JP2017136016A - Ethanol production method - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide production methods of lignocellulose system biomass-derived compound which does not require a facility for removal treatment of fermentation inhibition substances, such as excess degradation products of a monosaccharide produced by water treatment before fermentation, particularly by a pretreatment with acid, alkali and the like, and organic acid and the like as by-products.SOLUTION: A production method comprises (A) mixing pretreated lignocellulose system biomass and an enzyme to saccharify; and (B) inoculating yeast to saccharified solution and saccharified residue obtained in the step (A) to ferment; further comprises (M) in accordance to the concentration of a fermentation inhibition substance in a liquid comprising the pretreated lignocellulose system biomass before the step (A) or in a saccharified solution obtained in the step (A), determining the bacterial cell concentration of the yeast in the step (B) so as to be a predetermined reference value that is a bacterial cell concentration of the yeast equal to or over the critical value of the bacterial cell concentration of the yeast what is not subjected to fermentation inhibition; and yeast is inoculated so as to enable the bacterial cell concentration to become that determined in the step (M), in the step (B).SELECTED DRAWING: None

Description

  The present invention relates to a method for producing a lignocellulosic biomass-derived compound.

  In recent years, from the viewpoint of global warming countermeasures and effective utilization of waste, the use of biomass using plant resources as a raw material has attracted attention. In general, sugars such as sugar cane and starches such as corn are often used as raw materials for producing a compound such as ethanol from biomass. However, these raw materials are originally used as food or feed, and long-term utilization as industrial resources may cause competition with food or feed use and may cause a rise in raw material prices.

  Therefore, technology development that uses non-edible biomass as an energy resource is being promoted. Non-edible biomass includes the most abundant cellulose on the earth, most of which exists as lignocellulose, which is a complex with the aromatic polymer lignin and hemicellulose.

  As a method for producing a target compound from lignocellulosic biomass, pretreatment such as hydrothermal treatment is performed. At this time, if necessary, an acid or an alkali may be mixed as appropriate. In the pretreatment process, polymers such as hemicellulose and lignin constituting lignocellulose are decomposed to improve the reactivity of cellulose in the subsequent process. However, it is known that if the acid strength and temperature conditions are too strong, the monosaccharides produced by the decomposition of cellulose and hemicellulose are further decomposed to produce a hyperdegradation product, which inhibits the subsequent fermentation process. . It is also known that organic acids such as acetic acid and formic acid are produced as by-products mainly when hemicellulose is decomposed, and these also inhibit the subsequent fermentation process.

  Patent Document 1 discloses a method for removing a fermentation inhibitor by treating with a wood-based carbide. Patent Document 2 discloses a method of removing a fermentation inhibitor by adsorbing or holding a polystyrene resin.

JP 2005-270056 A JP 2011-78327 A

  In patent document 1, in order to remove a fermentation inhibitor, the wood type carbide | carbonized_material and the installation for a removal process are needed. In patent document 2, in order to remove a fermentation inhibiting substance, the polystyrene-type resin and the installation for a removal process are needed. Furthermore, equipment for performing desorption treatment (regeneration treatment) of the polystyrene resin is required.

  This invention is made | formed in view of the said situation, Comprising: It aims at providing the manufacturing method of a stable and efficient lignocellulosic biomass origin compound in presence of a fermentation inhibitory substance.

That is, the present invention is as follows.
(1) A method for producing a lignocellulosic biomass-derived compound,
A method for producing a lignocellulosic biomass-derived compound,
(A) mixing pre-treated lignocellulosic biomass and enzyme and saccharifying;
(B) a step of inoculating and fermenting yeast to the saccharified solution and saccharification residue obtained in the step (A),
Before step (A) or after step (A) and before step (B),
(M) Pre-set according to the concentration of the fermentation inhibitor in the liquid containing the pretreated lignocellulosic biomass before the step (A) or in the saccharified liquid obtained in the step (A). A step of determining the yeast cell concentration in the step (B) so as to be a reference value,
The preset reference value is a yeast cell concentration that is not less than a critical value of the yeast cell concentration that does not undergo fermentation inhibition according to the concentration of the fermentation inhibitor,
In the said process (B), yeast is inoculated so that it may become the said cell density | concentration determined in the said process (M), The manufacturing method characterized by the above-mentioned.
(2) The method for producing a lignocellulosic biomass-derived compound according to (1), wherein the preset reference value is 1.0 to 3.0 times the critical value.
(3) The method for producing a lignocellulosic biomass-derived compound according to (1) or (2), wherein the fermentation inhibitor is furfural.
(4) The critical value is represented by a concentration (CFU (Colony forming unit) / mL) using the number of yeast cells,
When the concentration of the furfural is X (g / L) and the critical value is Y (CFU / mL), the X and the Y are in a relationship represented by the following formula [1]. A method for producing a lignocellulosic biomass-derived compound.

(In Formula [1], a is a number of 1.0 × 10 ⁷ or more and 4.0 × 10 ⁷ or less, and b is 2.0 × 10 ^6. )
(5) The critical value is represented by a concentration (g / L) using dry cell weight of yeast,
The number of yeast cells contained per gram of dry cells is 1.5 × 10 ¹⁰ CFU,
When the concentration of the furfural is X (g / L) and the critical value is Y ′ (g / L), the X and Y ′ are in the relationship represented by the following formula [2] (3). The manufacturing method of the lignocellulosic biomass origin compound of description.

(In Formula [2], c is a number between 0.5 and 2.5, and d is 0.13.)

  According to the method of the present invention, the yield of the lignocellulosic biomass-derived compound can be improved stably and efficiently in the presence of a fermentation inhibitor.

It is the schematic which showed the path | route of the detoxification of the furfural in yeast. It is a figure which shows schematic structure of the manufacturing apparatus of the lignocellulosic biomass origin compound in this embodiment. It is a graph which shows the change of (A) glucose concentration, (B) xylose concentration, (C) furfural concentration, and (D) ethanol concentration in the saccharification process and fermentation process in Example 1. It is a graph which shows the relationship between the fermentation yield in the fermentation process in Example 2, and a furfural density | concentration. (A) is a graph showing the relationship between the critical value and the furfural concentration in Example 2, and (B) is the relationship between the critical value and the furfural concentration replaced with the number of yeast cells in Example 2. (C) is a graph which shows the relationship between said critical value substituted with the dry weight of the yeast in Example 2, and a furfural density | concentration.

  In the present specification, the lignocellulosic biomass mainly contains cellulose, hemicellulose and lignin, such as conifers, hardwoods, construction wastes, forest land remnants, pruning wastes, rice straw, rice husks, wheat straw, wood Agricultural and forestry product resources such as chips, wood fiber, chemical pulp, waste paper, and plywood, agricultural and forestry product waste such as sugarcane bagasse, sugarcane foliage, and corn stover, processed agricultural and forestry products, and plant tissues such as macroalgae and microalgae. These lignocellulosic biomasses may be used alone or as a mixture.

In this specification, hemicellulose is called pentose containing 5 carbons such as xylose, or hexose containing 6 carbons such as mannose, arabinose and galacturonic acid. In addition, since it has complex polysaccharides such as glucomannan and glucuronoxylan, when it is hydrolyzed, it is a 5-carbon pentose monosaccharide or a pentose oligo linked to multiple monosaccharides. Saccharose, six carbon hexose monosaccharides, hexose saccharide oligosaccharides linked to multiple monosaccharides, pentose saccharide monosaccharides and hexose sugar monosaccharides linked together Produces sugar.
Cellulose has 6 carbons as a structural unit, so when hydrolyzed, it produces 6-carbon monosaccharides composed of 6 carbons and hexose oligosaccharides in which a plurality of monosaccharides are linked. In general, the composition ratio and production amount of monosaccharides and / or oligosaccharides depends on the type of plant tissue such as pre-treatment methods and agricultural / forestry product resources, agricultural / forestry product wastes, processed agricultural / forestry products, macroalgae, and microalgae used as raw materials. It depends on.

  Hereinafter, embodiments of the present invention will be described in detail with reference to the drawings. In each of the drawings, portions not related to the description may be omitted.

<Method for producing lignocellulosic biomass-derived compound>
The method for producing the lignocellulosic biomass-derived compound of the present embodiment is as follows:
(A) mixing pre-treated lignocellulosic biomass and enzyme and saccharifying;
(B) a step of inoculating and fermenting yeast to the saccharified solution and saccharification residue obtained in the step (A),
Before step (A) or after step (A) and before step (B),
(M) Pre-set according to the concentration of the fermentation inhibitor in the liquid containing the pretreated lignocellulosic biomass before the step (A) or in the saccharified liquid obtained in the step (A). A step of determining the yeast cell concentration in the step (B) so as to be a reference value,
The preset reference value is a yeast cell concentration that is not less than a critical value of the yeast cell concentration that does not undergo fermentation inhibition according to the concentration of the fermentation inhibitor,
In the step (B), yeast is inoculated so as to achieve the cell concentration determined in the step (M).

  According to the production method of the present embodiment, the yield of the lignocellulosic biomass-derived compound can be improved stably and efficiently in the presence of a fermentation inhibitor.

≪Process (A): Saccharification process≫
In the production method of this embodiment, first, pretreated lignocellulosic biomass and enzyme are mixed and saccharified. The saccharification temperature is preferably 45 ° C to 70 ° C, more preferably 45 ° C to 55 ° C, and particularly preferably 50 ° C. The saccharification time is preferably 12 hours to 120 hours, more preferably 24 hours to 96 hours, and further preferably 24 hours to 72 hours.

In the present specification, the enzyme means an enzyme that decomposes lignocellulosic biomass into monosaccharides or oligosaccharide units, and any enzyme that decomposes lignocellulosic biomass into monosaccharides or oligosaccharides can be used. Any material having hemicellulase activity may be used.
The cellulase may be any one that decomposes cellulose into monosaccharides or oligosaccharides such as glucose. At least one activity of each activity of endoglucanase (EG), cellobiohydrolase (CBH), and β-glucosidase (BGL). It is preferable from the viewpoint of enzyme activity that it is an enzyme mixture having each of these activities.
Similarly, hemicellulase may be any one that decomposes hemicellulose into monosaccharides or oligosaccharides such as xylose, and has at least one activity of each activity of xylanase, xylosidase, mannanase, pectinase, galactosidase, glucuronidase, and arabinofuranosidase. From the viewpoint of enzyme activity, an enzyme mixture having each of these activities is preferable.
The origin of these cellulases and hemicellulases is not limited, and cellulases and hemicellulases such as filamentous fungi, basidiomycetes, and bacteria can be used.

  In this specification, the pretreated lignocellulosic biomass means lignocellulosic biomass that has been pretreated in order to efficiently perform a saccharification reaction. Examples of the pretreatment method include a steaming method using only steam, a method using an ionic liquid, and a pulverizing method using a mill. Further, in the pretreatment, an acid or an alkali may be appropriately mixed as necessary. The acid is selected from sulfuric acid, hydrochloric acid, nitric acid, phosphoric acid and the like, and these may be used alone or in combination. Among them, sulfuric acid which is inexpensive and easily available is particularly preferable for industrial use. Examples of the alkali include sodium hydroxide, potassium hydroxide, ammonia, calcium carbonate, sodium carbonate, sodium sulfite and the like, and these may be used alone or in combination. There is no particular limitation on the reaction vessel used for the pretreatment, but there is a form in which a heat pressure vessel having acid resistance or alkali resistance, or a vessel having acid resistance or alkali resistance is placed in a heating pressure device such as an autoclave for treatment. Conceivable.

  The pretreated lignocellulosic biomass contains various by-products in addition to at least one of cellulose, hemicellulose, monosaccharide and oligosaccharide. If these by-products are substances that do not adversely affect the subsequent saccharification process, fermentation process, etc., they can be removed in the final purification process, so this is not a big problem. However, if the fermentation inhibitor has an adverse effect, it is necessary to prevent adverse effects on each step in the saccharification step or the previous step of the fermentation step.

  In the present specification, the fermentation inhibitor is a substance that interferes with the fermentation reaction in the fermentation process. Representative fermentation inhibitors include sugar hyperdegradants, lignin or lignin-derived aromatic compounds, adhesives or paint-derived compounds. Among these, compounds derived from artificial chemicals such as adhesives and paints can be avoided to some extent by using naturally-derived lignocellulosic biomass that has not been treated. However, as long as lignocellulosic biomass is used as a raw material, it is difficult to avoid the production of sugar overdegradation products and lignin-derived aromatic compounds. Here, when the fermentation inhibitor is an insoluble solid such as lignin and at least one of cellulose, hemicellulose, monosaccharide and oligosaccharide is soluble, it can be removed by ordinary solid-liquid separation. In some cases. However, when both fermentation inhibitory substances and useful substances are soluble, ordinary solid-liquid separation cannot be applied. Therefore, there is a method for determining and inoculating the yeast cell concentration according to the concentration of fermentation inhibitory substances described later. Preferably applied. That is, in this embodiment, the fermentation inhibitor to be treated mainly forms a mixed solution with at least one of cellulose, hemicellulose, monosaccharide and oligosaccharide, and is usually It cannot be separated by solid-liquid separation, or it is difficult to separate. Examples of such fermentation inhibiting substances include acetic acid, formic acid, levulinic acid, a sugar hyperdegradation product furfural, 5-hydroxymethylfurfural (5-HMF), lignin-derived aromatic compound vanillin, acetovanillin , Guayacoal and so on. Of these fermentation inhibitors, typical fermentation inhibitors are furfural and 5-HMF.

The mechanism of yeast fermentation inhibition by the above-mentioned furfural or 5-HMF will be described below. Furfural or 5-HMF is known to inhibit yeast glycolysis and alcohol dehydrogenation (ADH) (Alemeida et al., J Chem. Technol. Biotechnol. 82: 320-349 (2007). reference). Further, FIG. 1 is a schematic diagram showing a route of detoxification of furfural in yeast. Under aerobic conditions, oxygen and water change to 2-fluoroic acid, which is a kind of carboxylic acid, and further change to 2-floryl-CoA by ATP, which is utilized in the TCA circuit. On the other hand, NADH is required to detoxify furfural under anaerobic conditions (see the following formula [3]). It is known that furfural is reduced to furfuryl alcohol by NADH, and further furfuryl alcohol is excreted from the cell (see Nieces et al. Front. Bioeng. Biotechnol. 18, Feb (2015)).
Therefore, in order for yeast to synthesize NADH, synthesis of acetic acid from glucose is preferentially performed (see the following formula [4]), and synthesis of ethanol from glucose is suppressed.

  The inventors of the present invention focused on the above-mentioned fermentation inhibition mechanism, and reached the present invention by inoculating the amount of yeast corresponding to the concentration of the fermentation inhibition substance.

≪Process (M): Determination process≫
Subsequently, the concentration of the fermentation inhibitor in the liquid containing the pretreated lignocellulosic biomass before the step (A) or in the saccharified liquid obtained in the step (A) is measured. In accordance with the measured concentration of the fermentation inhibitor, the yeast cell concentration in the step (B) described later is determined so as to be a preset reference value.
As a method for measuring the concentration of the fermentation inhibitor, for example, before saccharification is started in the saccharification apparatus, during saccharification, or after saccharification, the liquid is extracted and a color reaction using high-performance liquid chromatograph or nitrophenylhydrazine and an alkaline solution Examples thereof include a method for measuring a fermentation inhibitory substance (when the fermentation inhibitory substance is furfural), a method for calculating the concentration of the fermentation inhibitory substance based on pretreatment conditions on the line, and the like.

In the manufacturing method of the present embodiment, the reference value is preset as follows.
First, pretreated lignocellulosic biomass having different pretreatment conditions is prepared on a small scale. About pre-processing conditions, what changed the pre-processing method, temperature, time, the kind and density | concentration of the catalyst to be used, etc. are prepared as mentioned above. Subsequently, each pretreated lignocellulosic biomass and enzyme are mixed and saccharified. Subsequently, the concentration of the fermentation inhibitor in the obtained saccharified solution is measured. As shown in Example 2 to be described later with respect to the concentration of the fermentation inhibitor, the target lignocellulosic biomass is added by changing the amount of yeast inoculated so that the concentration of yeast contained in the saccharified solution changes. It is evaluated whether or not the derived compound can be obtained up to the target fermentation yield.

  When the target lignocellulosic biomass-derived compound is obtained up to the target fermentation yield, the yeast cell concentration at this time is critical for the yeast cell concentration that does not undergo fermentation inhibition according to the concentration of the fermentation inhibitor. It can be judged as a value. The preset reference value may be a yeast cell concentration above the above critical value, for example, 1.0 to 3.0 times the above critical value, preferably 1.0 above the above critical value. Double to 2.5 times, more preferably 1.0 to 1.5 times the critical value is set as a preset reference value.

  In the production method of the present embodiment, as a more specific example, the relationship between the critical value and the furfural concentration when the fermentation inhibitor is furfural will be described below.

[Critical value: Concentration using the number of yeast cells]
In the manufacturing method of this embodiment,
The above critical value is represented by the concentration (CFU / mL) using the number of yeast cells,
When the concentration of furfural is X (g / L) and the above critical value is Y (CFU / mL), X and Y are represented by the following formula [1].

(In Formula [1], a is a number of 1.0 × 10 ⁷ or more and 4.0 × 10 ⁷ or less, and b is 2.0 × 10 ^6. )

  As in Example 2 described later, the furfural concentration X and the critical value Y can be expressed in a linear relationship.

In Formula [1], the slope a is preferably 1.0 × 10 ⁷ or more and 4.0 × 10 ⁷ or less, more preferably 1.5 × 10 ⁷ or more and 3.5 × 10 ⁷ or less. More preferably, it is 2.0 × 10 ⁷ or more and 3.0 × 10 ⁷ or less. When the slope a is within the above range, the target lignocellulosic biomass-derived compound can be efficiently obtained at the target fermentation yield in the presence of furfural.

In equation [1], the intercept b may be 2.0 × 10 ⁶ or more. The above value is the minimum number of yeast cells necessary for obtaining the target lignocellulosic biomass-derived compound up to the target fermentation yield when no furfural is contained in the saccharified solution.

[Critical value: Concentration using dry cell weight of yeast]
In the manufacturing method of this embodiment,
The above critical value is represented by the concentration (g / L) using the dry cell weight of yeast,
The number of yeast cells contained per gram of dry cells is 1.5 × 10 ¹⁰ CFU,
When the concentration of furfural is X (g / L) and the critical value is Y ′ (g / L), X and Y ′ are represented by the following formula [2].

(In Formula [2], c is a number between 0.5 and 2.5, and d is 0.13.)

The above critical value may be expressed by the dry cell weight of yeast. The number of yeast cells contained in 1 g of dried yeast cells varies slightly depending on the type of yeast, but is usually 0.75 × 10 ^{10 to} 3.0 × 10 ¹⁰ CFU, and 1.5 × 10 ¹⁰ CFU is preferred.

  In the formula [2], the slope c is preferably a number of 0.5 or more and 2.5 or less, more preferably a number of 0.75 or more and 2.25 or less, and 1.0 or more and 1.5 or less. More preferably, the number is as follows. When the slope c is within the above range, the target lignocellulosic biomass-derived compound can be efficiently obtained at the target fermentation yield in the presence of furfural.

  In equation [2], the intercept d may be 0.13 or more. The above value is the minimum dry cell weight necessary for obtaining the target lignocellulosic biomass-derived compound up to the target fermentation yield when no furfural is contained in the saccharified solution.

[Critical value: Ratio of solution containing yeast to be used to saccharified solution]
In the manufacturing method of this embodiment,
The above critical value is represented by the ratio of the solution containing yeast to be used to the saccharified solution,
The yeast cell concentration in the solution containing yeast is 2.0 × 10 ⁸ CFU / mL,
When the concentration of furfural is X (g / L) and the critical value is Y ′ ′ (g / L), X and Y ′ are represented by the following formula [5].

(In Formula [5], e is a number between 4.5 and 20.0, and f is 1.0.)

The above critical value may be expressed as a ratio of the solution containing yeast to be used to the saccharified solution. The concentration of yeast cells in the solution containing yeast may be adjusted as appropriate, but is usually 1 × 10 ^{8 to} 3 × 10 ⁸ CFU / mL and 2 × 10 ⁸ CFU / mL. Is preferred.

  In Formula [5], the slope e is preferably a number of 4.5 or more and 20.0 or less, more preferably 5.0 or more and 15.0 or less, and 7.5 or more and 10.0. More preferably, the number is as follows. When the slope e is within the above range, the target lignocellulosic biomass-derived compound can be obtained up to the target fermentation yield in the presence of furfural.

  In Formula [5], intercept f should just be 1.0 or more. The above value is the ratio of the solution containing the yeast to be used to the required saccharified liquid in order to obtain the target lignocellulosic biomass-derived compound up to the target fermentation yield when no furfural is contained in the saccharified liquid. The lowest value.

≪Process (B): Fermentation process≫
Subsequently, yeast is inoculated into the saccharified solution and saccharification residue obtained in the above step (A) and fermented. At this time, the yeast is inoculated so as to achieve the cell concentration determined in the above step (M). The fermentation temperature is preferably 25 ° C to 50 ° C, more preferably 28 ° C to 35 ° C, and particularly preferably 32 ° C. The fermentation time is preferably 24 hours to 120 hours, more preferably 24 hours to 96 hours, and further preferably 24 hours to 72 hours.

  In the production method of this embodiment, the yeast is not particularly limited as long as the target lignocellulose-based biomass-derived compound can be produced. As the yeast to be inoculated, a culture solution containing yeast may be used as it is, or a culture solution containing yeast concentrated by centrifugation or a dry one may be appropriately used. Moreover, what is necessary is just to calculate the quantity to inoculate from the relationship between said critical value and a fermentation inhibitory substance according to the state of yeast.

  About the process after a process (B), it can select suitably by the utilization method of a fermented liquor. For example, when the purpose is to obtain ethanol, a distillation step can be provided as a step of purifying the fermentation broth.

  In this embodiment, the lignocellulosic biomass-derived compound means a compound produced by ingestion of monosaccharides and oligosaccharides obtained by decomposing lignocellulosic biomass. For example, alcohols such as ethanol, butanol, 1,3-propanediol, 1,4-butanediol, glycerol, pyruvic acid, succinic acid, malic acid, itaconic acid, citric acid, lactic acid, organic acids, inosine, guanosine, etc. Examples thereof include nucleotides such as nucleoside, inosinic acid and guanylic acid, and diamine compounds such as cadaverine. When the compound obtained by fermentation is a monomer such as lactic acid, it may be converted into a polymer by polymerization.

<Production device for lignocellulosic biomass-derived compound>
FIG. 2 is a diagram showing a schematic configuration of a lignocellulose-based biomass-derived compound production apparatus in the present embodiment. In the lignocellulosic biomass-derived compound production apparatus 10 of this embodiment, a pipe 2 is disposed between the saccharification apparatus 1 and the fermenter 3.
Furthermore, the saccharification apparatus 1 may be provided with a pipe 4 for extracting a part of the saccharified solution. Moreover, the fermenter 3 may be provided with a yeast supply tank 5 for supplying yeast via the pipe 6.
Moreover, in FIG. 2, although the aspect in which the saccharification apparatus 1 and the fermenter 3 were separately arrange | positioned is illustrated, it is good also as one saccharification fermenter which performs saccharification reaction and fermentation reaction simultaneously.

The saccharification apparatus 1 is an apparatus for mixing pretreated lignocellulosic biomass and enzyme to perform saccharification, and there is no particular limitation. Examples thereof include a stirring type, aeration stirring type, a bubble column type, a fluidized bed type, and a packed bed type.
The pipe 4 is a pipe for extracting a part of the saccharified liquid from the saccharification apparatus 1 and measuring the concentration of the fermentation inhibiting substance in the saccharified liquid, and is not particularly limited. In addition, when measuring the concentration of a fermentation inhibitor in a liquid containing pretreated lignocellulosic biomass before saccharification or before saccharification and fermentation, or when the concentration of a fermentation inhibitor contained in a pretreatment condition can be calculated The pipe 4 may not be provided.

  In the production apparatus of this embodiment, when measuring the concentration of a fermentation inhibitor in a liquid containing pretreated lignocellulosic biomass before saccharification or saccharification and fermentation, the saccharification apparatus contains pretreated lignocellulosic biomass. A pipe for extracting a part of the liquid may be provided in the pipe for feeding the liquid. Thereby, the density | concentration of a fermentation inhibitory substance can be measured.

  The pipe 2 is a pipe for sending the saccharified solution and saccharification residue obtained in the saccharification apparatus 1 to the fermenter 3, and there is no special limitation.

The fermenter 3 is a tank for inoculating and fermenting yeast to the saccharified solution and saccharification residue obtained by the saccharification apparatus 1, and there is no special limitation. Examples thereof include a stirring type, aeration stirring type, a bubble column type, a fluidized bed type, and a packed bed type.
The yeast supply tank 5 is a tank for supplying yeast to the fermenter 3 and is not particularly limited. In addition, when the yeast in a dry state is directly inoculated into the fermentation tank 3, the yeast supply tank 5 may not be provided.

Furthermore, you may have the pre-processing apparatus for pre-processing lignocellulosic biomass before the saccharification apparatus 1. FIG. There is no particular limitation on the pretreatment device, for example, a heating pressure device having acid resistance or alkali resistance, or a form in which a container having acid resistance or alkali resistance is placed in a heating pressure device such as an autograver, etc. Can be mentioned.
Moreover, the equipment that follows the fermenter 3 can be appropriately selected according to the use of the fermentation broth.

  Hereinafter, the present invention will be described in more detail with reference to specific examples. However, the present invention is not limited to the following examples.

[Example 1]
(1) Saccharification step Using 10 g-dry of pretreated lignocellulosic biomass as an enzyme substrate, adding water and 0.04 to 0.2 g of NaOH as a pH adjuster, the pretreated biomass concentration is 10%. It diluted so that it might become mass%, and the substrate solution was prepared (total amount 100g). An enzyme derived from Trichoderma reesei was added to the substrate solution. The mixture was stirred at 50 ° C. for 48 hours. Immediately after the start of the saccharification process, 1.0 g each of the samples was collected 24 hours and 48 hours later, and the furfural concentration and ethanol concentration were measured using a high performance liquid chromatograph (LC-20AD manufactured by Shimadzu Corporation). In addition, immediately after the start of the saccharification process, samples were taken 1.0 g at 24 hours and 48 hours later, and subjected to high performance liquid chromatography (manufactured by SHIMADZU, HPLC reducing sugar system) and Asahipak MH2p-50 4E column (manufactured by shodex) Used to measure glucose and xylose concentrations.

(2) Fermentation Step To the saccharified solution obtained in (1), yeast (“Saccharomyces. Cereviviae” manufactured by Toyota Motor Corporation) is added at 1% by mass, 4.5% by mass, 10% with respect to the saccharified solution. It added so that it might become 20 mass% and 20 mass%, and it stirred by shaking at 32 degreeC for 48 hours. In addition, yeast was added in the state of a culture solution. The number of yeast cells contained in the culture solution was 2 × 10 ⁸ CFU / mL. Samples of 1.0 g were collected 24 hours and 48 hours after the start of the fermentation process, and the furfural concentration and ethanol concentration were measured using a high performance liquid chromatograph (LC-20AD manufactured by Shimadzu Corporation). In addition, samples were collected 1.0 g each 24 hours and 48 hours after the start of the fermentation process, using a high-performance liquid chromatograph (manufactured by SHIMADZU, HPLC reducing sugar system) and an Asahipak MH2p-50 4E column (manufactured by shodex). Then, the glucose concentration and the xylose concentration were measured.

(3) Results The changes in glucose concentration, xylose concentration, furfural concentration and ethanol concentration in the saccharification step and fermentation step are shown in FIG. From FIG. 3, when the ratio of the solution containing yeast to be used to the saccharified solution is 20%, it is clear that even if the furfural concentration is about 1.3 g / L, it can be stably fermented and ethanol can be obtained. It became.

[Example 2]
(1) Preparation of saccharified solution In advance, the concentration of furfural contained was 0 g / L, 0.44 g / L, 0.5 g / L, 0.54 g / L, 0.6 g / L, 0.62 g / L, and 1. The saccharified liquid prepared so that it might become 0g / L, 1.15g / L, 1.19g / L, 1.37g / L, 1.4g / L was prepared.

(2) Fermentation step For each saccharified solution obtained in (1), 1% by mass, 4.5% by mass of yeast (“Saccharomyces. Cereviviae” manufactured by Toyota Motor Corporation) with respect to the saccharified solution, It added so that it might become 10 mass% and 20 mass%, respectively, and it stirred by shaking at 32 degreeC for 48 hours. In addition, yeast was added in the state of a culture solution. The number of yeast cells contained in the culture solution was 2 × 10 ⁸ CFU / mL. Furfural concentration and ethanol concentration were measured by the same method as in Example 1 (2).

(3) Results The relationship between the fermentation yield and furfural concentration in the fermentation process is shown in FIG. From FIG. 4, when the furfural concentration is 0.54 g / L, the critical value of the yeast cell concentration that does not undergo fermentation inhibition according to the concentration of the fermentation inhibiting substance is 4.5%, and the furfural concentration is 0.00. When 98 g / L, the critical value was 10%, and when the furfural concentration was 1.37 g / L, the critical value was 20%.

  5A is a graph showing the relationship between the critical value and the furfural concentration, and FIG. 5B is a graph showing the relationship between the critical value and the furfural concentration replaced by the number of yeast cells. Yes, (C) is a graph showing the relationship between the above critical value replaced with the dry weight of yeast and the furfural concentration. In addition, a graph of a linear function as an approximate value was created using three points of critical values 0%, 4.5%, and 10%.

From the above, the ratio of the solution containing yeast to be used to the saccharified solution (mass%), the number of yeast cells (CFU / mL) and the dry weight of yeast (g / L) can be used. The critical value of can be expressed.
In addition, since the relationship between the actual critical value and the furfural concentration is a curve graph, the slope of each linear graph in FIG. 5 is 0.5 times to 2 times, preferably 0.75 times to If it is 1.5 times, it is thought that it is in the range of the critical value of the yeast cell density | concentration of the yeast which does not receive the fermentation inhibition according to the density | concentration of a fermentation inhibitory substance.

  According to the present invention, the yield of a lignocellulosic biomass-derived compound can be improved stably and efficiently in the presence of a fermentation inhibitor.

  DESCRIPTION OF SYMBOLS 1 ... Saccharification apparatus, 2,4,6 ... piping, 3 ... Fermenter, 5 ... Yeast supply tank, 10 ... Production apparatus of lignocellulosic biomass origin compound.

The present invention relates to a method for producing ethanol .

That is, the present invention is as follows.
(1) A method for producing ethanol ,
(A) mixing pre-treated lignocellulosic biomass and enzyme and saccharifying;
(B) a step of inoculating and fermenting yeast to the saccharified solution and saccharification residue obtained in the step (A),
The yeast is Saccharomyces cerevisiae,
Before step (A) or after step (A) and before step (B),
(M) In accordance with the concentration of furfural in the liquid containing the pretreated lignocellulosic biomass before the step (A) or in the saccharified liquid obtained in the step (A) A step of determining the yeast cell concentration in the step (B) so as to be a value,
The preset reference value is a yeast cell concentration that is not less than a critical value of the yeast cell concentration that does not undergo fermentation inhibition according to the furfural concentration,
In the said process (B), yeast is inoculated so that it may become the said cell density | concentration determined in the said process (M), The manufacturing method characterized by the above-mentioned.
(2) The method for producing ethanol according to (1), wherein the preset reference value is 1.0 to 3.0 times the critical value.
( 3 ) The critical value is a concentration using the number of yeast cells (CFU (Colony forming).
unit) / mL),
When the concentration of the furfural is X (g / L) and the critical value is Y (CFU / mL), the X and the Y are in a relationship represented by the following formula [1] (1) or (2 ) Production method of ethanol .

(In Formula [1], a is a number of 1.0 × 10 ⁷ or more and 4.0 × 10 ⁷ or less, and b is 2.0 × 10 ^6. )
( 4 ) The critical value is represented by the concentration (g / L) using the dry cell weight of yeast,
The number of yeast cells contained per gram of dry cells is 1.5 × 10 ¹⁰ CFU,
When the concentration of the furfural is X (g / L) and the critical value is Y ′ (g / L), the X and the Y ′ are in a relationship represented by the following formula [2] (1) or The method for producing ethanol according to (2) .

Claims (5)

A method for producing a lignocellulosic biomass-derived compound,
(A) mixing pre-treated lignocellulosic biomass and enzyme and saccharifying;
(B) a step of inoculating and fermenting yeast to the saccharified solution and saccharification residue obtained in the step (A),
Before step (A) or after step (A) and before step (B),
(M) Pre-set according to the concentration of the fermentation inhibitor in the liquid containing the pretreated lignocellulosic biomass before the step (A) or in the saccharified liquid obtained in the step (A). A step of determining the yeast cell concentration in the step (B) so as to be a reference value,
The preset reference value is a yeast cell concentration that is not less than a critical value of the yeast cell concentration that does not undergo fermentation inhibition according to the concentration of the fermentation inhibitor,
In the said process (B), yeast is inoculated so that it may become the said cell density | concentration determined in the said process (M), The manufacturing method characterized by the above-mentioned.   The method for producing a lignocellulosic biomass-derived compound according to claim 1, wherein the preset reference value is 1.0 to 3.0 times the critical value.   The method for producing a lignocellulosic biomass-derived compound according to claim 1 or 2, wherein the fermentation inhibitor is furfural. The critical value is represented by a concentration using the number of yeast cells (CFU (Colony forming unit) / mL),
The concentration of the furfural is X (g / L), and when the critical value is Y (CFU / mL), the X and the Y are in a relationship represented by the following formula [1]. A method for producing a lignocellulosic biomass-derived compound.

(In Formula [1], a is a number of 1.0 × 10 ⁷ or more and 4.0 × 10 ⁷ or less, and b is 2.0 × 10 ^6. ) The critical value is represented by the concentration (g / L) using the dry cell weight of yeast,
The number of yeast cells contained per gram of dry cells is 1.5 × 10 ¹⁰ CFU,
The X and the Y ′ are in a relationship represented by the following formula [2] when the concentration of the furfural is X (g / L) and the critical value is Y ′ (g / L). The manufacturing method of the lignocellulosic biomass origin compound of description.

(In Formula [2], c is a number between 0.5 and 2.5, and d is 0.13.)

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