatment unit proposed in the example. 
         FIG. 2  shows the total percentage recovery of cellulose and hemicellulose produced over the fractionation of bagasse. 
         FIG. 3  illustrates the susceptibility of pre-treated cellulose from bagasse to enzymatic hydrolysis (cellulose to glucose conversion) and fermentability of hydrolyzed cellulose (glucose to ethanol conversion). 
     
    
    
     Table 1 shows cellulose to glucose conversion times of 12% consistency bagasse hydrolysate at various levels of digestion versus severity index for bagasse biomass. 
     Hydrolysis was carried out at 50° C., pH 5.0 and 0.4% enzyme load. 
     Pre-treatment of bagasse was carried out at pilot scale (500 kg per day). 250 liter hydrolysis of bagasse pre-hydrolysate was carried out at 12% consistency, 50° C., pH 5.0 and 0.4% enzyme load. Fermentation of bagasse hydrolysate was carried out at 33° C., pH 5.3 using an industrial grade C6-fermenting yeast. 
     Hydrolysis and fermentation pH adjustment was carried out using liquid ammonia (30%). Grey circles indicate glucose concentration. Black squares indicate ethanol concentration. 
     DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS 
     Before explaining the present invention in detail, it is to be understood that the invention is not limited to the preferred embodiments contained herein. The invention is capable of other embodiments and of being practiced or carried out in a variety of ways. It is to be understood that the phraseology and terminology employed herein are for the purpose of description and not of limitation. 
     The abbreviations used in the figures have the following meaning:
     ° C., temperature in degree Celsius   ms, millisecond   DM, Dry matter   

     SI, Severity index 
     PRE-TREATMENT OF SUGARCANE BAGASSE 
     This invention is a new process for fractionating lignocellulosic biomass from bagasse into two main components, specifically a cellulose-rich corncob fibre and a xylo-oligosaccharides-rich solution. The cellulose-rich component is valuable for many purposes. Specifically it may be more easily hydrolyzed to glucose which in turn may be more easily fermented to ethanol or other biofuels than in previous processes. 
     A preferred aspect of the invention is a continuous process for the pretreatment of bagasse that generates highly reactive cellulose prehydrolysate with a reduced content of compounds which have an inhibiting effect on cellulose hydrolysis and glucose fermentation. 
     Another preferred aspect of the invention is a process for the pretreatment of bagasse, for generating a lignin free solution of xylo-oligosaccharides with a ratio of xylo-oligosaccharide to acetic acid and volatile compounds from hemicellulose degradation of greater than 4. 
     The preferred process of the invention includes the steps of pre-steaming ground, preheated bagasse fibers to add moisture and remove air. This is followed by a pressurized squeezing step that removes a certain quantity of toxic extractives. Next the pre-steamed, squeezed biomass is pretreated at 170° C. to 220° C. at 100 to 322 psig for 5 to 90 minutes without the use of mineral acid catalysts. The pretreatment preferably includes the continuous purging of volatile and liquid compounds. The exposing step preferably steam treats the biomass to a temperature and hold time for a Severity Index of 3.8 SI to 4.1, the Severity Index being calculated according to the equation:
 
Severity Index=Log×Exp{(Temperature ° C.−100)/14.75)×Retention Time (min).
 
     The exposing step most preferably has a severity index of 4.0. 
     The exposing of bagasse to a severity index of 4.0 leads to a final pH of 3.5 to 4.0. 
     The process also includes extraction of the steam treated fibers with/or without eluent addition under pressure to remove water soluble hemicelluloses, acids and hemicellulose and cellulose degradation products. As an option these inhibitors may be extracted after pretreatment or both during and after. The extraction of the soluble biomass from the fiber preferably results in 4% to 10% xylose based sugars consisting of monomers and oligosaccharides remaining in the pre-hydrolysis fibers. 
     The hemicellulose rich extract is combined with the liquid purge from pretreatment that contains an additional amount of hemicellulose extracted under pressure. 
     The extracted fibers, also referred to as prehydrolysate, are separated from the gaseous reaction products in a cyclone separator, collected at the bottom of the separator, then shredded and diluted to the desired consistency and subsequently transported to the enzymatic hydrolysis step. 
     The prehydrolysate is diluted with water to 10-30% consistency and then reacted with cellulase enzymes to produce glucose. The glucose rich solution is readily utilized in the subsequent fermentation step where an organism converts the glucose into ethanol. 
     EXAMPLE 
     In the following example, reference numbers refer to features of the pre-treatment system and process streams, as shown in  FIG. 1 . 
     Continuous steam explosion pretreatment of bagasse is carried out in a continuous steam gun explosion pretreatment system ( FIG. 1 ). 
     50% to 70% moisture bagasse fibers ( 10 ) are received and fed through a V shaped hopper and screw auger (not shown) using a feed rate of 40 kg bagasse fibers per hour on a dry matter basis. 
     Bagasse fibers are preheated with live steam ( 20 ) at atmospheric pressure, in a holding bin or pre-heating and conditioning container ( 30 ) to a temperature of 95-100° C. for about 10-60 min. Moisture content is adjusted to 75-80%. Air and steam are vented through an air vent ( 35 ) from the pre-heating and conditioning container ( 30 ). 
     Preheated bagasse fibers are compressed in a first modular screw device ( 40 ) to remove air ( 50 ) through an air vent and inhibitory extracts ( 55 ). The bagasse fibers are then fed into a pressurized upflow tube ( 70 ). 
     Pressurized saturated steam at temperatures of 205° C. is injected upstream of and/or into the up flow tube ( 70 ) by direct injection ( 60 ) and/or indirect injection of steam ( 61 ) in a jacketed section of the up flow tube until the desired cooking pressure is reached. 
     Bagasse fibers are moved through the up flow tube with the aid of a screw conveyor/mixer (3 min) and are discharged into the pretreatment reactor ( 80 ). 
     Bagasse fibers are continuously discharged from the pretreatment reactor to a second pressurized modular screw device ( 100 ) after a residence time of 5 min at 205° C. in the pretreatment reactor ( 80 ). 
     During the residence time, condensate and cooking liquids collected at the bottom of the pre-treatment reactor are purged through purge discharge control valve ( 95 ). 
     Pretreated bagasse fibers are washed with water under pretreatment pressure. Hot water ( 90 ) is added to dilute the pretreated bagasse as the fibers are discharged from the pretreatment reactor. Further hot water is also added along the pressing device ( 100 ) to reach a ratio of about 6:1 wash water to bagasse and achieve a greater extraction of hemicellulose. The extracted hemicellulose solution ( 110 ) is collected, combined with the hemicellulose stream from the liquid purge and concentrated to the desired dryness for further applications. 
     The pressurized washed bagasse fibers are flashed into a cyclone ( 120 ). The solids i.e. purified cellulose collected at the bottom of cyclone separator are subjected to further processing i.e. shredded and then diluted with fresh water to the desired consistency for hydrolysis and fermentation. 
     The gaseous components are collected, condensed ( 130 ) and fed to the condensate tank. Any gaseous emissions from the steam gun, the cyclone separator and other parts of the setup are collected and treated in an environmental control unit (not shown). Cleaned gases are exhausted to atmosphere from the environmental control unit. 
     Screening of bagasse pre-treatment optima was carried out at pilot scale using 0.4% load of a commercial mixture of cellulase and hemicellulase enzymes on a dry matter basis. 
     Pre-treatment of bagasse fibers carried out with a severity index of 4.0 SI led to the production of the most digestible bagasse pre-hydrolysates. Severity of 4.0 let to the shortest times to reach 50% to 90% of the maximum theoretical cellulose to glucose conversion (See Table 1). 
     Extracted cellulose from continuous pilot scale pre-treatment was highly susceptible to enzymatic hydrolysis. 80% of the maximum theoretical cellulose to glucose conversion was achieved in 111 hours using only 0.3% load of commercial enzyme product (Table 1). 
     Cellulose extraction from bagasse was carried out at pilot scale with a percentage recovery of 98% ( FIG. 2 ). The content of inhibitory compounds in the extracted cellulose was less than 1% (w/w, DM) acetic acid and no furans were detected prior to or following enzymatic hydrolysis and fermentation. 
     63% of the incoming hemicellulose was recovered in a soluble form in the lignin free xylo-oligosaccharides solution consisting of a blend of the purge from the pretreatment step and the hemicellulose rich stream from the extraction stage. ( FIG. 2 ). 85% of the hemicellulose sugars were recovered in an oligomeric form. 
     Samples of the continuously pre-treated bagasse were hydrolyzed and fermented in a 250 liter fed batch hydrolysis and fermentation trial ( FIG. 3 ). The results were in accordance with laboratory scale results (Table 1). A concentration of 54 g/L glucose was reached when 80% of the maximum theoretical cellulose to glucose conversion was achieved i.e. 110 hours hydrolysis of 13% consistency slurry, using only 0.3% dm load of commercial cellulases product. 
     The fermentability of the hydrolyzed cellulose was high. A concentration of 2.6% (w/v) alcohol was reached in 20 hours ( FIG. 3 ). This is equivalent to a glucose to ethanol conversion yield of 95%. 
     Samples of biomass were analyzed at each step of the process using the following analytical methods: 
     Dry matter: DM determination was carried out by incubating solid (1 g to 2 g) and liquid (5 g to10 g) samples at 130° C. for a period of 16 h to 24 h. 
     HPLC analysis: Quantification of soluble products in liquid samples and slurry was carried out by High Performance Liquid Chromatography analysis (HPLC). The HPLC system used was an AGILENT 1200 Series equipped with a cation exchange column HPX 87H from BioRad, a refractive index detector and an isocratic pump. Samples i.e. liquid, slurry and solid in suspension were centrifuged, filtered and diluted using 0.02 N sulfuric acid also used as eluent. 
     The target molecules were sugar monomers such as glucose and xylose as well ethanol, toxic compounds such as different carboxylic acids, namely acetic acid, succinic acid and lactic acid and degradation products of carbohydrates such as HMF and furfural. Concentration of fermentation by product such as glycerol is also measured. 
     Elemental analysis and wet chemistry analysis of samples (lignin, protein, fat, ash, Non fiber carbohydrate) was carried out by an external laboratory (DairyOne). Internal controls i.e. samples with known composition and duplicate samples are included in set of samples sent for analysis. 
     Carbohydrate composition analysis of samples was carried out using a modified TAPPI method T249 and a GC 7890A from Agilent equipped with a column DB225 from Agilent. Briefly, the method is modified beginning with the alkination step. Instead of using barium hydroxide (as required by the TAPPI method), ammonium hydroxide is used. The acetylation step is altered by using a catalyst (1-methyl imidazole) and a larger volume of acetic anhydride than is required by the TAPPI method T249. 
     
       
         
               
             
               
               
               
               
               
               
               
               
               
               
               
             
               
               
               
               
               
               
               
               
               
               
               
             
           
               
                 TABLE 1 
               
             
             
               
                   
               
               
                 Conversion Time (hours) 
               
             
          
           
               
                   
                 Severity Index (SI) 
                 3.35* 
                 3.55** 
                 3.64 
                 3.79 
                 3.85 
                 3.99 
                 4.08 
                 4.29 
                 4.56 
               
               
                   
                 Temperature (° C.) 
                 190 
                 190 
                 200 
                 205 
                 200 
                 205 
                 215 
                 215 
                 215 
               
               
                   
                 Time (min) 
                 5 
                 8 
                 5 
                 5 
                 8 
                 8 
                 5 
                 8 
                 15 
               
               
                   
                   
               
             
          
           
               
                 Conversion 
                 50 
                 &gt;200 
                 &gt;200 
                 56 
                 35 
                 30 
                 25 
                 32 
                 38 
                 48 
               
               
                 (%) 
                 60 
                 &gt;200 
                 &gt;200 
                 110 
                 62 
                 52 
                 44 
                 55 
                 58 
                 61 
               
               
                   
                 70 
                 &gt;200 
                 &gt;200 
                 &gt;200 
                 118 
                 84 
                 66 
                 88 
                 84 
                 90 
               
               
                   
                 80 
                 &gt;200 
                 &gt;200 
                 &gt;200 
                 &gt;200 
                 178 
                 111 
                 126 
                 140 
                 157 
               
               
                   
                 90 
                 &gt;200 
                 &gt;200 
                 &gt;200 
                 &gt;200 
                 &gt;200 
                 200 
                 &gt;200 
                 &gt;200 
                 &gt;200 
               
               
                   
               
               
                 *20% conversion were reached in 100 hours 
               
               
                 **30% conversion were reached in 100 hours 
               
             
          
         
       
     
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