WO2014141896A1 - セルロース系バイオマスからのエタノール生産方法 - Google Patents
セルロース系バイオマスからのエタノール生産方法 Download PDFInfo
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- WO2014141896A1 WO2014141896A1 PCT/JP2014/054995 JP2014054995W WO2014141896A1 WO 2014141896 A1 WO2014141896 A1 WO 2014141896A1 JP 2014054995 W JP2014054995 W JP 2014054995W WO 2014141896 A1 WO2014141896 A1 WO 2014141896A1
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- 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
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
- C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
- C12P7/06—Ethanol, i.e. non-beverage
- C12P7/08—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate
- C12P7/10—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate substrate containing cellulosic material
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
- C12N1/00—Microorganisms, e.g. protozoa; Compositions thereof; Processes of propagating, maintaining or preserving microorganisms or compositions thereof; Processes of preparing or isolating a composition containing a microorganism; Culture media therefor
- C12N1/14—Fungi; Culture media therefor
- C12N1/16—Yeasts; Culture media therefor
- C12N1/165—Yeast isolates
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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
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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
- C13K13/00—Sugars not otherwise provided for in this class
- C13K13/002—Xylose
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12R—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES C12C - C12Q, RELATING TO MICROORGANISMS
- C12R2001/00—Microorganisms ; Processes using microorganisms
- C12R2001/645—Fungi ; Processes using fungi
- C12R2001/72—Candida
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Definitions
- the present invention relates to a method for producing ethanol by alcohol fermentation using a cellulosic biomass hydrolyzate.
- Cellulosic biomass is attracting attention as an ethanol production raw material by fermentation of microorganisms from the environmental aspect.
- agricultural waste such as wood, paper, bagasse (sugar cane squeezed), corn stover (corn core, stem, leaves, etc.) and straw
- Patent Documents 1 to 3 The use of cellulosic biomass raw materials has been studied.
- A. Petersson et al. ⁇ A 5-hydroxymethyl furfural reducing enzymes encoded by the Saccharomyces cerevisiae ADH6 gene conveys HMF tolerance '', Yeast 2006, Vol. 23, p.455-464 J. A. van Maris et al., ⁇ Alcoholic fermentation of carbon sources in biomass hydrolysates by Saccharomyces cerevisiae '', Antonie van Leeusenhoek, 2006, Volume 90, p.391-418 E. Palmqvist and B. Hahn-Hagardal, ⁇ Fermentation of lignocellulosic hydrolysate. II: inhibitors and mechanisms of inhibition '', Bioresource Technology, 2000, Vol. 74, p.25-33
- An object of the present invention is to provide a method for efficiently producing ethanol even when a fermentation inhibitor is present in a cellulosic biomass hydrolyzate.
- the present inventor has identified, using yeast belonging to Candida intermedia, in a method for producing ethanol using a fermentation liquid containing a cellulosic biomass hydrolyzate. It is possible to maintain efficient production of ethanol even when there is a fermentation inhibitor derived from cellulosic biomass hydrolyzate in the fermentation liquid by fermenting under the aeration conditions of The headline and the present invention were completed.
- the present invention provides the following [1] to [3].
- a cellulosic biomass hydrolyzate-containing fermentation solution is prepared under the conditions that the air supply rate into the fermenter is 0.0001 to 100 L / hour / g dry cell weight.
- a method for producing ethanol wherein the yeast is fermented using yeast belonging to (1).
- the fermentation according to [1], wherein the fermentation is a continuous method in which a fermentation liquid containing cellulosic biomass hydrolyzate is fed into the fermentor at a feed rate of 0.0002 to 2 L / hour / g dry cell weight. Ethanol production method.
- the method for producing ethanol according to [1] or [2], wherein the yeast belonging to Candida intermedia is a yeast named 4-6-4T2 and deposited as FERM BP-11509.
- ethanol can be efficiently produced from a cellulosic biomass hydrolyzate containing a fermentation inhibitor.
- Acetic acid 0.3% by mass (0.050 mol / L), levulinic acid 0.3% by mass (0.026 mol / L) and formic acid 0.2% by mass (0.043 mol / L) were added to the fermentation liquid, It is a figure which shows ethanol concentration time-dependent change at the time of making ethanol produce by each yeast.
- Add 0.22% by mass of furfural (0.023 mol / L) or 0.68% by mass (0.054 mol / L) of HMF to the fermentation liquid, and use Candida Intermedia 4-6-4T2 (FERM BP-11509).
- yeast belonging to Candida intermedia is used.
- the yeast is not particularly limited as long as it belongs to Candida intermedia, such as Candida intermedia “NBRC10601” available from National Institute of Technology and Evaluation (NITE). It may be a Candida intermedia mutant.
- the Candida intermedia “4-6-4T2” obtained by the present inventor by naturally mutating Candita intermedia “NBRC10601” as a parent strain according to a conventional method and selecting a strain having higher ethanol production ability than the parent strain.
- the 4-6-4T2 has the ability to efficiently produce ethanol from glucose and xylose in a short time in the presence of glucose and xylose.
- coexistence with glucose and xylose means that 4-6-4T2 coexists in a raw material liquid (fermentation liquid) containing at least glucose and xylose.
- the conventional yeast has insufficient xylose consumption efficiency, or has ethanol-producing ability from either glucose or xylose, but when both glucose and xylose are present, catabolite repression Xylose was hardly consumed until glucose was completely consumed, but 4-6-4T2 was able to efficiently remove ethanol from both in a short time even when both glucose and xylose were present. Have the ability to produce.
- 4-6-4T2 efficiently produces ethanol from a raw material liquid containing glucose and xylose in a short time, but at this time, almost no xylitol as a by-product is produced.
- 4-6-4T2 has the same properties as the parent strain except for the ability to produce ethanol from such sugars.
- yeasts which can produce ethanol from a cellulosic biomass hydrolyzate Pichia stipitis, Candida shihatae (Candida shehatae), Pachisolen tanofilus (Pacysolen tannofilus), etc. are also known. These yeasts can produce ethanol by consuming xylose which is difficult to consume among saccharides in cellulosic biomass hydrolyzate. However, since these yeasts cannot produce sufficient ethanol in the presence of fermentation inhibitors contained in cellulosic biomass hydrolysates, these yeasts can be used in place of yeasts belonging to Candida intermedia used in the present invention. Even if it does, efficient ethanol production cannot be achieved like this invention.
- a cellulose biomass hydrolyzate is contained as a carbon source.
- the cellulosic biomass refers to biomass containing cellulose and hemicellulose.
- Glucose is obtained by hydrolysis of cellulose in such biomass, while glucose, xylose, mannose, and galactose are obtained by hydrolysis of hemicellulose.
- sugar in a cellulose biomass hydrolyzate changes with kinds of cellulose biomass, all contain glucose, xylose, mannose, and galactose.
- cellulose-based biomass that is a raw material for hydrolysis
- agricultural residues rice straw, wheat straw, bagasse, corn stover, etc.
- forestry residues timber, etc.
- the cellulosic biomass hydrolyzate used in the present invention refers to a product obtained by hydrolyzing cellulosic biomass by dilute sulfuric acid method or hydrothermal decomposition method.
- the cellulosic biomass is dried and then pulverized, and distilled water and sulfuric acid (0.2 to 0.5% by mass) are added thereto so that the weight becomes 10 times, and 190 ° C. Hydrolysis at ⁇ 210 ° C for 5-10 minutes (PM.
- a saccharified solution suitable for ethanol production can be obtained by hydrolyzing cellulosic biomass at 190 ° C to 210 ° C for 5 to 10 minutes. (Id.).
- Cellulose biomass hydrolyzate contains furan compounds such as furfural and 5-hydroxymethylfurfural (HMF), weak acids such as acetic acid, formic acid, and levulinic acid as fermentation inhibitors generated during the hydrolysis process. It is.
- the typical content of a typical fermentation inhibitor in a cellulosic biomass hydrolyzate is, for example, 0.0 to 0.05 mol / L for furfural or HMF, and is 0.00 for acetic acid, formic acid, or levulinic acid. It is about 0 to 0.15 mol / L (HBKlinke et al. “Inhibiton of ethanol-producing yeast and bacteria by degradation products produced during pre-treatment of biomass”, Appl. Microbiol. Biotechnol. 66 vol. P.10-26).
- these fermentation inhibitors are weak acids such as acetic acid, for example, even if they are present in the fermentation solution at about 0.02 mol / L, usually the ethanol production efficiency is remarkably lowered, but the ethanol production method of the present invention is used. In that case, even if a weak acid as a fermentation inhibitor is present at 0.02 mol / L or more, it hardly affects the ethanol production efficiency, and even if it exists at 0.04 mol / L or more, it is efficient without any problem. Ethanol production can be performed. On the other hand, if it exceeds 0.20 mol / L, the ethanol production efficiency is likely to be affected.
- the ethanol production efficiency is usually significantly reduced.
- the ethanol production method of the present invention Even if 0.01 mol / L or more of a furan compound is present as a fermentation inhibitor, ethanol production efficiency is hardly affected, and even if 0.02 mol / L or more is present, efficient ethanol is satisfactory. Production can be done. On the other hand, if it exceeds 0.10 mol / L, the ethanol production efficiency tends to be affected, so that it is preferably 0.10 mol / L or less, more preferably 0.070 mol / L or less, and 0.040 mol / L. It is particularly preferred that In addition, the said content is content of the sum total of all the furan compounds.
- the ethanol production method of the present invention can naturally produce ethanol well even under conditions that do not contain weak acids or furan compounds, but it can produce ethanol well from cellulosic biomass hydrolysates despite the presence of fermentation inhibitors.
- the fermentation solution contains 0.02 mol / L to 0.15 mol / L of weak acid and / or 0.01 mol / L to 0.10 mol / L of furan compound. It is preferable. Further, it is more preferable that the weak acid is contained in the fermentation liquid at 0.04 mol / L to 0.12 mol / L and / or the furan compound is contained at 0.02 mol / L to 0.07 mol / L.
- fermentation production of ethanol is performed using the fermentation liquid containing the cellulosic biomass hydrolyzate, and the content of the cellulosic biomass hydrolyzate in the fermentation liquid is Although it can be selected as appropriate, it is more preferably 0.1 to 20% by mass, in terms of total monosaccharides based on the total amount in the fermentation liquid before being put into the fermenter, and 0.5 to 15% by mass. More preferably, the content is 1 to 10% by mass.
- Preferred sugar concentrations are 0.1 to 10% by mass for xylose, preferably 0.5 to 5% by mass, and 0.0 to 15% by mass for glucose and other hexoses in total. Is in the range of 0.5 to 5% by mass.
- the fermentation liquid used for ethanol production of the present invention may contain necessary components as appropriate in addition to the cellulose-based biomass hydrolyzate.
- saccharides such as glucose, mannose, galactose and xylose may be contained as a carbon source other than the cellulosic biomass hydrolyzate.
- the concentration of monosaccharides is preferably 0.1 to 10% by mass in total with saccharides derived from cellulosic biomass hydrolyzate, and is preferably 1 to 5% by mass. More preferably.
- nitrogen sources such as amino acids, urea, polypeptone, and amino acid-free nitrogen base, yeast extract and the like may be added.
- the yeast is also extracted when the fermentation solution containing ethanol in the culture tank is extracted, and it is necessary to grow the yeast in the fermentation tank. Therefore, when continuous fermentation over a long period of time is performed, it is preferable to appropriately include such components so as to be suitable for yeast growth.
- the air supply rate must be 0.0001 to 100 L / hour / g dry cell weight. Outside this range, ethanol production efficiency will be reduced.
- the air supply rate is preferably 0.005 to 100 L / hour / g dry cell weight, more preferably 0.005 to 10 L / hour / g dry cell weight, and 0.005 to 1.0 L / hour / g dry.
- the cell weight is preferred.
- the air supply rate is preferably 0.005 to 1.0 L / hour / g dry cell weight, more preferably 0.005 to 0.5 L / hour / g dry cell weight, 0.005 to 0.10 L / hour / g dry cell weight is more preferable, and 0.005 to 0.05 L / hour / g dry cell weight is particularly preferable.
- the air supply rate is preferably 0.05 to 100 L / hour / g dry cell weight, more preferably 0.05 to 10 L / hour / g dry cell weight, and 0.10 to 1.0 L.
- the weight of dried cells / hour / hour is more preferable, and the weight of dried cells of 0.10 to 0.5 L / hour / g is particularly preferable.
- the air is the atmosphere, which is 1/5 of the oxygen supply amount.
- the ethanol production method of the present invention may be carried out by a batch fermentation method or a continuous fermentation method. However, according to the present invention, since the problems of ethanol production in the continuous fermentation method can be improved, it is carried out by a continuous fermentation method. It is preferable.
- the present invention is carried out by a continuous fermentation method, it is preferable to supply the cellulosic biomass hydrolyzate-containing fermentation solution into the fermenter at a supply rate of 0.0002 to 2 L / hour / g dry cell weight. This supply rate is preferably 0.005 to 0.5 L / hour / g dry cell weight, more preferably 0.01 to 0.05 L / hour / g dry cell weight.
- the fermentation liquid is extracted at the same rate as the supply of the fermentation liquid.
- ethanol production by the continuous fermentation method is superior in that there is no switching of such processes, but conditions suitable for ethanol fermentation are often adopted rather than conditions suitable for growth.
- the growth of the yeast is suppressed, the yeast cannot be grown so as to supplement the yeast continuously extracted as the fermentation broth in the fermenter, the yeast concentration is reduced, and the ethanol production efficiency is also lowered. Therefore, in order to maintain high ethanol production efficiency by a normal continuous fermentation method, it is often necessary to supplement yeast.
- the balance between yeast growth and ethanol fermentation by the grown yeast can be effectively balanced, and efficient ethanol production can be maintained without additional supply of yeast during continuous fermentation. can do.
- batch fermentation with varying growth and ethanol production concentrations may not be suitable for ethanol fermentation with yeast using cellulosic biomass hydrolysates.
- the growth and ethanol production concentrations are kept almost constant, so the coenzyme production concentration is also constant, and there is no excess or deficiency in the supply of these coenzymes. This is because it is difficult to receive and ethanol can be produced efficiently.
- more preferable conditions for the ethanol production method of the present invention are an air supply rate of 0.05 to 100 L / hour / g dry cell weight, more preferably 0.05 to 10 L / hour / g dry cell weight, more preferably.
- the concentration of yeast during ethanol production is preferably adjusted to 0.5 to 5% by mass based on the dry cell weight. In the batch fermentation method, the concentration may be adjusted in the growth step before the ethanol fermentation step.
- the pre-cultured yeast is inoculated so as to be within this concentration range before the start of the culture, or after the inoculation, the yeast concentration may be multiplied by about twice, and during ethanol production, What is necessary is just to adjust so that it may become the range of this density
- the temperature during ethanol production is preferably 20 to 35 ° C.
- the following steps are used to adjust the amount of bacterial cells to a preferred concentration prior to ethanol production in the batch fermentation method, the pre-culture performed prior to the continuous fermentation method or the batch fermentation method, and the continuous fermentation method. It can be performed under such conditions.
- the medium contains a cellulosic biomass hydrolyzate as a carbon source, glucose and one or more sugars selected from mannose, galactose, and xylose, and further suitable amino acids, urea, polypeptone, amino acids suitable for growth
- a nitrogen source such as a nitrogen-free nitrogen base or a yeast extract or the like can be used.
- the concentration of monosaccharides is preferably 0.1 to 10% by mass in total, and more preferably 1 to 5% by mass.
- the amount used is preferably 20% by volume or less of the medium volume, and more preferably 10% by volume or less.
- the temperature is preferably 10 ° C. to 37 ° C., more preferably 25 ° C. to 30 ° C.
- the pH is preferably 4 to 7, more preferably 4.5 to 6.5.
- pre-culture is performed under aerobic conditions, it is more preferable to perform the culture at 5-6.
- the efficient ethanol production in the present invention means that a fermentation yield of 70% by mass or more is achieved within 24 hours from the start of fermentation in the batch fermentation method, and 24 hours from the start of fermentation in the continuous fermentation method. It means that 70 mass% or more is maintained in fermentation yield after that.
- the acclimatized strain solution was diluted 1000 times and applied to a medium of YNB agar medium (glucose: 5%, yeast extract: 1%, amino acid-free yeast nitrogen base: 2%, agar: 2%) at 25 ° C. After culturing for 4 days, a strain having formed a colony was obtained.
- Candida intermedia 4-6-4T2 strain This strain has been deposited with the Patent Organism Depositary Center (NITE) of the National Institute for Product Evaluation Technology (NITE), and the deposit number is FERM BP-11509.
- Example 1 Candida Intermedia NBRC10601 or Candida Intermedia 4-6-4T2 (FERM BP-11509) was added to YNB medium (2% glucose and 1% xylose, 2% yeast nitrogen base (without amino acids), 1 % Yeast extract) and precultured at a temperature of 30 ° C. and a pH of 5.5 to 6 (no adjustment) for 48 hours. Thereafter, a simulated cellulose-based biomass hydrolyzate-containing fermentation solution (glucose 3% by mass, xylose 2% by mass, acetic acid 0.5% by mass (0.08 mol / L), 0.05M phosphate buffer, pH 5.5) Bacteria were added to 2% by mass (corresponding to dry cell weight).
- YNB medium 2% glucose and 1% xylose, 2% yeast nitrogen base (without amino acids), 1 % Yeast extract
- the simulated cellulosic biomass hydrolyzate-containing fermentation liquid of Example 1 contains glucose and xylose, which are typical sugars in cellulosic biomass hydrolysate, and is also contained in cellulosic biomass hydrolyzate.
- a fermentation inhibitor As a fermentation inhibitor, acetic acid is contained, and a fermentation liquid containing cellulosic biomass hydrolyzate is simulated.
- ethanol was produced by batch fermentation without supplying the fermentation liquid and extracting the fermentation liquid, that is, without using the continuous fermentation method. For comparison, ethanol production was performed with an air supply of 0 L / hour / g dry cell weight.
- Example 2 Candida intermedia NBRC10601 or Candida intermedia 4-6-4T2 (FERM BP-11509) is pre-cultured under the same conditions as in Example 1, and then a simulated cellulose-based biomass hydrolyzate-containing fermentation solution (Glucose 3%, xylose 2%, acetic acid 0.3% by mass (0.05 mol / L), furfural 0.1% by mass (0.010 mol / L), 5-hydroxymethylfurfural (HMF) 0.1% by mass (0.008 mol / L), 0.05M phosphate buffer solution, pH 5.5) was added with a bacterium so as to be 2% by mass (corresponding to dry cell weight).
- a simulated cellulose-based biomass hydrolyzate-containing fermentation solution Glucose 3%, xylose 2%, acetic acid 0.3% by mass (0.05 mol / L), furfural 0.1% by mass (0.010 mol / L), 5-hydroxymethylfurfural (HMF) 0.1% by mass (0.008 mol / L),
- the simulated cellulose-based biomass hydrolyzate-containing fermentation liquid of Example 2 contains glucose and xylose, which are typical sugars in the cellulose-based biomass hydrolyzate, and the cellulose-based biomass hydrolyzate contains The fermentation inhibitor contains acetic acid, furfural, and HMF, and simulates a fermentation liquid containing cellulosic biomass hydrolyzate.
- ethanol was produced by batch fermentation without supplying the fermentation liquid and extracting the fermentation liquid, that is, without using the continuous fermentation method. For comparison, ethanol production was performed with an air supply of 0 L / hour / g dry cell weight.
- Example 3 Candida intermedia NBRC10601 or Candida intermedia 4-6-4T2 (FERM BP-11509) is pre-cultured under the same conditions as in Example 1, and then a simulated cellulose-based biomass hydrolyzate-containing fermentation solution (Glucose 3% by mass, xylose 2% by mass, acetic acid 0.3% by mass (0.050 mol / L), levulinic acid 0.3% by mass (0.026 mol / L), formic acid 0.2% by mass (0.043 mol) / L), 0.05 M phosphate buffer solution, pH 5.5) was added with a bacterium so as to be 2 mass% (corresponding to dry cell weight).
- a simulated cellulose-based biomass hydrolyzate-containing fermentation solution Glucose 3% by mass, xylose 2% by mass, acetic acid 0.3% by mass (0.050 mol / L), levulinic acid 0.3% by mass (0.026 mol / L), formic acid 0.2% by mass (0.043 mol) / L
- the simulated cellulose-based biomass hydrolyzate-containing fermentation liquid of Example 3 contains glucose and xylose, which are typical sugars in the cellulose-based biomass hydrolyzate, and contains the cellulose-based biomass hydrolyzate.
- the fermentation inhibitor acetic acid, levulinic acid, and formic acid are contained, and a fermentation liquid containing cellulosic biomass hydrolyzate is simulated.
- ethanol was produced by batch fermentation without supplying the fermentation liquid and extracting the fermentation liquid, that is, without using the continuous fermentation method. For comparison, ethanol production was performed with an air supply of 0 L / hour / g dry cell weight.
- Example 4 After pre-culturing Candida intermedia 4-6-4T2 (FERM BP-11509) under the same conditions as in Example 1, a simulated cellulosic biomass hydrolyzate-containing fermentation solution (glucose 3 mass%, xylose Bacteria were added to 2% by mass (corresponding to dry cell weight) to 2% by mass, furfural 0.22% by mass (0.023 mol / L), 0.05M phosphate buffer, pH 5.5). Using this, ethanol production was performed with an air supply amount of 0.01 L / h / g dry cell weight, and the change in ethanol concentration with time was measured.
- a simulated cellulosic biomass hydrolyzate-containing fermentation solution (glucose 3 mass%, xylose Bacteria were added to 2% by mass (corresponding to dry cell weight) to 2% by mass, furfural 0.22% by mass (0.023 mol / L), 0.05M phosphate buffer, pH 5.5).
- ethanol production was performed with an air supply amount of
- simulated cellulose-based biomass hydrolyzate-containing fermentation liquid of Example 4 contains glucose and xylose, which are typical sugars in the cellulose-based biomass hydrolyzate, and also contains the cellulose-based biomass hydrolyzate.
- a fermentation inhibitor furfural or HMF is contained, and a fermentation liquid containing cellulosic biomass hydrolyzate is simulated. Further, in this ethanol production, ethanol was produced by batch fermentation without supplying the fermentation liquid and extracting the fermentation liquid, that is, without using the continuous fermentation method. For comparison, ethanol production was performed with an air supply of 0 L / hour / g dry cell weight.
- Example 5 After pre-culturing Candida intermedia NBRC10601 under the same conditions as in Example 1, fermentation liquid containing simulated cellulose biomass hydrolyzate (glucose 3 mass%, xylose 2 mass%, acetic acid 0.5 mass% (0.08 mol / L), 0.05 M phosphate buffer solution, pH 5.5) was added to 0.36 L so as to be 2% by mass (7.2 g (dry cell weight)). Using this, the supply rate of the fermentation liquid was 0.015 L / hour, the extraction rate of the fermentation liquid was 0.015 L / hour, the air supply amount was 0 L / hour / g dry cell weight, 0.17 L / hour.
- simulated cellulose biomass hydrolyzate glucose 3 mass%, xylose 2 mass%, acetic acid 0.5 mass% (0.08 mol / L), 0.05 M phosphate buffer solution, pH 5.5
- the simulated cellulose-based biomass hydrolyzate-containing fermentation liquid of Example 5 contains glucose and xylose, which are typical sugars in the cellulose-based biomass hydrolyzate, and in the cellulose-based biomass hydrolyzate.
- acetic acid is contained, and a fermentation liquid containing cellulosic biomass hydrolyzate is simulated.
- Example 6 After pre-culturing Candida intermedia 4-6-4T2 (FERM BP-11509) under the same conditions as in Example 1, a simulated cellulosic biomass hydrolyzate-containing fermentation solution (glucose 3 mass%, xylose 2% by mass, 0.5% by mass of acetic acid (0.08 mol / L), 0.05M phosphate buffer, pH 5.5) 0.36 L, 2% by mass (equivalent to 7.2 g dry cell weight) was added as follows. Using this, the supply rate of the fermentation liquid was 0.015 L / hour, the extraction rate of the fermentation liquid was 0.015 L / hour, the air supply amount was 0 L / hour / g dry cell weight, 0.17 L / hour.
- a simulated cellulosic biomass hydrolyzate-containing fermentation solution (glucose 3 mass%, xylose 2% by mass, 0.5% by mass of acetic acid (0.08 mol / L), 0.05M phosphate buffer, pH 5.5) 0.
- the simulated cellulose-based biomass hydrolyzate-containing fermentation liquid of Example 6 contains glucose and xylose, which are typical sugars in the cellulose-based biomass hydrolyzate, and the cellulose-based biomass hydrolyzate contains As a fermentation inhibitor, acetic acid is contained, and a fermentation liquid containing cellulosic biomass hydrolyzate is simulated.
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Abstract
Description
〔1〕セルロース系バイオマス加水分解物含有発酵用液を、発酵槽内へのエア供給速度が0.0001~100L/時/g乾燥菌体重量となる条件下で、カンジダ・インターメディア(Candida intermedia)に属する酵母を用いて発酵させることを特徴とするエタノールの生産方法。
〔2〕発酵が、セルロース系バイオマス加水分解物含有発酵用液を0.0002~2L/時/g乾燥菌体重量の供給速度で発酵槽内に供給する連続法である、〔1〕記載のエタノールの生産方法。
〔3〕カンジダ・インターメディア(Candida intermedia)に属する酵母が、4-6-4T2と命名されFERM BP-11509として寄託された酵母である〔1〕又は〔2〕記載のエタノールの生産方法。
本発明のエタノールの生産方法では、カンジダ・インターメディア(Candida intermedia)に属する酵母が用いられる。該酵母としてはカンジダ・インターメディア(Candida intermedia)に属する酵母であれば特に限定されず、例えば、独立行政法人 製品評価技術基盤機構(NITE)から入手可能なカンジタ・インターメディア「NBRC10601」等であってもよいし、カンジダ・インターメディアの突然変異株であってもよい。その中でも、本発明者がカンジタ・インターメディア「NBRC10601」を親株として常法に従い自然変異させ、親株よりもエタノール生産能が高い株を選抜することにより取得したカンジダ・インターメディア「4-6-4T2」と命名し、「FERM BP-11509」として独立行政法人 製品評価技術基盤機構 特許生物寄託センター(NITE)(日本国茨城県つくば市東1丁目1番地1 中央第6)に寄託した酵母(原寄託日,2011年9月6日)を用いることが特に好ましい。
また、4-6-4T2は、グルコース及びキシロースを含有する原料液体から短時間で効率良くエタノールを生産するが、このとき副生成物としてのキシリトールがほとんど生成されない。また、4-6-4T2は、このような糖からのエタノールの生産能力以外については親株と同等の性質を有する。
本発明のエタノールの生産方法においては、セルロース系バイオマス加水分解物を炭素源として含有する。
ここで、セルロース系バイオマスとは、セルロースとヘミセルロースを含むバイオマスをいう。斯かるバイオマス中のセルロースが加水分解されることでグルコースが得られ、一方、ヘミセルロースが加水分解されることでグルコース、キシロース、マンノース、ガラクトースが得られる。なお、セルロース系バイオマス加水分解物中の各糖類の含有比率はセルロース系バイオマスの種類によって異なるが、いずれもグルコース、キシロース、マンノース、ガラクトースを含有する。
また、フルフラールやHMF等のフラン化合物であれば発酵用液中に0.01mol/L程度存在しても通常では著しくエタノール生産効率を低下させるが、本発明のエタノールの生産方法を用いた場合には、発酵阻害物質としてフラン化合物が0.01mol/L以上存在していても、エタノール生産効率にはほとんど影響せず、さらには0.02mol/L以上存在していても問題なく効率のよいエタノール生産を行うことができる。一方、0.10mol/Lを超えるとエタノール生産効率に影響しやすくなるため、0.10mol/L以下であることが好ましく、0.070mol/L以下であることがより好ましく、0.040mol/L以下であることが特に好ましい。なお、上記含有量は全てのフラン化合物の合計の含有量である。
従って、本発明のエタノール生産方法は、当然、弱酸やフラン化合物を含有しない条件下でも良好にエタノールを生産できるが、発酵阻害物質の存在にもかかわらずセルロース系バイオマス加水分解物から良好にエタノールを生産できるという効果を享受しやすいという観点からは、発酵用液中に弱酸が0.02mol/L~0.15mol/L及び/又はフラン化合物が0.01mol/L~0.10mol/L含有することが好ましい。さらに発酵用液中に弱酸が0.04mol/L~0.12mol/L及び/又はフラン化合物が0.02mol/L~0.07mol/L含有することがより好ましい。
本発明のエタノール生産方法においては、エア供給速度を0.0001~100L/時/g乾燥菌体重量とする必要がある。この範囲を外れると、エタノール生産効率が低下してしまう。エア供給速度は、0.005~100L/時/g乾燥菌体重量が好ましく、0.005~10L/時/g乾燥菌体重量がより好ましく、0.005~1.0L/時/g乾燥菌体重量が好ましい。また、回分発酵法の場合のエア供給速度は0.005~1.0L/時/g乾燥菌体重量が好ましく、0.005~0.5L/時/g乾燥菌体重量がより好ましく、0.005~0.10L/時/g乾燥菌体重量がさらに好ましく、0.005~0.05L/時/g乾燥菌体重量が特に好ましい。連続発酵法の場合のエア供給速度は0.05~100L/時/g乾燥菌体重量が好ましく、0.05~10L/時/g乾燥菌体重量がより好ましく、0.10~1.0L/時/g乾燥菌体重量がさらに好ましく、0.10~0.5L/時/g乾燥菌体重量が特に好ましい。ここでエアとは、大気であり、酸素供給量に換算すれば、その1/5である。
しかし、本発明のエタノール生産方法によれば、酵母の増殖と増殖した酵母によるエタノール発酵とのバランスを有効にとれ、連続発酵中に酵母の追加供給を行うことなく効率的なエタノールの生成を持続することができる。
すなわち、増殖および発酵工程において、酵母はセルロース系バイオマス加水分解物中に存在する糖以外に発酵阻害物質であるフルフラールやHMFもいっしょに取り込む。取り込まれたこれらの物質は増殖あるいは発酵過程で酵母の細胞内の酵素により、酸化および/または還元され無毒化される。その際、酵素は補酵素(NADHあるいはNADPH)を必要とするが、補酵素は増殖または発酵過程にともない生成する(非特許文献1)。そのため、増殖およびエタノール生産濃度が変動する回分発酵は、セルロース系バイオマス加水分解物を用いる酵母によるエタノール発酵には適さない場合がある。これに対し、連続発酵では、増殖およびエタノール生産濃度がほぼ一定に保たれるため、補酵素の生成濃度も一定となり、これら補酵素の供給に過不足が生じないため、発酵阻害物質の影響が受けにくく、効率的にエタノールを生産することが可能となるためである。
エタノール生産中の酵母濃度は、乾燥菌体重量で0.5~5質量%に調整することが好ましい。回分発酵法においては、エタノール発酵工程前の増殖工程においてこの濃度に調整すればよい。連続発酵法においては、培養開始前に前培養した酵母をこの濃度の範囲となるように植菌するか、植菌後、酵母濃度を2倍程度の増殖をともなってもよく、エタノール生産中はセルロース系バイオマス加水分解物含有発酵用液の供給速度(すなわち発酵液抜き出し速度)や酸素濃度等の培養条件を調整しこの濃度の範囲となるように調整すればよい。
以下の手順に従い、独立行政法人 製品評価技術基盤機構 特許生物寄託センター(NITE)に保存されている酵母カンジタ・インターメディア(Candida intermedia)「NBRC10601」を親株として、馴養及び自然変異により4-6-4T2株を取得した。
次いで、上記と同様にしてpHを5.0に調整したグルコース及びキシロースをそれぞれ1質量%含有する酢酸水溶液と液体培地を50%ずつ混合し、この混合液10mLに上記3日間培養した培養液を100μL添加し、更に7日間培養した。更に、上記と同様にしてpHを5.0に調整したグルコース及びキシロースをそれぞれ1質量%含有する酢酸水溶液80%と培地20%を混合し、この混合液10mLに上記7日間培養した培養液を100μL加え30日間更に培養し、馴養株液とした。
上記馴養株液を1000倍希釈し、YNB寒天培地(グルコース:5%、酵母エキス:1%、アミノ酸不含酵母ニトロゲンベース:2%、寒天:2%)の培地に塗布し、25℃で4日間培養した後、コロニーを形成した株を取得した。
カンジダ・インターメディア NBRC10601または、カンジダ・インターメディア 4-6-4T2(FERM BP-11509)を、YNB培地(グルコース2質量%およびキシロース1質量%、2%酵母ニトロゲンベース(アミノ酸不含)、1%酵母エキス)に添加し、48時間、温度30℃、pH5.5~6(調整なし)で前培養を行った。その後、模擬セルロース系バイオマス加水分解物含有発酵用液(グルコース3質量%、キシロース2質量%、酢酸0.5質量%(0.08mol/L)、0.05Mリン酸緩衝液、pH5.5)に2質量%(乾燥菌体重量相当)となるように菌を添加した。これを用い、エア供給量が0.01L/h/g乾燥菌体重量としてエタノール生産を行い、エタノール濃度の経時変化を測定した。結果は図1に示す。
なお、実施例1の上記模擬セルロース系バイオマス加水分解物含有発酵用液は、セルロース系バイオマス加水分解物中で代表的な糖類であるグルコースとキシロースを含有させ、またセルロース系バイオマス加水分解物中の発酵阻害物質としては酢酸を含有させ、セルロース系バイオマス加水分解物含有発酵用液を模擬したものである。
また、このエタノール生産では発酵用液の供給、発酵液の抜き出しは行わずに、すなわち連続発酵法は用いずに回分発酵法によってエタノール生産を行った。また、比較としてエア供給を0L/時/g乾燥菌体重量としてエタノール生産を行った。
カンジダ・インターメディア NBRC10601または、カンジダ・インターメディア 4-6-4T2(FERM BP-11509)を、実施例1と同様の条件で前培養を行った後に、模擬セルロース系バイオマス加水分解物含有発酵用液(グルコース3%、キシロース2%、酢酸0.3質量%(0.05mol/L)、フルフラール0.1質量%(0.010mol/L)、5-ヒドロキシメチルフルフラール(HMF)0.1質量%(0.008mol/L)、0.05Mリン酸緩衝液、pH5.5)に、2質量%(乾燥菌体重量相当)となるように菌を添加した。これを用い、エア供給量が0.01L/h/g乾燥菌体重量としてエタノール生産を行い、エタノール濃度の経時変化を測定した。結果は図2に示す。
なお、実施例2の上記模擬セルロース系バイオマス加水分解物含有発酵用液は、セルロース系バイオマス加水分解物中で代表的な糖類であるグルコースとキシロースを含有させ、またセルロース系バイオマス加水分解物中の発酵阻害物質としては酢酸、フルフラール、HMFを含有させ、セルロース系バイオマス加水分解物含有発酵用液を模擬したものである。
また、このエタノール生産では発酵用液の供給、発酵液の抜き出しは行わずに、すなわち連続発酵法は用いずに回分発酵法によってエタノール生産を行った。また、比較としてエア供給を0L/時/g乾燥菌体重量としてエタノール生産を行った。
カンジダ・インターメディア NBRC10601または、カンジダ・インターメディア 4-6-4T2(FERM BP-11509)を、実施例1と同様の条件で前培養を行った後に、模擬セルロース系バイオマス加水分解物含有発酵用液(グルコース3質量%、キシロース2質量%、酢酸0.3質量%(0.050mol/L)、レブリン酸0.3質量%(0.026mol/L)、ギ酸0.2質量%(0.043mol/L)、0.05Mリン酸緩衝液、pH5.5)に2質量%(乾燥菌体重量相当)となるように菌を添加した。これを用い、エア供給量が0.01L/h/g乾燥菌体重量としてエタノール生産を行い、エタノール濃度の経時変化を測定した。結果は図3に示す。
なお、実施例3の上記模擬セルロース系バイオマス加水分解物含有発酵用液は、セルロース系バイオマス加水分解物中で代表的な糖類であるグルコースとキシロースを含有させ、またセルロース系バイオマス加水分解物中の発酵阻害物質としては酢酸、レブリン酸、ギ酸を含有させ、セルロース系バイオマス加水分解物含有発酵用液を模擬したものである。
また、このエタノール生産では発酵用液の供給、発酵液の抜き出しは行わずに、すなわち連続発酵法は用いずに回分発酵法によってエタノール生産を行った。また、比較としてエア供給を0L/時/g乾燥菌体重量としてエタノール生産を行った。
カンジダ・インターメディア 4-6-4T2(FERM BP-11509)を、実施例1と同様の条件で前培養を行った後に、模擬セルロース系バイオマス加水分解物含有発酵用液(グルコース3質量%、キシロース2質量%、フルフラール0.22質量%(0.023mol/L)、0.05Mリン酸緩衝液、pH5.5)に2質量%(乾燥菌体重量相当)となるように菌を添加した。これを用い、エア供給量が0.01L/h/g乾燥菌体重量としてエタノール生産を行い、エタノール濃度の経時変化を測定した。また、模擬セルロース系バイオマス加水分解物含有発酵用液中のフルフラール0.22質量%に代えて5-ヒドロキシメチルフルフラール(HMF)0.68質量%(0.054mol/L)を含有させた発酵用液、比較としてこれら発酵阻害物質を含有しない発酵用液をそれぞれ用い、これ以外は同じ条件にてエタノール生産を行い、エタノール濃度の経時変化を測定した。結果は図4に示す。
なお、実施例4の上記模擬セルロース系バイオマス加水分解物含有発酵用液は、セルロース系バイオマス加水分解物中で代表的な糖類であるグルコースとキシロースを含有させ、またセルロース系バイオマス加水分解物中の発酵阻害物質としてはフルフラールまたはHMFを含有させ、セルロース系バイオマス加水分解物含有発酵用液を模擬したものである。
また、このエタノール生産では発酵用液の供給、発酵液の抜き出しは行わずに、すなわち連続発酵法は用いずに回分発酵法によってエタノール生産を行った。また、比較としてエア供給を0L/時/g乾燥菌体重量としてエタノール生産を行った。
カンジダ・インターメディア NBRC10601を、実施例1と同様の条件で前培養を行った後に、模擬セルロース系バイオマス加水分解物含有発酵用液(グルコース3質量%、キシロース2質量%、酢酸0.5質量%(0.08mol/L)、0.05Mリン酸緩衝液、pH5.5)0.36Lに、2質量%(7.2g(乾燥菌体重量))となるように添加した。これを用い、発酵用液の供給速度を0.015L/時、発酵用液の抜き出し速度を0.015L/時とし、エア供給量を0L/時/g乾燥菌体重量、0.17L/時/g乾燥菌体重量または1.7L/時/g乾燥菌体重量のいずれかとし、連続発酵法にてエタノール生産を行い、エタノール濃度の経時変化を測定した。結果は図5に示す。
なお、実施例5の上記模擬セルロース系バイオマス加水分解物含有発酵用液は、セルロース系バイオマス加水分解物中で代表的な糖類であるグルコースとキシロースを含有させ、またセルロース系バイオマス加水分解物中の発酵阻害物質としては酢酸を含有させ、セルロース系バイオマス加水分解物含有発酵用液を模擬したものである。
カンジダ・インターメディア 4-6-4T2(FERM BP-11509)を、実施例1と同様の条件で前培養を行った後に、模擬セルロース系バイオマス加水分解物含有発酵用液(グルコース3質量%、キシロース2質量%、酢酸0.5質量%(0.08mol/L)、0.05Mリン酸緩衝液、pH5.5)0.36Lに、2質量%(7.2g乾燥菌体重量相当)となるように添加した。これを用い、発酵用液の供給速度を0.015L/時、発酵用液の抜き出し速度を0.015L/時とし、エア供給量を0L/時/g乾燥菌体重量、0.17L/時/g乾燥菌体重量または1.7L/時/g乾燥菌体重量のいずれかとし、連続発酵法にてエタノール生産を行い、エタノール濃度の経時変化を測定した。結果は図6に示す。
なお、実施例6の上記模擬セルロース系バイオマス加水分解物含有発酵用液は、セルロース系バイオマス加水分解物中で代表的な糖類であるグルコースとキシロースを含有させ、またセルロース系バイオマス加水分解物中の発酵阻害物質としては酢酸を含有させ、セルロース系バイオマス加水分解物含有発酵用液を模擬したものである。
Claims (3)
- セルロース系バイオマス加水分解物含有発酵用液を、発酵槽内へのエア供給速度が0.0001~100L/時/g乾燥菌体重量となる条件下で、カンジダ・インターメディア(Candida intermedia)に属する酵母を用いて発酵させることを特徴とするエタノールの生産方法。
- 発酵が、セルロース系バイオマス加水分解物含有発酵用液を0.0002~2L/時/g乾燥菌体重量の供給速度で発酵槽内に供給する連続発酵である請求項1のエタノールの生産方法。
- カンジダ・インターメディア(Candida intermedia)に属する酵母が、4-6-4T2と命名されFERM BP-11509として寄託された酵母である請求項1または2に記載のエタノールの生産方法。
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JP2012080824A (ja) * | 2010-10-12 | 2012-04-26 | Actree Corp | エタノールの製造装置及びそれを用いた製造方法 |
WO2013065541A1 (ja) * | 2011-11-01 | 2013-05-10 | コスモ石油株式会社 | 新規酵母及びこれを用いたエタノールの生産方法 |
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JP2011205987A (ja) * | 2010-03-30 | 2011-10-20 | Toray Ind Inc | キシロース糖液の製造方法 |
JP2012080824A (ja) * | 2010-10-12 | 2012-04-26 | Actree Corp | エタノールの製造装置及びそれを用いた製造方法 |
WO2013065541A1 (ja) * | 2011-11-01 | 2013-05-10 | コスモ石油株式会社 | 新規酵母及びこれを用いたエタノールの生産方法 |
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JYOTHI CH . P. ET AL.: "ETHANOL PRODUCTION FROM D-XYLOSE BY CANDIDA INTERMEDIA MTCC-1404 : PARAMETER OPTIMIZATION USING TAGUCHI'S OVERALL EVALUATION CRITERIA TECHNIQUE", ASIAN JOURNAL OF MICROBIOLOGY, BIOTECHNOLOGY & ENVIRONMENTAL SCIENCES PAPER, vol. 7, no. 4, 2005, pages 679 - 684, XP008173321 * |
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NIDETZKY B. ET AL.: "Multiple forms of xylose reductase in Candida intermedia: comparison of their functional properties using quantitative structure-activity relationships, steady-state kinetic analysis, and pH studies", J. AGRIC. FOOD CHEM., vol. 51, no. 27, 2003, pages 7930 - 7935, XP055067471, DOI: doi:10.1021/jf034426j * |
Cited By (2)
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JP6097869B1 (ja) * | 2016-08-01 | 2017-03-15 | 新日鉄住金エンジニアリング株式会社 | エタノールの製造方法 |
JP2018019613A (ja) * | 2016-08-01 | 2018-02-08 | 新日鉄住金エンジニアリング株式会社 | エタノールの製造方法 |
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CN105026568A (zh) | 2015-11-04 |
BR112015023657A2 (pt) | 2017-07-18 |
JP6322187B2 (ja) | 2018-05-09 |
JPWO2014141896A1 (ja) | 2017-02-16 |
US20160002675A1 (en) | 2016-01-07 |
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