WO2015063549A1 - A method of preparing fermentable sugars from biomass resources - Google Patents

A method of preparing fermentable sugars from biomass resources Download PDF

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WO2015063549A1
WO2015063549A1 PCT/IB2013/060847 IB2013060847W WO2015063549A1 WO 2015063549 A1 WO2015063549 A1 WO 2015063549A1 IB 2013060847 W IB2013060847 W IB 2013060847W WO 2015063549 A1 WO2015063549 A1 WO 2015063549A1
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acid
biomass
sugars
pretreated
calcium carbonate
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PCT/IB2013/060847
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English (en)
French (fr)
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WO2015063549A9 (en
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Ravindra Kumar
Alok SATLEWAL
Ravi Prakash GUPTA
Deepak Kumar Tuli
Ravinder Kumar Malhotra
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Indian Oil Corporation Limited
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Publication of WO2015063549A1 publication Critical patent/WO2015063549A1/en
Publication of WO2015063549A9 publication Critical patent/WO2015063549A9/en

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    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
    • C13K1/00—Glucose; Glucose-containing syrups
    • C13K1/02—Glucose; Glucose-containing syrups obtained by saccharification of cellulosic materials
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P19/00—Preparation of compounds containing saccharide radicals
    • C12P19/02—Monosaccharides
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P19/00—Preparation of compounds containing saccharide radicals
    • C12P19/14—Preparation of compounds containing saccharide radicals produced by the action of a carbohydrase (EC 3.2.x), e.g. by alpha-amylase, e.g. by cellulase, hemicellulase

Definitions

  • the present invention relates to a method of preparing fermentable sugars from biomass resources.
  • Ethanol is one of the most promising alternative fuels to replace or supplement gasoline being used across the world.
  • current production of ethanol is based on sugarcane, corn and other starch rich grains.
  • sugarcane, corn and other starch rich grains For the ethanol industry to realize its goal of more th an 10 billion gallons production per year it needs to rely on a more sustainable and inexpensive feed stocks.
  • the use of these feed stocks raised the issue of food vis-a-vis fuel and, therefore, prompts to look for the production of ethanol from the non-food materials like liginocellulosic biomass. All these biomass contains a large amount of iiginocelluiose, which could be a potential feedstock for commercial ethanol production.
  • Plant cell walls are composed of lignocellulosic materials, which are represented by cellulose (linear glucose polymers), hemicellulose (highly branched heteropolymers) and lignin (crossiinked aromatic macromolecules with large molecular weight).
  • cellulose linear glucose polymers
  • hemicellulose highly branched heteropolymers
  • lignin crossiinked aromatic macromolecules with large molecular weight.
  • the bonding between the polysaccharide components (cellulose and hemicellulose) and iioii-polysaceharide components (lignin) is the main cause of mechanical and biological resistance.
  • Cellulose the most abundant polysaccharide on earth, is a polymer accounting about 50% of the wood weight.
  • the cellulose chain which forms fibrils consists of about 10,000 glucose units.
  • the cellulosic material has a crystal domain separated from the less-ordered, amorphous domain, which allows chemical and biochemical attack.
  • Cellulases can hydrolyze the cellulose polymer to monomers, and the resulting glucose is fermented into ethanol by the yeast Saccharomyces cerevisiae.
  • Hemicellulose is a short (100-200 sugar units), highly-branched heteropoiymer consisting of the predominant xylose as well as glucose, mannose, galactose, arabmose and other uronic acids.
  • C5 and C6 sugars are linked by 1 ,3-, 1,6- or 1 ,4-glucosidic linkages, which differentiate cellulose from lignin, and are often acetylated.
  • Lignin is a 3-dimensional polyphenohc network of dimethoxylated, monomethoxylated and non- methoxylated phenyipropanoid units, derived from p-hydroxycinnamyl alcohol. Lignin is hydrophobic and highly resistant to chemical and biological degradation. Celluiosic fibrils are embedded in an amorphous matrix network of hemiceiluiose and lignin, and they serve as glues between the plant cells, providing resistance to biodegradation. Other non-structural components (phenols, tannins, fats, sterols, sugars, starches, proteins and ashes) of the plant tissue generally accounts for 5% or less of the dry weight of biomass.
  • pretreatment processes such as steam explosion, mild acid treatment, strong acid treatment, ammonia treatment, alkali treatment, etc. are employed. No matter what it is, the pretreatment process should be environment-friendly and economically feasible. The pretreatment method will be selected considering process dependency and cost, as well as process yield and production parameters.
  • U.S. Pat. No. 5,628,830 discloses the use of calcium carbonate to adjust the pH of an aqueous sugar solution containing xylose, glucose, mannose and galactose arising from acid hydrolysis of lignocellulosic feedstock. After pH adjustment of the aqueous sugar solution, the solution is submitted to fermentation.
  • Brink's process employs full acid hydrolysis, which suffers from the disadvantage discussed above.
  • Shortcoming of processing lignocellulosic feedstocks to produce glucose is the large amounts of alkali that are required to adjust the pH of the acid pretreated feedstock prior to enzymatic hydrolysis with cellulase enzymes and special metallurgy of the vessel like hastalioy, which is very expensive.
  • alkali adds significant cost to the process.
  • the alkali reacts with the acid to produce salt, which must be processed or disposed of.
  • U.S. Pat. No. 4,425,433 discloses the use of sodium carbonate or sodium bicarbonate to neutralize an acidic feedstock slurry containing glucose, which slurry is produced by acid hydrolysis of the cellulose and hemiceiluiose components of the feedstock. After the neutralization, the acidic slurry or "wort", as referred to therein, is submitted to fermentation.
  • a disadvantage of this process is that the amount of sodium carbonate and sodium bicarbonate required for the ⁇ adjustment would add significant cost to the process and produce a large amount of salt to be disposed of.
  • special metallurgy of the vessel like Hastelloy is required, which is very expensive.
  • U.S. Pat. No. 6,927,048 discloses a process in which calcium carbonate and an amine or an alcohol are added during the fermentation of glucose to acetic acid.
  • the calcium carbonate controls the pH while the amine or alcohol complexes with the acetic acid.
  • the calcium carbonate is precipitated by the addition of carbon dioxide and then recovered from the fermentation broth.
  • the recovered calcium carbonate is then reused in the subsequent fermentation.
  • Verser et al does not address the reduction of alkali use during the pretreatment and neutralization of a lignocellulosic feedstock.
  • special metallurgy of the vessel like Hastelloy is required, which is very expensive.
  • U.S. Pat. No. 6,043,392 (Holtzapple et al.) also does not address reducing alkali usage during a neutralization conducted after acid pretreatment of a lignocellulosic feedstock. Rather, Holtzapple discloses a process that involves lime (alkali) treatment of lignocellulosic feedstocks with a subsequent fermentation step to produce volatile fatty acids (VFAs), followed by a thermal conversion of the VFAs to produce ketones. Calcium carbonate may be produced during an evaporation step involving carbon dioxide addition prior to thermal conversion of the VFAs.
  • the calcium carbonate is recycled to the fennentor to neutralize acids that are produced by the fermentation or is burned in a lime kiln to produce lime which may be used in the lime treatment.
  • special metallurgy of the vessel like Hastelloy is required, which is very expensive.
  • U.S. Pat. No. 5,693,296, also to Holtzapple discloses a process involving treating biomass with calcium oxide or hydroxide, followed by carbonating the pretreated material to form calcium carbonate or bicarbonate.
  • the calcium carbonate may be heated in a lime kiln to form calcium oxide, which can be hydrated to form calcium hydroxide, which, in turn, can be used to treat the biomass.
  • this process also does not address reducing chemical usage during a neutralization of an acid pretreated feedstock in the production of glucose.
  • special metallurgy of the vessel like hastalloy is required, which is very expensive.
  • a similar process is disclosed by Chang et al., 1998, Applied Biochemistry and Biotechnology, 74: 135- 159.
  • US 2006/0188965 discloses a process involving acid pretreatment of ceilulosic biomass.
  • the acid-pretreated feedstock slurry is then mixed with a lime solution to impart a pH of 10 to 1 1, followed by the addition of sulfuric acid to adjust the pH into a range of 5-7 prior to cellulose hydrolysis by cellulase.
  • a fermentation of the hydrolyzed material is carried out to produce alcohol, which is then concentrated by distillation.
  • Remaining liquids and/or solids from the distillation are subjected to a recycle processing step to filter fine particulates.
  • the resulting material is then sent back to the acid pretreatment, along with lignocellulosic material fed to the process.
  • the recycling of this material back to pretreatment does not reduce the amount of alkali used to neutralize the pretxeated cellulose.
  • special metallurgy of the vessel like Hastelloy is required, which is very expensive.
  • EP 2336195 relates a process of obtaining sugars and lignin from lignocellulosic biomass material.
  • the process uses formic acid for the purpose of treating lignocellulose biomass.
  • US20110144359 relates to a method of producing furfural from lignocellulosic biomass material.
  • WO2011002832 relates to a biomass process comprising removal and/or inactivation of an enzyme inhibitors from recycled washing solution.
  • WO 2010059825 relates to a process of obtaining sugar solutions from polysaccharide enriched biomass by contracting biomass with water and at least one nucelophilic base to produce a polysaccharide enriched biomass comprising a solid fraction and a liquid fraction.
  • the solid fraction is separated from the lignin-containing liquid fraction with an acid solution, the acid solution comprising about 70 weight percent to about 100 weight percent sulphuric acid or an acid mixture comprising phosphoric acid and sulphuric acid.
  • the present invention provides a method to prepare fermentable sugars from biomass resources, said method comprising the steps of:
  • step (d) hydrolysing the biomass slurry of step (c);
  • fermentable sugars can be produced with high yield via using an environment-friendly chemical e.g. tricarboxylic organic acid which includes citric acid, isocitric acid, aconitic acid, propane- 1 ,2,3 - tricarboxylic acid and trimesic acid.
  • an environment-friendly chemical e.g. tricarboxylic organic acid which includes citric acid, isocitric acid, aconitic acid, propane- 1 ,2,3 - tricarboxylic acid and trimesic acid.
  • carboxylic organic acids require no special metallurgy like Hastalloy, which is very expensive, for reaction vessel, which is required for acid pretreatment. This process can be done in the steel vessel.
  • the present disclosure provides a method for preparing fermentable sugars from biomass, comprising: (a) pretreatment of biomass with dilute citric acid, isocitric acid, aconitic acid, propane- 1,2,3-tricarboxylic acid and trimesic acid as an individual or in mixture from 0.5-20% w/v; (b) neutralizing the pretreated biomass mixture (c) separating the pentose sugars and solid pretreated biomass; (d) hydro lyzing the pretreated biomass slurry and (e) Integration of pretreatment process with enzymatic hydrolysis to convert them into fermentable sugars.
  • the biomass used as the source material in the present disclosure may include various known biological resources containing cellulose or lignocellulosic materials. Specifically, it may be rice straw, Jatropha pruning, wheat straw, corn cob, corn stover, rice husk, paper, wood, sawdust, agricultural waste, grass, sugar cane bagasse, cotton, flax, bamboo, abaca, algae, fruit skin or seaweed. More specifically, it may be wheat straw, corn stover, rice straw, sorghum stalk, rice husk, wood, sawdust, sugar cane bagasse or fruit skin.
  • the biomass can be pretreated with dilute solution from 0.5-20% of citric acid, isocitric acid, aconitic acid, propane- 1,2, 3 -tricarboxylic acid and trimesic acid as an individual or in mixture thereof.
  • the experiment was carried out in high pressure reactor at 130-220°C with 5-50% (w/w) biomass loading for 5-60 min resident time.
  • the neutral izer used may include various acid-neutralizing neutralizers known in the art. Specifically sodium hydroxide (NaOH), calcium carbonate (CaC0 3 ), sodium carbonate (Na 2 C0 3 ), magnesium hydroxide (Mg(OH) 2 , slaked lime (Ca(OH) 2 , quicklime (CaO) or calcium carbonate (CaC0 3 may be used. More specifically, sodium hydroxide (NaOH), sodium carbonate (Na 2 C0 3 ) or calcium carbonate (CaC0 3 ) may be used.
  • the resultant of the step (b), which is a mixture of liquid hydrolysate rich in pentose sugars and solid biomass rich in cellulose, may be separated using various known filtration apparatuses.
  • a filter press, a centrifuge, a membrane filter or a nanofilter may be used for the separation.
  • the cellulase treatment may be performed at pH 4-7 and 30-70°C for 12-48 hours. More specifically, the cellulase treatment may be performed at pH 4.8-5.5 and 48- 52°C for 24-36 hours.
  • Enzymatic hydrolysis of the pretreated slurry has to be done in citrate or phosphate buffer.
  • citrate buffer is commonly used. All the effective pretreatment process reported like sulfuric acid and alkali pretreatment. After pretreatment these chemicals need to be neutralized either in the separable salts like calcium sulphate if neutralized with calcium carbonate or soluble salts like sodium sulphate if neutralized with alkali and vice-versa in case of alkali pretreatment.
  • these chemicals need to be neutralized either in the separable salts like calcium sulphate if neutralized with calcium carbonate or soluble salts like sodium sulphate if neutralized with alkali and vice-versa in case of alkali pretreatment.
  • pretreatment is carried out in citric acid and pretreated slurry was neutralized with alkali, which provide in-situ citrate buffer and the solid stream received from the pretreatment can be directly incubated for enzymatic hydrolysis without any wash and without any separation process.
  • the LCB is treated with sulfuric, nitric or hydrochloric acids at higher temperatures to open up the LCB structure for subsequent enzymatic hydrolysis.
  • Enzymatic hydrolysis by cellulase enzymes works best at a pH of 5 to 5.5, however the LCB after pretreatment yields a solution with much lower pH, in range of 1-1.5. Therefore this solution needs to be neutralized with bases like calcium carbonate, sodium hydroxide etc to get a pH of about 5- 5.5.
  • This basic treatment generally produces insoluble alkali salts which need to be removed by filtration before these can be taken for enzymatic hydrolysis.
  • buffer- generally citrate or phosphate buffers need to be added.
  • the LCB pretreatment is effected by dilute organic acids like citric acid and after completion of pre-treatment, the acidic solution is treated with sodium hydroxide to get a pH of 5.0-5.5.
  • This treatment with base generates sodium citrate and the need to add buffer is avoided. It has been observed that the final concentration of citric acid buffer, after neutralization with strong base, fails between 0.5-0.1 molar which is an apt condition for enzymatic hydrolysis. Also the need to separate insoluble inorganic salts by filtration is done away with.
  • Additional benefits of pretreatment catalysed with organic acids include avoidance of use of special metallurgy reactors, Hastelloy type, which are essentially used when inorganic acids are employed in pretreatment. Accordingly, the main embodiment of the present invention relates to a method to prepare fermentable sugars from biomass resources, said method comprising the steps of:
  • step (d) hydro iysing the biomass slurry of step (c);
  • Another embodiment of the present invention relates to a method, wherein the step (a) the dilute acid is selected from group comprising of citric acid, isocitric acid, aconitic acid, propane- 1 ,2, 3- tricarboxylic acid and trimesic acid alone or as a mixture.
  • the dilute acid is selected from group comprising of citric acid, isocitric acid, aconitic acid, propane- 1 ,2, 3- tricarboxylic acid and trimesic acid alone or as a mixture.
  • Another embodiment of the present invention relates to a method, wherein the step (a) the dilute acid is in the concentration of 0.5-20% w/v.
  • the neutralizer is selected from the group comprising of sodium hydroxide (NaOH), calcium carbonate (CaCCK), sodium carbonate (Na 2 C0 3 ), magnesium hydroxide (Mg(OH) 2 , slaked lime (Ca(OH) 2 , quicklime (CaO) or calcium carbonate (CaC0 3 may be used. More specifically, sodium hydroxide (NaOH), sodium carbonates (Na 2 C0 3 ) or calcium carbonate (CaC0 3 ).
  • Yet another embodiment of the present invention relates to a method, wherein the step (b) the neutralizer is in the concentration of 1-lOM.
  • Yet another embodiment of the present invention relates to a method, wherein the step (b) the neutralizer is 5M.
  • Yet another embodiment of the present invention relates to a method, wherein the step (c), the penstose sugars and solid pretreated biomass slurry is separated using various known filtration methods selected from group comprising a filter press, a centrifuge, a membrane filter or a nanofilter.
  • Another embodiment of the present invention relates to a method, wherein step (d) hydrolysis of pre-treated biomass slurry is carried out using celiulase at a pH 4-7 at a temperature of 30°C- 70°C for 12-48 hours.
  • Another embodiment of the present invention relates to a method, wherein the step (d) hydrolysis of pre-treated biomass slurry is carried out using celiulase at a pH 4,8-5.5 at a temperature of 48°C-52 e C for 24-36 hours.
  • step (a) is carried out under high pressure of at 130°C-220°C.
  • Yet another embodiment of the present invention relates to a method, wherein the step (a) the biomass concentration is in the range of 5-50% (w/w).
  • Yet another embodiment of the present invention relates to a method, wherein the step (a) the pressure is in the range of 5-10 bars.
  • Yet another embodiment of the present invention relates to a method, wherein the step (a) the pressure is 5.5 bar.
  • Example-1 A mixture of biomass (150 g) in de-mineralized water (1200ml) was taken in the high pressure reactor equipped with agitator, temperature and pressure probe and temperature control, sampling port and re-circulating coil. The reactor was also has a port to add catalyst at high pressure and temperature. The stirred mixture was heated to 160 C (pressure 5.5bar). After the reaction temperature reached to 160°C a solution of citric acid (30g) and de-mineralized water (150g) was pumped in the reactor using pressure vessel at 8 bar. The stirring was continued for 30 min and the reaction mixture was cooled to room temperature in 15 min using chilling water circulation. The whole mixture was neutralized by 5M Sodium hydroxide solution till pH 5. Solid and liquid materials were separated using centrifuge.
  • the liquid hydrolysate was tested for inhibitors and sugars.
  • Solid pretreated slurry 300g on dry weight basis
  • Reactor temperature was maintained at 50°C and cellulase preparation from cellulases was added at 15 FPU/g of pretreated biomass and total reaction volume was making up to lOOOg using de- mineralized water at 5 pH.
  • 20g of sodium azide was added to the reactor to prevent the growth of any micro-organisms during the hydrolysis process.
  • the continuous agitation of reaction mixture was carried out for 24 hours to release maximum monomelic sugars.
  • the liquid sample after complete hydrolysis was subjected to DNS for sugar analysis. The data received is summarized in Table- 1.
  • Example-2 A mixture of biomass (100 g) in de-mineralized water (900ml) was taken in the high pressure reactor equipped with agitator, temperature and pressure probe and temperature control, sampling port and re-circulating coil. The reactor was also has a port to add catalyst at high pressure and temperature. The stirred mixture was heated to 170 C (pressure 5.5bar). After the reaction temperature reached to 170°C a solution of citric acid (20g) and de-mineralized water (l OOg) was pumped in the reactor using pressure vessel at 8 bar. The stirring was continued for 30 min and the reaction mixture was cooled to room temperature in 15 rain using chilling water circulation. The whole mixture was neutralized by 5M Sodium hydroxide solution till pH 5. Solid and liquid materials were separated using centrifuge. The liquid hydrolysate was tested for inhibitors and sugars.
  • Solid pretreated slurry (300g on dry weight basis) having pH 5 was taken in the hydrolysis reactor equipped with agitator and a temperature probe. Reactor temperature was maintained at 50 C and cellulase preparation from cellulases was added at 1 5 FPU/g of pretreated biomass and total reaction volume was making up to lOOOg using de-mineralized water at 5 pH. 20g of sodium azide was added to the reactor to prevent the growth of any micro-organisms during the hydrolysis process. The continuous agitation of reaction mixture was carried out for 24 hours to release maximum monomeric sugars. The liquid sample after complete hydrolysis was subjected to DNS for sugar analysis. The data received is summarized in Table- 1.
  • Solid and liquid materials were separated using centrifuge.
  • the liquid hydrolysate was tested for inhibitors and sugars.
  • Solid pretreated slurry 300g on dry weight basis
  • Reactor temperature was maintained at 50°C and ceilulase preparation from cellulases was added at 15 FPU/g of pretreated biomass and total reaction volume was making up to lOOOg using de- mineralized water at 5 pH.
  • 20g of sodium azide was added to the reactor to prevent the growth of any micro-organisms during the hydrolysis process.
  • the continuous agitation of reaction mixture was carried out for 24 hours to release maximum monomeric sugars.
  • the liquid sample after complete hydrolysis was subjected to DNS for sugar analysis. The data received is summarized in Table-1.
  • Example-4 A mixture of biomass (100 g) in de-mineralized water (900ml) was taken in the high pressure reactor equipped with agitator, temperature and pressure probe and temperature control, sampling port and re-circulating coil. The reactor was also has a port to add catalyst at high pressure and temperature. The stirred mixture was heated to 170 C (pressure 5.5bar). After the reaction temperature reached to 170 IJ C a solution of citric acid (lOg) and isocitric acid (20g) and de-mineralized water (lOOg) was pumped in the reactor using pressure vessel at 8 bar. The stirring was continued for 60 min and the reaction mixture was cooled to room temperature in 15 min using chilling water circulation. The whole mixture was neutralized by 5M Sodium hydroxide solution till pH 5.
  • Solid and liquid materials were separated using centrifuge. The liquid hydrolysate was tested for inhibitors and sugars.
  • Solid pretreated slurry 300g on dry weight basis
  • having Ph 5 was taken in the hydrolysis reactor equipped with agitator and a temperature probe. Reactor temperature was maintained at 50°C and ellulose preparation from cellulases was added at 15 FPU/g of pretreated biomass and total reaction volume was making up to lOOOg using de-mineralized w r ater at 5 Ph. 20g of sodium azide was added to the reactor to prevent the growth of any micro-organisms during the hydrolysis process. The continuous agitation of reaction mixture was carried out for 24 hours to release maximum monomeric sugars.
  • Example 5 (Control); Same as example 4 except that the organic acid was not used in pre- treatment. Data received was summarised in Table- 1.
  • Table-1 Isihibitors and sugars in pretreatment and enzymatic hydrolysate

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AU2019200694A1 (en) * 2018-02-09 2019-08-29 Department Of Biotechnology Additive composition useful for improved production of fermentable sugars from lignocellulosic biomass
US10487347B2 (en) 2015-12-09 2019-11-26 Indian Oil Corporation Limited Method of pretreatment for enhanced enzymatic hydrolysis
US10612059B2 (en) 2015-04-10 2020-04-07 Comet Biorefining Inc. Methods and compositions for the treatment of cellulosic biomass and products produced thereby
US10633461B2 (en) 2018-05-10 2020-04-28 Comet Biorefining Inc. Compositions comprising glucose and hemicellulose and their use
US20210047661A1 (en) * 2018-03-12 2021-02-18 Indian Oil Corporation Limited Sscf process for second generation ethanol production from lignocellulosic biomass and 2g residual biomass
US12263184B2 (en) 2019-05-10 2025-04-01 Comet Biorefining Inc. Materials and methods for producing arabinoxylan compositions

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