Patent Application
20130017589
The present invention generally relates to the production of ethanol from lignocellulosic biomass and in particular to a process for extracting cellulose and hemicellulose fractions from low lignin containing biomass.
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.
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's. Most gasoline-powered vehicles can run on a blend consisting of gasoline and up to 10 percent ethanol, known as “E-10”.
While corn is the major raw material for producing ethanol in North America, 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.
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.
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.
In lignocellulosic biomass, 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. The cellulose is present as microfibrils. The lignin covers the cellulose microfibrils and protects them from enzymatic and chemical degradation. These polymers provide plant cell walls with strength, but also provide resistance to degradation, which makes lignocellulosic biomass a challenge to use as a substrate for biofuel production. Relatively small variations in the content or organization of these polymers from biomass to biomass generate significant differences in the results of conventional biomass treatment processes. A large number of different processes are therefore used for cellulosic ethanol production from lignocellulosic biomass.
Cellulose, or poly-1-4-glucan, is a linear polysaccharide polymer of glucose made of cellobiose units. The cellulose chains are packed by hydrogen bonds into microfibrils. These fibrils are attached to each other by the hemicelluloses and are covered by the lignin.
Hemicellulose is a physical barrier which surrounds the cellulose fibers and protects cellulose against degradation. Moreover, hemicellulose also has a chemical protection effect, since there is evidence that hemicellulose, containing xylose polymers (xylan), limits the activity of cellulolytic enzymes. This chemical inhibition has a negative effect on cellulose to glucose conversion rates. Thus for the production of fermentable sugars and ethanol from cellulose, it is desirable to generate a highly reactive cellulose with a low xylan content for the enzymatic hydrolysis to the fermentable sugars.
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 have been found to inhibit enzymatic hydrolysis and fermentation processes. Thus, it is desirable to generate a highly reactive cellulose which low in xylan content and low in lignin content.
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. Lignocellulosic microfibrils are associated in the form of macrofibrils. This complicated structure and the presence of lignin provide 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 reacting well with catalysts such as enzymes.
The products resulting from pretreatment, such as 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.
It is generally accepted in the field that the best pretreatment method and conditions will depend greatly on the type of lignocellulosic starting material used. Pretreatment configuration and operating conditions must be adjusted with respect to the content or organization of the above discussed lignocellulosic polymers in the starting material, if one is to attain optimal conversion of cellulose to fermentable sugars. The cellulose-to-lignin ratio is the main factor. However, other parameters which play a significant role are the content of hemicellulose, degree of acetylation of hemicellulose, cellulose-accessible surface area, degree of polymerization and crystallinity. For example, the lignin content of corncobs and certain hybrids of Miscanthus for example, is similarly low i.e. 5% to 10%. Yet, their contents of cellulose and hemicellulose are very different with the ratios of cellulose:lignin:hemicellulose for Corncobs and Miscanthus being 8:1:7 and 5:1:2, respectively. Thus, despite their similar lignin contents, Corncobs and Miscanthus are generally subjected to significantly different pre-treatment conditions. It is this variability in the required pre-treatment conditions from biomass to biomass, which makes it very difficult to develop an efficient process for use with different biomasses, or more importantly, biomass mixtures. A single process for the efficient treatment of biomass mixtures would of course be desirable, since that would obviate the need to supply only a specific biomass or an assorted biomass stream for ethanol production.
An effective pretreatment should: (a) produce reactive cellulosic fiber for enzymatic attack, (b) minimize destruction of cellulose and hemicelluloses, and (c) minimize the formation of inhibitors for hydrolytic enzymes and fermenting microorganisms.
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.
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.
Pretreatments that combine both chemical and physical processes are referred to as physicochemical processes. These methods are among the most effective and include the most promising processes for industrial applications. Hemicellulose hydrolysis and lignin removal are often nearly complete. Increase in cellulose surface area, decrease in cellulose degree of polymerization and crystallinity greatly increase overall cellulose reactivity. Treatment rates are usually rapid. These pretreatment methods usually employ hydrolytic techniques using acids (hemicellulose hydrolysis) and alkalis for lignin removal.
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. 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<pH 4.0. The pressure of the pretreated biomass is suddenly reduced, which makes the materials undergo an explosive decompression leading to defibrization of the lignocellulosic fibers.
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.
Steam explosion pretreatment has been successfully applied on a wide range of lignocellulosic biomasses. Acetic acid, sulfuric acid or sulfur dioxide are the most commonly used catalysts.
In one variant of steam explosion pretreatment process, the autohydrolysis process, no acid is added to the biomass, as long as pH values below 4.0 are achieved in the pretreatment process. This is made possible by the release of acetic acid during the breakdown of acetylated hemicellulose resulting from the high pressure steam applied to the biomass during the cooking stage. However, the degree of hemicellulose acetylation is variable among different sources of biomass, which again makes it difficult to develop a single set of process conditions useful for different biomasses. The hemicellulose content of corncobs is high, much of the hemicellulose in corncobs is acetylated. It is therefore relatively easy to achieve a pH value below 4.0 in the pretreated biomass, which means the breakdown and solubilization of the hemicellulose for release of the cellulose is achieved without acid addition. Thus, one could theorize that other biomasses could be treated equally well if acetic acid were added in an amount sufficient to achieve a pH of 4.0 in the treated biomass.
That however does not hold true, for example, for the pretreatment of Miscanthus, which does not have a high degree of acetylation. To achieve a degree of hemicellulose hydrolysis similar to that of the autohydrolysis pretreatment process for highly acetylated biomass, such as corncobs, Miscanthus requires the addition of sufficient acid prior to the steam heating process to reach a pH of 2.0.
Consequently, although the presence of acetic acid in the biomass reduces the need for acid catalysts most known steam explosion pretreatment processes require the use of an acid catalyst. Yet, mineral acids, acetic acid and other carboxylic acids are all powerful inhibitors of the cellulose hydrolysis process as well as the glucose fermentation process. Mineral and carboxylic acids added during pretreatment often remain in the pretreated biomass and carry through to the hydrolysis and fermentation steps, decreasing the efficiency of the overall process. In addition, although acids may be used to catalyze the hydrolysis of hemicellulose, they also lead to the unwanted decomposition of the sugars released in the process, thereby reducing the value of the decomposition products obtained during pretreatment. Moreover, those sugar breakdown products may also have an inhibitory effect on downstream hydrolysis and fermentation processes. Consequently, washing of the cellulose prior to the cellulose hydrolysis step must be used to remove residual acids and inhibitory components generated by the action of the acid catalysts, which renders the overall process inefficient.
It is now an object of the present invention to provide a process which overcomes at least one of the above disadvantages.
The inventors have now surprisingly discovered, that the most important treatment conditions during pretreatment for the achievement of autohydrolysis of acetyl group containing biomasses are neither the pH of the treated biomass, which means the amount of added acid catalyst, nor the type of acid catalyst used, but rather the severity (temperature/pressure and residence time) of the steam treatment. Moreover, the inventors have surprisingly discovered, that any biomass with a lignin content below 12% by weight on a dry matter basis and an acetyl group content of 3-6% by weight on a dry matter basis can be subjected to autohydrolysis without the addition of any acid catalyst, thereby minimizing the amount of residual acid in the pretreated biomass. In particular, the inventors have surprisingly discovered that all those types of biomass can be successfully treated to achieve highly digestible cellulose by using exactly the same steam pretreatment conditions, namely steam pretreatment conditions which result in a severity index of about 4.
The inventors surprisingly discovered that using steam pretreatment conditions resulting in a severity index of about 4 will result in a cellulose of equal digestibility for biomasses of such diverse content as corncobs (8:1:7, cellulose:lignin:hemicellulose) and bagasse (1.8 :1:1.3), without the addition of any acid catalyst and without controlling the amount of acetic acid released in the pretreatment step as long as the lignin content of the biomass is below 12% and the biomass has an acetyl group content of 3-6% by weight on a dry matter basis.
The inventors have discovered that for these types of biomass (acetyl group content of 3-6%) the detrimental effect of the hemicellulose breakdown products generated by the addition of acid catalysts during pretreatment on the catalytic activities of cellulolytic enzymes outweighs the benefits of increased hemicellulose breakdown and cellulose release. In other words, it would appear that products of hemicellulose decomposition released during biomass pretreatment which remain in the pretreated biomass and carry through to the hydrolysis and fermentation steps, can have a stronger negative effect on enzymatic conversion of cellulose to glucose than a less complete hydrolysis of hemicellulose during autohydrolysis due to a lower acetyl group content in the biomass.
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.
The inventors have not only discovered a single pretreatment process useful for a range of different biomasses, but an autohydrolysis process that generates cellulose having the same digestibility as cellulose obtained from corncobs, the biomass previously believed to have the best acetyl group content for autohydrolysis.
When this process is then combined with the steps of purging impurities during steam pretreatment and liquid extraction of inhibitory substances resulting from the hemicellulose autohydrolysis prior to cellulose hydrolysis, an economical process to convert low lignin lignocellulosic biomasses to fermentable sugar is achieved.
In addition, the economics of ethanol production demand the maximization of the value in all the byproduct streams from the process. As an example, 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. The xylo-oligosaccharides mixture derived from corncob autohydrolysis exhibits prebiotic potential similar to commercially available xylo-oligosaccharide products.
In summary, a process is described for the continuous steam explosion pretreatment of biomass with a lignin content below 12% and an acetyl group content of 3-6% weight/weight on a dry matter basis by autohydrolysis of the biomass at a severity index of about 4, without the addition of any acid catalyst and without controlling the amount of acetic acid released in the pretreatment step or the pH of the treated biomass.
Preferably, the pretreated biomass is extracted prior to cellulose hydrolysis, which means either while still under pressure prior to exiting the pretreatment reactor or after exiting the reactor, or both. 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). Minimal water is preferably used as an eluent to remove water soluble hemicellulose and cellulose degradation products generated during autohydrolysis, such as, xylose, xylo-oligosaccharides, furans, fatty acids, sterols, ester, ethers and acetic acid. The extraction can be 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 preferably 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 collected and preferably concentrated to the desired dryness for further applications. A final refining step may be 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.
The biomass is preferably chopped or ground and preheated with live steam at atmospheric pressure prior to the pretreatment step. Air is preferably removed from the biomass by pressing. Liquefied inhibiting extracts can be removed at this time. As mentioned above, no acid for catalyzing the breakdown/hydrolysis of the hemicellulose is added. However, the biomass is cooked with steam at elevated temperatures and pressures for a preselected amount of time to achieve a severity index of about 4, which means 3.9 to 4.1. During the pretreatment purging of condensate and venting of volatiles is preferably carried out continuously.
The pressurized activated cellulose is preferably flashed into a cyclone by rapidly releasing the pressure to ensure an explosive decompression of the pretreated biomass into fibrous solids and vapors. This opens up the fibres to increase accessibility for the enzymes. Purified cellulose with a low level of residual hemicellulose can be sent to the hydrolysis and fermentation stages.
Other objects and advantages of the invention will become apparent upon reading the detailed description and upon referring to the drawings in which:
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:
This invention is a new process for fractionating lignocellulosic biomass with a lignin content below 12% by weight on a dry matter basis and an acetyl group content of 3-6% by weight on a dry matter basis, in particular a process for fractionating the lignocellulosic biomass into two main components, a cellulose-rich fraction and a xylo-oligosaccharides-rich solution. The cellulose-rich component is valuable for many purposes, since it can be more easily hydrolyzed to glucose and in turn 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 these types of lignocellulosic biomass solely by autohydrolysis, in the absence of any acid catalyst, thereby minimizing the amount of residual acid in the pretreated biomass. In particular, all those types of biomass are treated in accordance with the invention by using exactly the same steam pretreatment conditions to achieve highly digestible cellulose, namely steam pretreatment conditions which result in a severity index of about 4. This not only makes it possible to use the same process equipment for different types of biomass, thereby significantly lowering the capital cost for plants intended to treat different biomasses, but also allows for the treatment of a mixture of biomasses, thereby providing much wider access to a larger amount of biomass sources.
The inventors discovered that using steam pretreatment without the addition of any acid catalyst and without controlling the amount of acetic acid released in the pretreatment step and solely at conditions resulting in a severity index of about 4 will result in a cellulose of equal digestibility for biomasses of such diverse content as corncobs (8:1:7, cellulose:lignin:hemicellulose) and bagasse (1.8 :1:1.3), as long as the lignin content of the biomass is below 12% and the biomass has an acetyl group content of 3-6% by weight on a dry matter basis.
The preferred process of the invention includes the steps of exposing ground, lignocellulosic biomass (<12% lignin and 3-6% acetic acid by weight in the dry matter) to steam at 170° C. to 220° C. at 100 to 322 psig for 2 to 300 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 with translates into a Severity Index of 3.9 to 4.1, most preferably about 4, the Severity Index being calculated according to the equation:
Severity Index=Log×Exp [(Temperature ° C.−100)/14.75]×Retention Time (min).
Steam pretreating corncobs at a severity index of 4.0 leads to a final pH of 3.5 to 4.0 of the pretreated biomass, while the same severity index leads to a final pH of 4.5 to 5 with bagasse biomass.
The process also includes extraction of the steam pretreated fibres with/or without eluent addition under pressure to remove water soluble hemicelluloses, acids and hemicellulose and cellulose degradation products. As an option these compounds, which are inhibitors of downstream hydrolysis and fermentation may be extracted during pretreatment, after pretreatment, or both during and after pretreatment. The extraction of the soluble compounds from the pretreated fibers preferably results in 4% to 10% xylose based sugars consisting of monomers and oligosaccharides remaining in the prehydrolysis fibers.
The extracted fibers, also referred to as prehydrolysate, are then separated from the gaseous reaction products in a cyclone separator and collected at the bottom of the separator, shredded and diluted to a desired consistency and subsequently transported to the enzymatic hydrolysis step.
The collected prehydrolysate is then shredded, 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.
In the following example, reference numbers refer to features of the pretreatment system and process streams, as shown in
Continuous steam explosion pretreatment of lignocellulosic biomass is carried out in a steam explosion pretreatment system. In this example the biomass is corncobs.
Corncobs 10 are received, stored, cleaned, ground (0.5 to 1 cm3 particle size) and fed through a V shaped hopper and screw auger (not shown). The corncob moisture is adjusted to 50% DM.
Prepared corncobs are pre-conditioned by preheating them with live steam 20 at atmospheric pressure, in a holding bin or preheating and conditioning container 30 to a temperature of about 95° C. for about 10-60 minutes. Air and steam are vented through an air vent 35 from the preheating and conditioning container 30.
Preheated corncobs are compressed in a first modular screw device 40 to remove air 50 through an air vent and inhibitory extracts 5. The corncobs are then fed into a pressurized upflow tube 70.
Pressurized saturated steam at a temperature of 205° C. is injected upstream of and/or directly into the upflow tube 70 by direct injection 60 and/or indirect injection of steam 61 in a jacketed section of the upflow tube until the desired cooking pressure is reached.
Corncobs are moved through the upflow tube with the aid of a screw conveyor/mixer (3 min) and are discharged into a pretreatment reactor 80.
Corncobs are continuously discharged from the pretreatment reactor 80 to a second pressurized modular screw device 100 after a residence time of 5 min at 205° C. in the pretreatment reactor 80. This results in a treatment severity index of 4).
During the residence time, condensate and cooking liquids collected at the bottom of the pretreatment reactor are purged through a purge discharge control valve 95.
Pretreated corncobs are washed with water eluent under pretreatment pressure. Hot water 90 is added to dilute the pretreated corncobs as the fiber is 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:corncobs and to achieve a greater extraction of hemicellulose. The extracted hemicellulose solution 110 is collected and concentrated to the desired dryness for further applications.
The pressurized washed corncobs are then flashed into a cyclone 120. The solids, i.e. purified cellulose, collected at the bottom of the cyclone separator and 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 and fed to a condensate tank 130. Any gaseous emissions from the pretreatment reactor, the cyclone separator and other parts of the steam gun setup are collected and treated in an environmental control unit (not shown). Cleaned gases are exhausted to atmosphere from the environmental control unit.
In order to simulate this new process, steam explosion pretreatment of corncobs was followed by batch washing at pilot scale with a 97% recovery of cellulose (
Extracted cellulose from the pilot scale pretreatment was highly susceptible to enzymatic hydrolysis. 80% of the maximum theoretical cellulose to glucose conversion was achieved in 60 h. 90% conversion of the 17% consistency slurry was reached in 95 h, using only 0.23% load of commercial cellulases product (
In
Samples of the continuously pretreated corncobs were hydrolyzed and fermented in a 2.5 metric tonne batch hydrolysis and fermentation trial (
The fermentability of the hydrolyzed cellulose was high. A concentration of 4.9% alcohol was reached in 20 hours (
In
The production of soluble xylo-oligosaccharides was equivalent to 12% of the weight of raw corncobs processed at pilot scale. 63% of the original content of corncobs hemicellulose was converted to volatile degradation products (
81% of the hemicellulose remaining in the corncobs prehydrolysate after autohydrolysis was collected through the prehydrolysate water washing step. The resulting lignin free solution contained dissolved solids of which 87% were sugars, including 63% of xylo-oligosaccharides (w/w) on a dry matter basis.
Steam explosion pretreatment of corncobs was carried out in a steam explosion pretreatment system pressurized with saturated steam at a temperature of 205° C. No acid was added to the corncobs during the heating step. The corncob moisture was adjusted to 60% DM. The overall retention time of corncob pretreatment was 8 min e.g. 3 min in the up flow tube, 5 min in the pretreatment reactor at pH 3.8. Corncob acidification resulted from the release of acetic acid from hemicellulose breakdown.
Pretreated corncobs were water washed.
Cellulose extraction from corncobs was carried out at pilot scale with a percentage recovery of 98% (
59% of the incoming hemicellulose was recovered after high pressure pretreatment of corncobs. 52% of incoming hemicellulose was collected into the xylo-oligosaccharides solution (
Steam explosion pretreatment of corncobs was carried out in a steam explosion pretreatment system pressurized with saturated steam at a temperature of 170° C. No acid was added to the corncobs during the heating step. The corncob moisture was adjusted to 50% DM. The overall retention time of corncobs pretreatment was 85 min e.g. 15 min in an up flow tube, 70 min in a pretreatment reactor at pH 3.8. Corncob acidification resulted from the release of acetic acid from hemicellulose breakdown.
Pretreated corncobs were water washed.
Cellulose extraction from corncobs was carried out at pilot scale with a percentage recovery of 98% (
51% of incoming hemicellulose was recovered after low pressure pretreatment of corncobs. 43% of incoming hemicellulose was collected in the xylo-oligosaccharides solution (
After explosive decompression, the solid fraction from high or low pressure pretreatment i.e. purified cellulose was collected at the bottom of cyclone separator, shredded and then diluted with fresh water up to 17% consistency.
Extracted cellulose from high and low pressure continuous pilot scale pretreatment of corncobs was highly susceptible to enzymatic hydrolysis. Digestibility of cellulose pretreated at high and low pressure was similar (
In
At pilot scale (2.5 metric tonne fed batch hydrolysis and fermentation trial,
In
Fermentability of the hydrolyzed cellulose was evaluated by adding enough C6-industrial grade commercial yeast to reach a concentration of 108 yeast cells per gram hydrolysate at 33° C., pH 5.3 when 90% of the maximum theoretical cellulose to glucose conversion was reached. pH adjustment was carried out with aqueous ammonia (30%) prior to yeast addition.
Fermentability of the hydrolyzed cellulose was high. A concentration of 4.9% alcohol was reached in 20 hours (
Steam explosion pretreatment of Bagasse was carried out in a system pressurized with saturated steam at a temperature of 205° C. No acid was added to the bagasse fibers during the heating step. The overall retention time of the bagasse fibers during pretreatment was 8 min e.g. 3 min in the up flow tube and 5 min in the pretreatment reactor at pH 4.8. Bagasse acidification resulted from the release of acetic acid from hemicellulose breakdown.
Pretreated Bagasse was water washed.
Cellulose extraction from the pretreated and washed Bagasse mash was carried out at pilot scale with a percentage recovery in the solid fraction of 95% (
72% of the incoming hemicellulose was recovered after pretreatment of Bagasse. 63% of the incoming hemicellulose was collected in the xylo-oligosaccharides solution (
Extracted cellulose from pilot scale pretreatment of Bagasse was highly susceptible to enzymatic hydrolysis. 80% of the maximum theoretical cellulose to glucose conversion was achieved in 110 h (
In
A concentration of 54 g/L glucose representing 80% conversion of cellulose was reached after 110 hours of hydrolysis of a 13% consistency slurry, using only a 0.3% load of commercial cellulase.
Fermentability of the hydrolyzed cellulose was evaluated by adding enough C6-industrial grade commercial yeast to reach a concentration of 108 yeast cells per gram hydrolysate at 33° C., pH 5.3. The time needed to reach the maximum theoretical cellulose to glucose conversion was determined. pH adjustment was carried out with aqueous ammonia (30%) prior to yeast addition.
The fermentability of the hydrolyzed cellulose was high. A concentration of 2.6% alcohol was reached in 20 hours (
The achieved high degree of cellulose digestibility and cellulose to glucose conversion rates of cellulose derived from bagasse biomass subjected to pretreatment solely by autohydrolysis and without the addition of any acid catalyst was surprising. Numerous prior art references cited below teach the use of acid to improve hemicellulose hydrolysis during pretreatment for biomass having a low inherent acetic acid content. To date, it was not recognized in the art that due to the delicate interplay between the higher amount of hemicellulose breakdown achieved with added acid catalyst and the inhibitory effects of the breakdown products and the catalyst on the downstream cellulose hydrolysis and glucose fermentation processes, the use of acid catalyst for biomass with low acetic acid content is not always advantageous and may in fact lead to lower ethanol yields for certain lignocellulosic biomasses. The inventors have now surprisingly discovered that autohydrolysis without the addition of any acid catalyst can be carried out on lignocellulosic biomass of <12% lignin content and an acetyl group content of 3-6% weight/weight in the dry matter, with satisfactory ethanol yield and even higher ethanol yield compared to processes using added acid catalyst in the pretreatment step. In fact, as can be seen from
This application claims the benefit of priority of U.S. Provisional Patent Application No. 61/172,057 filed Apr. 23, 2009, and of U.S. Provisional Application No. 61/171,997 filed Apr. 23 2009, and is a Continuation in Part Application of U.S. Ser. No. 13/460,207 filed Apr. 30, 2012, all of which are incorporated herein by reference in their entirety.
| Number | Date | Country | |
|---|---|---|---|
| 61171997 | Apr 2009 | US | |
| 61172057 | Apr 2009 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 12766599 | Apr 2010 | US |
| Child | 13460207 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 13460207 | Apr 2012 | US |
| Child | 13551087 | US |
