Patent Application
20190292500
The present disclosure relates to improved processes of producing fermentation products from starch-containing material using a fermenting organism.
A vast number of commercial products that are difficult to produce synthetically are today produced by fermenting organisms. Such products include alcohols (e.g., butanol, ethanol, methanol, 1,3-propanediol); organic acids (e.g., acetic acid, citric acid, gluconate, gluconic acid, itaconic acid, lactic acid, succinic acid, 2,5-diketo-D-gluconic acid); ketones (e.g., acetone); amino acids (e.g., glutamic acid); gases (e.g., H2 and CO2), and more complex compounds, including, for example, antibiotics (e.g., penicillin and tetracycline); enzymes; vitamins (e.g., riboflavin, B12, beta-carotene); and hormones. Fermentation is also commonly used in the consumable alcohol (e.g., beer and wine), dairy (e.g., in the production of yogurt and cheese), leather, and tobacco industries.
Fermentation products, such as ethanol, are produced by first degrading starch-containing material into fermentable sugars by liquefaction and saccharification and then converting the sugars directly or indirectly into the desired fermentation product using a fermenting organism. Liquid fermentation products such as ethanol are recovered from the fermented mash (often referred to as “beer” or “beer mash”), e.g., by distillation, which separate the desired fermentation product from other liquids and/or solids. The remaining faction, referred to as “whole stillage”, is dewatered and separated into a solid and a liquid phase, e.g., by centrifugation. The solid phase is referred to as “wet cake” (or “wet grains” or “WDG”) and the liquid phase (supernatant) is referred to as “thin stillage”. Dewatered wet cake is dried to provide “Distillers Dried Grains” (DDG) used as nutrient in animal feed. Thin stillage is typically evaporated to provide condensate and syrup (or “thick stillage”) or may alternatively be recycled directly to the slurry tank as “backset”. Condensate may either be forwarded to a methanator before being discharged or may be recycled to the slurry tank. The syrup consisting mainly of limit dextrins and non-fermentable sugars may be blended into DDG or added to the wet cake before drying to produce DDGS (Distillers Dried Grain with Solubles).
Ethanol plants have struggled to maintain profitability, which is highly variable depending upon corn price, demand and price of DDGS, tax credits, gasoline consumption, ethanol exports, and changes to the Renewable Fuels Standard (RFS) mandates. New technologies for energy savings, higher yield of ethanol and higher value for co-products as well as various oil separation technologies contribute to the profitability of producing ethanol.
Therefore, there is a need for providing processes that can increase the yield of the fermentation product and thereby reduce the production costs. It is an object of the present invention to provide improved processes for producing fermentation products.
The present invention relates to processes of producing fermentation products from starch-containing material using a fermenting organism.
In one aspect, the present disclosure relates to methods of producing a fermentation product from starch containing material, said method comprising the steps of:
In another aspect, the present disclosure pertains to methods of producing a fermentation product, comprising
The object of the present disclosure is to provide methods/processes of producing fermentation products from starch-containing material using a fermenting organism.
In an advantageous embodiment, the present disclosure relates to methods of producing a fermentation product from starch containing material, said method comprising the steps of:
Stillage or Whole stillage is the product which remains after the mash has been converted to sugar, fermented and distilled into ethanol. Stillage can be separated into two fractions, such as, by centrifugation or screening: (1) wet cake (solid phase) and (2) the thin stillage (supernatant). The solid fraction or distillers' wet grain (DWG) can be pressed to remove excess moisture and then dried to produce distillers' dried grains (DDG). After ethanol has been removed from the liquid fraction, the remaining liquid can be evaporated to concentrate the soluble material into condensed distillers' solubles (DS) or dried and ground to create distillers' dried solubles (DDS). DDS is often mixed with DDG to form distillers' dried grain with solubles (DDGS). DDG, DDGS, and DWG are collectively referred to as distillers' grain(s).
In one embodiment of the present disclosure enzymes were added during and/or after the fermentation in the production process to the fermented mash and/or the fermentation medium and before the separation step like distillation, where the desired fermentation main product is separated from the rest of the fermented mash. The enzymes according to the present disclosure were capable of degrading components in the fermented mash (beer or beer mash) and/or the fermentation medium.
The phrase “fermentation media” or “fermentation medium” refers to the environment in which fermentation is carried out and comprises the fermentation substrate, that is, the carbohydrate source that is metabolized by the fermenting organism(s).
The fermentation medium may comprise other nutrients and growth stimulator(s) for the fermenting organism(s). Nutrient and growth stimulators are widely used in the art of fermentation and include nitrogen sources, such as ammonia; vitamins and minerals, or combinations thereof. Recovery Subsequent to fermentation, the fermentation product may be separated from the fermentation medium. The fermentation medium may be distilled to extract the desired fermentation product or the desired fermentation product may be extracted from the fermentation medium by micro or membrane filtration techniques. Alternatively, the fermentation product may be recovered by stripping. Methods for recovery are well known in the art.
The feedstock for producing the fermentation product may be any starch-containing material, preferably starch-containing plant material, including: tubers, roots, whole grain; and any combination thereof. The starch-containing material may be obtained from cereals. Suitable starch-containing material includes corn (maize), wheat, barley, cassava, sorghum, rye, potato, or any combination thereof. Corn is the preferred feedstock, especially when the fermentation product is ethanol. The starch-containing material may also consist of or comprise, e.g., a side stream from starch processing, e.g., C6 carbohydrate containing process streams that may not be suited for production of syrups. Whole stillage typically contains about 10-15 wt-% dry solids. Whole stillage components include fiber, hull, germ, oil and protein components from the starch-containing feedstock as well as non-fermented starch.
Production of a fermentation product is typically divided into the following main process stages:
a) Reducing the particle size of starch-containing material, e.g., by dry or wet milling;
b) Cooking the starch-containing material in aqueous slurry to gelatinize the starch,
c) Liquefying the gelatinized starch-containing material in order to break down the starch (by hydrolysis) into maltodextrins (dextrins);
d) Saccharifying the maltodextrins (dextrins) to produce low molecular sugars (e.g., DP1-2) that can be metabolized by a fermenting organism;
e) Fermenting the saccharified material using a suitable fermenting organism directly or indirectly converting low molecular sugars into the desired fermentation product;
f) Recovering the fermentation product, e.g., by distillation in order to separate the fermentation product from the fermentation mash.
As also explained in the “Background”-section above whole stillage is a by-product consisting of liquids and solids remaining after recovery (e.g. by distillation) of a desired fermentation product from fermented mash (beer mash). According to the invention the fermentation product may be any fermentation product, including alcohols (e.g., ethanol, methanol, butanol, 1,3-propanediol); organic acids (e.g., citric acid, acetic acid, itaconic acid, lactic acid, gluconic acid, gluconate, succinic acid, 2,5-diketo-D-gluconic acid); ketones (e.g., acetone); amino acids (e.g., glutamic acid); gases (e.g., H2 and CO2), and more complex compounds, including, for example, antibiotics (e.g., penicillin and tetracycline); enzymes; vitamins (e.g., riboflavin, B12, beta-carotene); and hormones. Fermentation is also commonly used in the consumable alcohol (e.g., beer and wine), dairy (e.g., in the production of yogurt and cheese), leather, and tobacco industries. In a preferred embodiment the fermentation product is a liquid, preferably an alcohol, especially ethanol.
As mentioned above, the starch-containing material may be obtained from cereals. Suitable starch-containing material includes corn (maize), wheat, barley, cassava, sorghum, rye, triticale, potato, or any combination thereof.
Corn is the preferred feedstock, especially when the fermentation product is ethanol. The starch-containing material may also consist of or comprise, e.g., a side stream from starch processing, e.g., C6 carbohydrate containing process streams that may not be suited for production of syrups. Beer components include fiber, hull, germ, oil and protein components from the starch-containing feedstock as well as non-fermented starch, yeasts, yeast cell walls and residuals. Production of a fermentation product is typically divided into the following main process stages: a) Reducing the particle size of starch-containing material, e.g., by dry or wet milling; b) Cooking the starch-containing material in aqueous slurry to gelatinize the starch, c) Liquefying the gelatinized starch-containing material in order to break down the starch (by hydrolysis) into maltodextrins (dextrins); d) Saccharifying the maltodextrins (dextrins) to produce low molecular sugars (e.g., DP1-2) that can be metabolized by a fermenting organism; e) Fermenting the saccharified material using a suitable fermenting organism directly or indirectly converting low molecular sugars into the desired fermentation product; f) Recovering the fermentation product, e.g., by distillation in order to separate the fermentation product from the fermentation mash.
As mentioned above beer (or fermented mash) is the fermentation product consisting of ethanol, other liquids and solids of a desired fermentation product. According to the invention the fermentation product may be any fermentation product, including alcohols (e.g., ethanol, methanol, butanol, 1,3-propanediol); organic acids (e.g., citric acid, acetic acid, itaconic acid, lactic acid, gluconic acid, gluconate, succinic acid, 2,5-diketo-D-gluconic acid); ketones (e.g., acetone); amino acids (e.g., glutamic acid); gases (e.g., H2 and CO2), and more complex compounds, including, for example, antibiotics (e.g., penicillin and tetracycline); enzymes; vitamins (e.g., riboflavin, B12, beta-carotene); and hormones. Fermentation is also commonly used in the production of consumable alcohol (e.g., spirits, beer and wine), dairy (e.g., in the production of yogurt and cheese), leather, and tobacco industries. In a preferred embodiment the fermentation product is a liquid, preferably an alcohol, especially ethanol. The beer contemplated according to the invention may be the product resulting from a fermentation product production process including above mentioned steps a) to f). However, the beer may also be the product resulting from other fermentation product production processes based on starch- and/or lignocellulose containing starting material.
The fermenting organism may be a fungal organism, such as yeast, or bacteria. Suitable bacteria may e.g. be Zymomonas species, such as Zymomonas mobilis and E. coli. Examples of filamentous fungi include strains of Penicillium species. Preferred organisms for ethanol production are yeasts, such as e.g. Pichia or Saccharomyces. Preferred yeasts according to the disclosure are Saccharomyces species, in particular Saccharomyces cerevisiae or baker's yeast.
Further, by adding the enzymes according to the present disclosure to the fermented mash or the fermentation medium before the distillation step is an advantage since the enzymes in the enzyme compositions are inactivated during the distillation.
Processes for producing fermentation products, such as ethanol, from a starch or lignocellulose containing material are well known in the art. The preparation of the starch-containing material such as corn for utilization in such fermentation processes typically begins with grinding the corn in a dry-grind or wet-milling process. Wet-milling processes involve fractionating the corn into different components where only the starch fraction enters into the fermentation process. Dry-grind processes involve grinding the corn kernels into meal and mixing the meal with water and enzymes. Generally two different kinds of dry-grind processes are used. The most commonly used process, often referred to as a “conventional process,” includes grinding the starch-containing material and then liquefying gelatinized starch at a high temperature using typically a bacterial alpha-amylase, followed by simultaneous saccharification and fermentation (SSF) carried out in the presence of a glucoamylase and a fermentation organism. Another well-known process, often referred to as a “raw starch hydrolysis” process (RSH process), includes grinding the starch-containing material and then simultaneously saccharifying and fermenting granular starch below the initial gelatinization temperature typically in the presence of an acid fungal alpha-amylase and a glucoamylase.
In a process for producing ethanol from corn, following SSF or the RSH process the ethanol is distilled from the whole mash after fermentation. The resulting ethanol-free slurry, usually referred to as whole stillage, is separated into solid and liquid fractions (i.e., wet cake and thin stillage containing about 35 and 7% solids, respectively). The thin stillage is often condensed by evaporation into a thick stillage or syrup and recombined with the wet cake and further dried into distillers' dried grains with solubles distillers' dried grain with solubles (DDGS) for use in animal feed.
In an embodiment of the present disclosure the xylanase may preferably be of microbial origin, such as of fungal origin (e.g., Aspergillus, Fusarium, Humicola, Meripilus, Trichoderma) or from a bacterium (e.g., Bacillus). In a preferred embodiment the xylanase is derived from a filamentous fungus, preferably derived from a strain of Aspergillus, such as Aspergillus aculeatus; or a strain of Humicola, preferably Humicola lanuginosa. Examples of xylanases useful in the methods of the present invention include, but are not limited to, Aspergillus aculeatus xylanase (GeneSeqP:AAR63790; WO 94/21785), Aspergillus fumigatus xylanases (WO 2006/078256), and Thielavia terrestris NRRL 8126 xylanases (WO 2009/079210). The xylanase may preferably be an endo-1,4-beta-xylanase, more preferably an endo-1,4-beta-xylanase of GH 10 or GH 1 1. Examples of commercial xylanases include SHEARZYME™, BIOFEED WHEAT™, HTec and HTec2 from Novozymes A/S, Denmark.
Examples of beta-xylosidases useful in the methods of the present invention include, but are not limited to, Trichoderma reesei beta-xylosidase (UniProtKB/TrEMBL accession number Q92458), Talaromyces emersonii (SwissProt accession number Q8X212), and Neurospora crassa (SwissProt accession number Q7SOW4).
Examples of suitable bacterial xylanases include xylanases derived from a strain of Bacillus, such as Bacillus subtilis, such as the one disclosed in U.S. Pat. No. 5,306,633.
Contemplated commercially available xylanases include SHEARZYM E™, BIOFEED WHEAT™, (from Novozymes AJS), Econase CE™ (from AB Enzymes), Depol 676™ (from Biocatalysts Ltd.) and SPEZYME™ CP (from Genencor Int.).
Xylanase may be added in an amount effective in the range from 0.16×106-460×106 Units per ton beer mash or fermentation medium.
Example for the determination of Xylanase Activity (FXU)
The endoxylanase activity is determined by an assay, in which the xylanase sample is incubated with a remazol-xylan substrate (4-O-methyl-D-glucurono-D-xylan dyed with Remazol Brilliant Blue R, Fluka), pH 6.0. The incubation is performed at 50° C. for 30 min. The background of non-degraded dyed substrate is precipitated by ethanol. The remaining blue colour in the supernatant is determined spectrophotometrically at 585 nm and is proportional to the endoxylanase activity.
The endoxylanase activity of the sample is determined relatively to an enzyme standard.
The pectinase used in the methods according to the present disclosure may be any pectinase, in particular of microbial origin, in particular of bacterial origin, such as a pectinase derived from a species within the genera Bacillus, Clostridium, Pseudomonas, Xanthomonas and Erwinia, or of fungal origin, such as a pectinase derived from a species within the genera Trichoderma or Aspergillus, in particular from a strain within the species A. niger and A. aculeatus. Contemplated commercially available pectinases include Pectinex Ultra-SPL™ (from Novozymes), Pectinex Ultra Color (from Novozymes), Rohapect Classic (from AB Enzymes), Rohapect 10 L (from AB Enzymes). Pectinase may be added in an amount effective in the range from 1.4×109-23500×109 Units per ton beer mash or fermentation medium.
The method is based on the enzyme's degradation of a pectin solution by a transeliminase reaction, the double bonds formed result in an increase in the absorption at 238 nm which is followed by a spectrophotometer.
pH: 3.50±0.02
Enzyme concentration: 1.9-2.3 PECTU/mL
Reaction time: 6 minutes
Measuring time: 5 minutes
The activity is determined relative to a PECTU standard. The result is given in the same units as for the standard, which is designated: PECTU-Pectintranseliminase Unit.
The term “alpha-amylase” means an alpha-1,4-glucan-4-glucanohydrolase (E.C. 3.2.1.1) that catalyzes the hydrolysis of starch and other linear and branched 1,4-glucosidic oligo- and polysaccharides.
In an embodiment, the xylanase is added in an amount of 1-30, e.g., 5-30 7-25, 10-20, 10-17, or 12-15 micrograms/g dry solids.
In an embodiment, the pectinase is added in an amount of 0.01-1.0, e.g., 0.015-0.08, 0.015-0.06, 0.015-0.04, or 0.02-0.03 FXU/g dry solids.
The saccharification and fermentation steps may be carried out either sequentially or simultaneously. The xylanase and the pectinase may be added during saccharification and/or after fermentation when the process is carried out as a sequential saccharification and fermentation process and before or during fermentation when steps (b) and (c) are carried out simultaneously (SSF process).
As mentioned above, the fermenting organism is preferably yeast, e.g., a strain of Saccharomyces cerevisiae or Saccharomyces diastaticus. In an advantageous embodiment a yeast strain of Saccharomyces diastaticus is used (SIHA Amyloferm®, E. Begerow GmbH&Co, Langenlonsheim, Germany) since their exo-amylase activity can split liquid starch and also dextrin, maltose and melibiose.
In the liquefaction step the gelatinized starch (downstream mash) is broken down (hydrolyzed) into maltodextrins (dextrins). To achieve starch hydrolysis a suitable enzyme, preferably an alpha-amylase, is added. Liquefaction may be carried out as a three-step hot slurry process. The slurry is heated to between 60-95° C., preferably 80-85° C., and an alpha-amylase may be added to initiate liquefaction (thinning). Then the slurry may be jet-cooked at a temperature between 95-140° C., preferably 105-125° C., for about 1-15 minutes, preferably for about 3-10 minutes, especially around about 5 minutes. The slurry is cooled to 60-95° C. and more alpha-amylase may be added to complete the hydrolysis (secondary liquefaction). The liquefaction process is usually carried out at a pH of 4.0 to 6.5, in particular at a pH of 4.5 to 6.
The saccharification step and the fermentation step may be performed as separate process steps or as a simultaneous saccharification and fermentation (SSF) step. The saccharification is carried out in the presence of a saccharifying enzyme, e. g. a glucoamylase, a beta-amylase or maltogenic amylase. Optionally a phytase and/or a protease is added.
Saccharification may be carried out using conditions well known in the art with a saccharifying enzyme, e.g., beta-amylase, glucoamylase or maltogenic amylase, and optionally a debranching enzyme, such as an isoamylase or a pullulanase. For instance, a full saccharification process may last up to from about 24 to about 72 hours, however, it is common to do a pre-saccharification for typically 40-90 minutes at a temperature between 30-65° C., typically about 60° C., followed by complete saccharification during fermentation in a simultaneous saccharification and fermentation process (SSF process). Saccharification is typically carried out at a temperature from 20-75° C., preferably from 40-70° C., typically around 60° C., and at a pH between 4 and 5, normally at about pH 4.5.
The most widely used process to produce a fermentation product, especially ethanol, is the simultaneous saccharification and fermentation (SSF) process, in which there is no holding stage for the saccharification, meaning that a fermenting organism, such as a yeast, and enzyme(s), including the hemicellulase(s) and/or specific endoglucanase(s), may be added together. SSF is typically carried out at a temperature from 25° C. to 40° C., such as from 28° C. to 35° C., from 30° C. to 34° C., preferably around about 32° C. In an embodiment, fermentation is ongoing for 6 to 120 hours, in particular 24 to 96 hours.
During and/or after the fermentation, the fermented mash is subjected to an enzyme composition according to the present disclosure. In an embodiment, the enzyme composition comprises a xylanase and a pectinase.
In a particular embodiment, the process of the present disclosure further comprises, prior to liquefying the starch-containing material the steps of:
The aqueous slurry may contain from 10-55 w/w % dry solids (DS), preferably 25-45 w/w % dry solids (DS), more preferably 30-40 w/w % dry solids (DS) of the starch-containing material. The slurry is heated to above the gelatinization temperature and an alpha-amylase, preferably a bacterial and/or acid fungal alpha-amylase, may be added to initiate liquefaction (thinning). The slurry may be jet-cooked to further gelatinize the slurry before being subjected to an alpha-amylase in step (a).
In a preferred embodiment, the starch containing material is milled cereals, preferably barley or corn, and the methods comprise a step of milling the cereals before step (a). In other words, the disclosure also encompasses methods, wherein the starch containing material is obtainable by a process comprising milling of cereals, preferably dry milling, e. g. by hammer or roller mils. Grinding is also understood as milling, as is any process suitable for opening the individual grains and exposing the endosperm for further processing. Two processes of milling are normally used in alcohol production: wet and dry milling. The term “dry milling” denotes milling of the whole grain. In dry milling the whole kernel is milled and used in the remaining part of the process Mash formation. The mash may be provided by forming a slurry comprising the milled starch containing material and brewing water. The brewing water may be heated to a suitable temperature prior to being combined with the milled starch containing material in order to achieve a mash temperature of 45 to 70° C., preferably of 53 to 66° C., more preferably of 55 to 60° C. The mash is typically formed in a tank known as the slurry tank.
Subsequent to fermentation the fermentation product may be separated from the fermentation medium. The slurry may be distilled to extract the desired fermentation product or the desired fermentation product from the fermentation medium by micro or membrane filtration techniques. Alternatively the fermentation product may be recovered by stripping. Methods for recovering fermentation products are well known in the art. Typically, the fermentation product, e.g., ethanol, with a purity of up to, e.g., about 96 vol. % ethanol is obtained.
Thus, in one embodiment, the methods of the disclosure further comprise distillation to obtain the fermentation product, e.g., ethanol. The fermentation and the distillation may be carried out simultaneously and/or separately/sequentially; optionally followed by one or more process steps for further refinement of the fermentation product.
Further details on how to carry out liquefaction, saccharification, fermentation, distillation, and recovering of ethanol are well known to the skilled person.
The fermentation product(s) can be optionally recovered from the fermentation medium using any method known in the art including, but not limited to, chromatography, electrophoretic procedures, differential solubility, distillation, or extraction. For example, alcohol is separated from the fermented cellulosic material and purified by conventional methods of distillation as mentioned above. Ethanol with a purity of up to about 96 vol. % can be obtained, which can be used as, for example, fuel ethanol, drinking ethanol, i.e., potable neutral spirits, or industrial ethanol.
The inventions described and claimed herein are not to be limited in scope by the specific embodiments herein disclosed, since these embodiments are intended as illustrations of several aspects of the invention. Any equivalent embodiments are intended to be within the scope of this invention. Indeed, various modifications of the invention in addition to those shown and described herein will become apparent to those skilled in the art from the foregoing description. Such modifications are also intended to fall within the scope of the appended claims. In the case of conflict, the present disclosure including definitions will control. Various references are cited herein, the disclosures of which are incorporated by reference in their entireties. The present invention is further described by the following examples which should not be construed as limiting the scope of the invention.
The effectiveness of any fermentative process is defined by the production rate of the target product. Therefore increasing the fermentative production rate of ethanol, i.e. the acceleration of ethanol production is highly economical.
For that example the ethanol production of the fermentation process in presence and absence of additional enzymes accelerating ethanol concentration were tested.
Three different setups were tested.
In the first fermentor (Fermentor#1) the fermentation cultivation was not treated with enzymes (0 g/t xylanase; 0 g/t pectinase), in the second and third fermentor (Fermentor#2 to #3) the fermentation cultivation was treated with the enzyme composition comprising a xylanase and a pectinase from the beginning of the fermentation in different concentrations (from 75 g/t to 200 g/txylanase and from 75 g/t to 200 g/t pectinase).
The trials were performed in 2 L fermentation scale. Samples were taken during the fermentation process and the concentrations of ethanol was determined by HPLC.
In one embodiment, the process of the production of ethanol from corn was performed as follows:
a) Reducing the particle size of the starch-containing material by milling
The enzyme stock was transferred into a 50 mL tube and then stored at 4° C. until use within one hour.
DNSA solution: For the DNSA solution the following compounds were used:
Substrates: Polygalacturonic acid (Sigma 81325)
Substrates were dissolved in buffer to a concentration of 0.8% (w/v)
Buffer: 50 mM sodium acetate, pH 4.5
For the assay 96 well PCR microtiter plates (company Greiner) were used. The enzymes were diluted in buffer. 90 μl substrate and 10 μl enzyme solution were mixed. A blank was measured replacing enzyme solution with water. Incubation was carried out for 30 min at 37° C., followed by a 5 minute enzyme inactivation step at 99° C. and followed by cooling for 10 min at 4° C. In a second 96 well PCR microtiter plates (company Greiner) 50 μl of the incubated substrate-enzyme mix was incubated with 50 μl of the DNSA solution at 98° C. for 10 minutes and then cooled to 4° C. and incubated for 5 minutes at 4° C.
100 μl of the reaction was transferred into a well of 96 well transparent, flat bottom micro titer plate and the adsorption was measured at 540 nm by a micro titer plate reader (Tecan M1000).
Substrates: Xylan from birchwood (Sigma X0502)
Substrate was dissolved in buffer to a concentration of 1.5% (w/v)
Buffer: 100 mM sodium acetate, pH 5.0 containing 20 mM CaCl2 and 0.4 g/L Tween20
For the assay 96 well PCR microtiter plate (company Greiner) were used. The enzymes were diluted in buffer. 90 μl substrate and 10 μl enzyme solution were mixed. A blank was measured replacing enzyme solution with water. Incubation was carried out for 20 min at 40° C., followed by a 5 minute enzyme inactivation step at 99° C. and followed by cooling for 5 min at 4° C. 45.5 μL of the DNSA solution was added to the 96 well PCR microtiter plate by a multidrop (company Fisher-Scientific) and then the plate was incubated for 98° C. for 10 minutes and cooled to 4° C. and incubated for 5 minutes at 4° C.
100 μl of the reaction was transferred into well of a new 96 well transparent, flat bottom micro titer plate and then the adsorption was measured at 540 nm by a micro titer plate reader (Tecan M1000).
The activity is calculated as Units per μl or mg of enzyme product. 1 unit is defined as the amount of formed reducing ends in μmol per minute. The enzyme activities are shown in Table 1.
Frozen samples of the fermentation process were thawed up and the ethanol concentrations in the fermentation samples were measured by HPLC. Fermentation samples were centrifuged at 20000 g at 10° C. for 15 minutes and the supernatant was transferred into HPLC vials. The samples (30 μL) were injected into a VWR/Hitachi equipment comprising the isocratic pump L-2130, the auto-sampler L-2200, the column oven L-2350, the refractic index detector L-2490 and a degasser at 10° C. The EZ Chrome Elite 3.3.1 software was used. The VWR/Hitachi HPLC was equipped with a Rezex ROA Organic Acid H+ (8%) LC column (300×7.8 mm, Phenomenex, Torance Calif.) and a guard column (carbo-H 4×3.0 mm, Phenomenex, Torance Calif.). The column was eluted with 0.0025 M H2SO4 at 0.45 mL/min flow rate at 60° C. The system was standardized by a 6-point calibration ethanol standard (100 g/L, 50 g/L, 25 g/L, 12.5 g/L, 6,125 g/L and 0 g/L ethanol).
Table 2 and
| Number | Date | Country | Kind |
|---|---|---|---|
| 13156260.5 | Feb 2013 | EP | regional |
| 14179841.3 | Aug 2014 | EP | regional |
| 14179848.8 | Aug 2014 | EP | regional |
| 14179851.2 | Aug 2014 | EP | regional |
This is a continuation in part of U.S. patent application Ser. No. 15/501,563, filed Feb. 3, 2017, which is a US national phase application under 35 U.S.C. § 371 of international application no. PCT/EP2015/064101, filed Jun. 23, 2015, which claims benefit of priority to EP application no. 14179848.8, filed Aug. 5, 2014, and U.S. provisional application No. 62/033,338, filed Aug. 5, 2014, now expired; the entire content of each is herein incorporated by reference in its entirety. This is also a continuation in part of U.S. patent application Ser. No. 15/501,574, filed Feb. 3, 2017, which is a US national phase application under 35 U.S.C. § 371 of international application no. PCT/EP2015/064179, filed Jun. 24, 2015, which claims benefit of priority to EP application no. 14179851.2, filed Aug. 5, 2014, and U.S. provisional application No. 62/033,327, filed Aug. 5, 2014, now expired; the entire content of each is herein incorporated by reference in its entirety. This is also a continuation in part of U.S. patent application Ser. No. 16/357,903, filed Mar. 19, 2019, which is a continuation in part of U.S. patent application Ser. No. 15/501,533, filed Feb. 3, 2017, now abandoned, which is a US national phase application of PCT/EP2015/064090, filed Jun. 23, 2015, which claims priority to U.S. provisional patent application No. 62/033,349, filed Aug. 5, 2014, now expired, and European patent application no. 14179841.3, filed Aug. 5, 2014. Each application cited in this paragraph is herein incorporated by reference in its entirety. U.S. patent application Ser. No. 16/357,903 is also a continuation in part of U.S. patent application Ser. No. 14/767,148, filed Aug. 11, 2015, which is a US national phase application of PCT/EP2013/055918, filed Mar. 21, 2013, which claims priority to European patent application no. 13156260.5, filed Feb. 21, 2013. Each application cited in this paragraph is herein incorporated by reference in its entirety. U.S. patent application Ser. No. 16/357,903 is also a continuation in part of U.S. patent application Ser. No. 14/627,753, filed Feb. 20, 2015, which is a continuation of U.S. patent application Ser. No. 13/995,079, now U.S. Pat. No. 8,962,286, which is a US national phase application of PCT/EP2011/006473 filed Dec. 21, 2011, which claims benefit of priority to U.S. provisional patent application Ser. No. 61/425,893 filed Dec. 22, 2010, now expired. Each application cited in this paragraph is herein incorporated by reference in its entirety.
| Number | Date | Country | |
|---|---|---|---|
| 62033338 | Aug 2014 | US | |
| 62033327 | Aug 2014 | US | |
| 62033349 | Aug 2014 | US | |
| 61425893 | Dec 2010 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 13995079 | Aug 2013 | US |
| Child | 14627753 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 15501563 | Feb 2017 | US |
| Child | 16431356 | US | |
| Parent | 15501574 | Feb 2017 | US |
| Child | 15501563 | US | |
| Parent | 16357903 | Mar 2019 | US |
| Child | 15501574 | US | |
| Parent | 15501533 | Feb 2017 | US |
| Child | 16357903 | US | |
| Parent | 14767148 | Aug 2015 | US |
| Child | 16357903 | US | |
| Parent | 14627753 | Feb 2015 | US |
| Child | 16357903 | US |
