WO1994013826A1 - Procede ameliore de pretraitement pour la production d'acide lactique - Google Patents

Procede ameliore de pretraitement pour la production d'acide lactique Download PDF

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Publication number
WO1994013826A1
WO1994013826A1 PCT/US1993/011759 US9311759W WO9413826A1 WO 1994013826 A1 WO1994013826 A1 WO 1994013826A1 US 9311759 W US9311759 W US 9311759W WO 9413826 A1 WO9413826 A1 WO 9413826A1
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starch
lactic acid
glucose
containing material
material mixture
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PCT/US1993/011759
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English (en)
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Tenlin S. Tsai
Cynthia S. Millard
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University Of Chicago
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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
    • C12P19/00—Preparation of compounds containing saccharide radicals
    • C12P19/14—Preparation of compounds containing saccharide radicals produced by the action of a carbohydrase (EC 3.2.x), e.g. by alpha-amylase, e.g. by cellulase, hemicellulase
    • 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
    • C12P7/40—Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
    • C12P7/56—Lactic acid
    • 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
    • C13K1/06—Glucose; Glucose-containing syrups obtained by saccharification of starch or raw materials containing starch

Definitions

  • This invention generally relates to the bioconversion of industrial food waste containing starch to lactic acid suitable for conversion to photodegradable or biodegradable plastics More particularly, this invention relates to a pretreatment process for the bioconversion of high carbohydrate, or starch containing materials such as potato waste, cheese whey or the like into lactic acid.
  • Cheese whey permeate which contains lactose rather than starch can also be used with slight modifications
  • Lactic acid is one of the products which can potentially be extremely useful in industry From lactic acid can be made various degradable plastics.
  • Lactic acid can be bioconverted directly from cheese whey permeate, cane and beet sugars using various lactic acid bacteria, such as Lactobacilli, in relatively high yields or indirectly by first hydrolyzing the starch in corn, potato or rice followed by bioconversions with lactic acid bacteria.
  • Lactic acid and its sodium or calcium salts are non-toxic and are classified as GRAS (Generally Recognized As Safe) by the FDA.
  • the cytolase is preferably the 123 formulation which is added to the starch waste
  • the material is subjected to a blending operation to reduce viscosity, and the blended material is allowed to incubate about 2-3 hours at about 60°C before the conversion process is started This process results in an improved yield of glucose in the order of 10-30% for waste with peels and 5-10% for waste without peels
  • Overall conversion levels are in the range of about 95-97%
  • the mixed culture, code-named LBM5 is preferably composed ofL delbrueckii subsp lactis ATCC 12315, L casei NRRL B-1445, L delbrueckii NRLL B-445, L helveticus NRRL B-1937, and L casei NRRL B-1922 Acclimation techniques were used to improve growth temperature and product tolerance of the strains before the mixed culture was composed Individually, L delbrueckii subsp lactis ATCC 12315 was the most preferred strain in terms of batch fermentation rate The mixed culture LBM5 exhibited a reduced batch fermentation time compared with L delbrueckii subsp. lactis ATCC 12315 This difference is likely due to symbiosis The mixed culture LBM5 was also found to be able to maintain cell viability at high lactate concentration
  • the starch-containing material such as a homogenized potato waste
  • alpha-amylase enzyme is first liquefied by alpha-amylase enzyme at an elevated temperature in the range of from about 90°C to about 130°C for a time no less than about 15 minutes
  • the step also sterilizes or pasteurizes the material to control microbial contamination during fermentation
  • the temperature of the liquefied material is then lowered to about 42°C and the pH adjusted to about 5 5
  • glucoamylase enzyme, lactic acid bacteria and nutrients are added at effective concentrations to effect simultaneous conversions of liquefied starch to glucose and glucose to lactic acid, catalyzed by glucoamylase and the bacteria, respectively
  • the combined process reduces the total process time for conversion of starch to lactic acid It can also reduce the capital and operating costs of the process Simultaneous
  • the hydrolyzed starch such as the potato hydrolysate prepared from potato wastes or the commercially available glucose syrup from corn processors, normally contains up to 5% of impurity sugars such as maltose and oligosaccharides.
  • the impurity sugars tend to remain unutilized at the end of fermentation and cause difficulties in product purification.
  • This invention provides a method of reducing the broth impurity sugar levels by adding carbohydrases during fermentation.
  • Carbohydrases such as maltase and glucoamylase, can convert maltose and oligosaccharides into glucose which is readily consumed by the microorganisms. Also, with this invention the fermentation process can accept a "bad" (incompletely hydrolyzed) batch of material, which contains higher than normal levels of sugar impurities and is normally unsuitable for fermentation. This will allow one to use less stringent quality control methods and criteria for the hydrolysis process and thus improve the economics of the whole process.
  • a nutrient formulation that has yielded satisfactory results comprises the following: 2g/L KH2PO4, 5 g L sodium acetate, 10 g/L trypticase peptone, 5 g/L yeast extract, 3 g/L tryptose, lml/L Tween 80, 0.573 g/L MgS ⁇ 4*7H 2 0, 0.034 g/L FeSO 4 7H 2 O, and 0.12 g/L MnSO 4 .
  • STLM-B comprises the following: 3 g/L KH PO , 3 g/L K2HPO4, 1 g/L sodium acetate, 10 g/L trypticase peptone, 5 g/L yeast extract, 3 g/L tryptose, 1 ml/L Tween 80, 229 mg/L L-cystein-HCl*H 2 O, 0.573 g/L MgSO 4 7H 2 O, 0.034 g/L FeSO 7H 2 O, and 0.12 g/L MnSO .
  • the configuration of the continuous bioreactor system can be a single stage or a two-stage bioreactor.
  • Cell recycle effected by a membrane filter or a continuous centrifuge, would be preferred to increase cell concentration and thus increase the volumetric productivity of the bioreactor.
  • a single stage system is more simplistic, a two-stage system may favor cell viability at high product concentrations, at the expense of increased system complexity. If a two-stage system is employed, it would be particularly advantageous to operate the system in a manner that the lactate concentration in the first stage is below the critical concentration that would inhibit cell growth, and the recycled cell mass from the second stage is fed into the first stage.
  • the electrodialytic cell is divided by ion-exchange membranes into separate compartments.
  • lactate ions in the fermentation broth migrate through an anion-exchange membrane into a product compartment and are recovered as a free acid solution and sent for further processing.
  • Sodium ions migrate through a cation-exchange membrane, resulting in a sodium hydroxide stream which can be recycled for pH control in fermentation or other uses in the plant.
  • the hydrogen and hydroxide ions needed for the balance of electrical charges in the lactic acid and sodium hydroxide compartments can be provided either by electrolysis of water in the electrode compartments in a conventional electrodialysis system or by water splitting in the bipolar membrane.
  • Primary considerations in the electrodialysis process include: membrane transfer area requirement, energy consumption, yield of recovery, lactic acid purity and lactic acid concentration.
  • the obtainable lactic acid purity is affected by the characteristics of the anion- exchange membrane.
  • a "tighter" membrane such as Ionics Corp.'s 204-UZRA-412 or equivalent conventional membrane is preferred for high lactic acid purity, although other membranes, such as, Ionics' 103-QZL-386 are also satisfactory.
  • the lactic acid product concentration can be affected by manipulating the volume ratio of the feed and product streams.
  • the membrane transfer area requirement (capital costs) and the energy consumption (operating costs) are inversely correlated. In general, the optimal conditions need to be determined case by case with considerations of the economics of the particular plant.
  • the electrodialysis product can be concentrated to about 35% by vacuum evaporation at 60-70°C, resulting in a concentrated crude acid.
  • Lactic acid can be further purified by liquid-liquid extraction followed by back-extraction.
  • the process involves contacting the crude lactic acid with an extractant (such as a tertiary amine in a water- immiscible organic solvent) and back-extracting the lactic acid from the extractant using a concentrated alkali solution (such as sodium hydroxide) resulting in a lactate salt (e.g., sodium lactate).
  • the lactate solution can then be processed by electrodialysis to recover the alkali solution and a purified lactic acid.
  • the process effectively reduces the level of total impurity which can interfere with certain end applications, such as synthesis of poly-lactic acid.
  • a mineral acid such as sulfuric acid
  • ion-exchange In the former case, the mineral acid is co-extracted with lactic acid and contaminates the product.
  • Electrodialysis acid ifies the fermentation broth without generating these problems. Also, extraction of the acidified fermentation broth directly often suffers from phase separation problems due to formation of precipitates at the interface or stable emulsion caused by certain impurities.
  • Electrodialysis removes many impurities and thus eliminates the phase separation problems.
  • extracting from a concentrated (e.g., lactic acid) stream compared to a dilute stream (e.g., an acidified fermentation broth containing about 10% lactic acid) has other advantages, such as, generating a smaller volume of a solvent-contaminated spent broth wastestream and ease of operation.
  • Another further object of the invention is to provide a process for converting industrial food waste to glucose and then to lactic acid by the use of both enzyme and microbiological action, wherein the processing time to produce over 90% glucose is reduced to less than ten hours and the subsequent process time is less than about forty-eight hours to produce lactic acid from the glucose.
  • Yet another object of the invention is to convert industrial starchy waste into lactic acid while providing a glucose intermediate product which is substantially devoid of microbial contamination.
  • FIGURES 1 A and IB illustrate process flow diagrams in accordance with the invention.
  • FIGS. 1 A and IB A flow diagram of the preferred process of pretreating and converting the potato waste to high purity lactic acid is given in FIGS. 1 A and IB.
  • the potato waste 100 is fed to the homogenizer 104 which can be a hammer mill or Rietz mill, to produce a potato waste homogenate 106
  • the starch slurry 1 10 (or the homogenate 106 directly, if starch separation is omitted) is pumped to a pretreatment station 11 1 wherein the pH is adjusted to almost 5 0 with an acid, such as 5M HC1 Cytolase (preferably a Cytolase 123, or its equivalent, manufactured by Genecor Inc ) is added to the starch slurry 1 10 or the homogenate 106 and blended thoroughly Approximately 0.03g (m
  • This mixture is incubated at 60°C for about three hours, and is mixed occasionally with the mixture having steadily reduced viscosity over the incubation time period.
  • the pretreated mixture is then pumped the liquefaction unit 112 to produce a liquefied starch 114, which is charged to the fermenter 116 for simultaneous saccharification and fermentation.
  • Use of this enzyme allows the mixture to have the proper viscosity without having to add water which would dilute the mixture. Such an unnecessary dilution would reduce the reaction rate and slow the processing
  • the liquefied starch 114 is sent to a saccharification unit 117 to produce a glucose syrup before it is fed into the fermenter 116. Also fed into the fermenter 116 are the microbial inoculum 118 and nutrients 120. During fermentation, a sodium hydroxide solution 122 is added to the fermenter for pH control.
  • the fermentation broth 124 containing cell mass and sodium lactate is processed by a cell separator 126 which can be a centrifuge or a membrane micro- or ultra-filtration device, to produce a cell-free broth 128 containing sodium lactate solution and a cell mass concentrate 130.
  • the fermenter and separator units can be operated in a batch or continuous mode. In the batch mode, all the cell mass concentrate 130 goes to waste 132. In the continuous mode, part of the cell mass concentrate 130 is recycled to the fermenter 110 and part of it goes to waste 132. If desired, a filtration device can be used to further recover the product (sodium lactate solution) from the wastestream 132.
  • the cell-free broth 128 is fed to the primary recovery unit (electrodialysis) 134 to generate a sodium hydroxide solution 122 which is recycled for fermentation pH control, and a crude lactic acid 136 which is further concentrated in a vacuum evaporator 138.
  • the concentrated crude lactic acid 140 produced from the vacuum evaporator 138 is further processed in the purification process 142 to produce a purified lactic acid 160.
  • the purification process 142 can be esterification or extraction. If esterification is used (see dotted lines on flow diagram) the process includes an esterification reactor 146, a hydrolysis tank 148, and distillation columns 150 for separation of lactic acid. If extraction is used, the process includes a contactor 152 for extraction, a phase- separator 154, a second contactor 156 for back-extraction, and an acidification device 158.
  • the purified lactic acid 160 is fed into the polishing unit 162, which may include treatment by ion-exchange resins and activated carbon.
  • the polished lactic acid 164 is further concentrated in the final evaporation 166 to generate the final product 168, a high purity lactic acid.
  • a pretreatment of potato waste homogenate or starch slurry was performed by adjusting pH to 5.0 with 5M H Cl. Cytolase 123 was added and blended into the starch slurry or homogenate. About 0.03g (ml) per gram of dry substance was added. The blended sample was poured into a large container holding at least twice as much volume as the material mixture. The mixture was incubated for three hours at 60°C and was mixed about once an hour. Subsequent to the pretreatment step liquefaction is carried out and other processing in accordance with the following examples.
  • Example 2 Five lactic acid bacterial strains, L. delbrueckii subsp. lactis ATCC 12315, L. casei NRRL B-1445, L. delbrueckii NRRL B-445, L. helveticus NRRL B-1937, and L. casei NRRL B-1922, were mixed in equal parts to form the mixed culture code-named LBM5.
  • a batch fermentation with STLM-B medium was carried out in a 3-L fermenter. An inoculum grown in the shake-flask for about 12 h was used at 10% (v/v) inoculum size. The fermentation temperature was controlled at 42°C. The pH of the medium was 6.3 initially and was allowed to drop to 5.5 as lactic acid was produced.
  • Example 2 In another batch fermentation of LBM5 performed as in Example 2, the inoculum was cultivated in a seed bioreactor at controlled pH of 5.5 to maintain a highly active state. The fermentation progressed rapidly and the initial 1 10 g/L of glucose was completely utilized in 18.6 h, resulting in further improved batch productivity of 5.3 g/(L , h). In both fermentations, the mixed culture exhibited a high stereospecificity and 98% of the lactic acid produced was the L-lactic acid.
  • the mixed culture LBM5 was tested in a chemostat at a moderate dilution rate (0.05 h ⁇ ) and at high lactic acid concentrations (80 to 1 10 g/L). Lactic acid, the fermentation product, was added in the feed medium to obtain a high product concentration in the bioreactor.
  • One medium tank (Medium A) contained STLM-B medium with 105 g/L of glucose.
  • the second medium tank (Medium B) contained STLM-B medium that was devoid of glucose, but contained 105 g/L of lactic acid. Initially the bioreactor containing the regular STLM-B medium was operated in the batch mode for 28 h to accumulate cell mass.
  • the total feed rate was maintained at 25 ml/h while the individual feed rates of Medium A and Medium B were varied. Consequently, the effective lactic acid concentration in the feed varied in the range of 0 to 67.2 g/L.
  • the bioreactor agitation speed was 80 rpm, the working volume was 550 ml, and the pH was controlled at 5.5 with 10 N NaOH solution.
  • the effective dilution rate taking into account the rate that NaOH was added, varied between 0.045 and 0.05 h"**, depending on the lactic acid production rate.
  • LBM5 Five 4-strain subconsortia of LBM5 were evaluated in shake flask experiments for their batch fermentation rate in a CaCO3 -buffered STLM-B medium.
  • LBM4 which was LBM5 less L. casei NRRL B-1922, was found to perform as well as LBM5 and better than all other 4-strain subconsortia.
  • a batch fermentation of LBM4 was performed in the bioreactor as described in Example 2, using an active inoculum grown at pH 5.5. The fermentation, with an initial glucose concentration of 110 g/L, was completed in less than 23.5 h, resulting in a lactic acid concentration of 100.3 g/L.
  • a nutrient solution which was prepared at pH 5.9 and was autoclaved separately, was added at 50 ml to each flask, to provide nutrients of PM-C medium.
  • a continuous cell-recycle fermenter was set-up as follows A 2 5-liter stirred tank fermenter and a cross-flow microfiltration or ultrafiltration device were connected by a recirculating loop that drew the fermenter broth into the inlet of the filtration device. The outlet for retentate, which contained cell mass, was connected back to the fermenter, while the outlet for filtrate, which was a cell-free broth, was connected to a product reservoir via a pump controlled by a level controller. The level controller activated the filtrate pump when the fermentation broth raised to a set level, to maintain a constant working volume. The fermentation pH was maintained at the set point by addition of 10 N NaOH. The total working volume of the fermenter was maintained at 1200 ml, including the recycle loop hood-up volume.
  • a continuous cell-recycle fermenter was set-up as in Example 9.
  • a continuous fermentation of the STLM-B medium by the mixed culture LBM5 was performed.
  • the fermentation temperature was 42°C and pH was maintained at 5.5 by addition of 5N NaOH.
  • With 1 10 g/L of glucose in the feed a stable steady state was achieved at a dilution rate of 0.05 h"', resulting in a productivity of 5.7 g/(L-hr) at a lactic acid concentration of 90 g/L.
  • the sugar impurities levels in the product were 0.03 g/L glucose and 2 g/L TRS.
  • the cell concentration was 30 g/L.
  • the bioreactor was operated for 527 hours without contamination.
  • a fermentation broth was obtained from lactic acid fermentation using potato hydrolysate as the carbon source and corn steep liquor as the nutrient supplement.
  • the fermentation broth contained 1 19.3 g/L sodium lactate (i.e., equivalent to 94.8 g/L lactic acid) and 9.9 g/L TRS.
  • the electrodialysis system employed a stack manufactured by Ionics. The stack consisted of 4 cells, each containing a pair of electrodes and 4 compartments (catholyte, feed, product, and anolyte, respectively) divided by three ion- exchange membranes (in the sequence of cation-, anion-, and cation- exchange membranes). The total effective membrane transfer area of the stack was 928 c ⁇ _2.
  • Vfj initial volume of the feed stream
  • Vpj initial volume of the product stream
  • i current density
  • Y yield of recovery
  • [LacH] p final lactic acid concentration in the product stream
  • [NaOH] c final sodium hydroxide concentration in the catholyte stream
  • [TRS] p final TRS concentration in the product stream
  • Electrodialysis successfully converted sodium lactate into lactic acid and sodium hydroxide with a good yield of recovery
  • the lactic acid recovered was partially purified, as indicated by the TRS concentration
  • the obtainable lactic acid concentration was strongly affected by the ratio of volumes of feed and product streams initially charged to the system
  • the obtainable sodium hydroxide similarly, was affected by the ratio of the initial feed and catholyte stream volumes
  • Phase separation during extraction was examined using the fermentation broth that was used as the feed stream of electrodialysis in Example 11.
  • the broth was acidified with sulfuric acid to pH below 2, which resulted in precipitation of denatured proteins. After centrifugal separation of the proteins, a clear supernatant was obtained. 15 ml of the supernatant was brought into contact with 3 ml of the extractant (40% tri-n- octyl amine in 2-heptanone) in a separatory funnel. The funnel was then placed on a ringstand for phase separation. After 10 minutes, the organic- continuous phase was still filled with emulsions and no clear organic layer was observed.
  • Phase separation was also examined for a crude lactic acid, which was obtained by vacuum evaporation of the pooled crude lactic acid solutions produced by electrodialysis in Example 1 1. 50 ml of the crude acid solution and 10 ml of the extractant were brought into contact in a separatory funnel. After 10 minutes of settling, a satisfactory phase separation was obtained. Electrodialysis processing followed by vacuum evaporation appeared to be effective in eliminating the phase separation problem in the subsequent extraction step.
  • a concentrated (by evaporation) and acidified fermentation broth, containing 140 g/L lactic acid and 12% TRS/LacH was processed via methyl esterification, hydrolysis, and distillation, to obtain a purified lactic acid.
  • the purified product contained a total acidity of 0.53 N and a TRS concentration of 0.075 g/L, resulting in a TRS/LacH of 0.16% which was two orders-of- magnitude lower than the initial value.
  • Another crude fermentation broth which was obtained by vacuum evaporation of the pooled crude lactic acid solutions produced by electrodialysis in Example 1 1 , was purified similarly.
  • the crude broth contained 320 g/L lactic acid and 2.4% TRS/LacH.
  • the purified product contained 170 g/L of lactic acid and a TRS/LacH of 0.055%.
  • a test tube containing 3 ml of the purified lactic acid was heated in a dry bath with the temperature initially set at 60°C and gradually increased to 145°C over three and half hours. The temperature was then maintained at 145°C for 75 minutes before the tube was removed from the heated bath.
  • the sample that remained in the tube was a slightly yellowish viscous liquid. By the extent of color formation, the heat-stability of this sample was much better than a commercial food-grade fermentation lactic acid and comparable to a commercial heat-stable grade fermentation lactic acid that is known to be suitable for polymer synthesis.

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Abstract

Méthode consistant à hydrolyser l'amidon en glucose puis à convertir le glucose en acide lactique tout en procédant simultanément à sa saccharification et à sa fermentation pour obtenir le plus grand rendement d'acide possible. Le prétraitement des hydrates de carbone et une activité enzymatique favorable améliorent la vitesse du procédé et la pureté du produit.
PCT/US1993/011759 1992-12-04 1993-12-03 Procede ameliore de pretraitement pour la production d'acide lactique WO1994013826A1 (fr)

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US07/985,765 1992-12-04

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Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2816321A1 (fr) * 2000-11-09 2002-05-10 Roquette Freres Procede de preparation d'un milieu de fermentation a partir d'une matiere premiere renouvelable
WO2005100583A3 (fr) * 2004-03-31 2006-12-14 Natureworks Llc Procede de fermentation de sucres contenant des saccharides oligomeriques
US7273734B2 (en) 2001-07-16 2007-09-25 Canon Kabushiki Kaisha Process for producing a polyester
WO2009025547A1 (fr) * 2007-08-23 2009-02-26 Wageningen Universiteit Prétraitement alcalin doux et saccharification et fermentation simultanées de biomasse lignocellulosique en acides organiques
WO2011098843A2 (fr) 2010-02-10 2011-08-18 Sveučilište u Zagrebu Production d'acide lactique à partir de matières à base d'amidon par des bactéries lactiques amylolytiques
WO2018226358A1 (fr) * 2017-05-10 2018-12-13 The Quaker Oats Company Matière d'origine végétale hydrolysée et fermentée
US10426181B2 (en) 2011-03-21 2019-10-01 The Quaker Oats Company Method for preparing high acid RTD whole grain beverages
US10913963B2 (en) 2016-03-22 2021-02-09 The Quaker Oats Company Method and apparatus for controlled hydrolysis
US11136602B2 (en) * 2016-11-29 2021-10-05 Purac Biochem Bv Fermentation process
US11172695B2 (en) 2016-03-22 2021-11-16 The Quaker Oats Company Method, apparatus, and product providing hydrolyzed starch and fiber

Citations (4)

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Publication number Priority date Publication date Assignee Title
US4771001A (en) * 1986-03-27 1988-09-13 Neurex Corp. Production of lactic acid by continuous fermentation using an inexpensive raw material and a simplified method of lactic acid purification
US4808419A (en) * 1987-02-02 1989-02-28 Hsu Edward J Automated method for a semi-solid fermentation used in the production of ancient quality rice vinegar and/or rice wine
US4857339A (en) * 1987-09-28 1989-08-15 Nabisco/Cetus Food Biotechnology Research Partnership Method for making cereal products naturally sweetened with fructose
US5120552A (en) * 1991-01-30 1992-06-09 The Pillsbury Company Enzymatic treatment of produce cell wall fragments

Patent Citations (4)

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US4771001A (en) * 1986-03-27 1988-09-13 Neurex Corp. Production of lactic acid by continuous fermentation using an inexpensive raw material and a simplified method of lactic acid purification
US4808419A (en) * 1987-02-02 1989-02-28 Hsu Edward J Automated method for a semi-solid fermentation used in the production of ancient quality rice vinegar and/or rice wine
US4857339A (en) * 1987-09-28 1989-08-15 Nabisco/Cetus Food Biotechnology Research Partnership Method for making cereal products naturally sweetened with fructose
US5120552A (en) * 1991-01-30 1992-06-09 The Pillsbury Company Enzymatic treatment of produce cell wall fragments

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
CEREAL CHEMISTRY, Volume 68, No. 2, issued March-April 1991, D. LING et al., "Corn Wet Milling with a Commercial Enzyme Preparation", pages 205-206. *

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2816321A1 (fr) * 2000-11-09 2002-05-10 Roquette Freres Procede de preparation d'un milieu de fermentation a partir d'une matiere premiere renouvelable
EP1205557A1 (fr) * 2000-11-09 2002-05-15 Roquette FrÀ¨res Procédé de préparation d'un milieu de fermentation à partir d'une matière première renouvelable
US7273734B2 (en) 2001-07-16 2007-09-25 Canon Kabushiki Kaisha Process for producing a polyester
WO2005100583A3 (fr) * 2004-03-31 2006-12-14 Natureworks Llc Procede de fermentation de sucres contenant des saccharides oligomeriques
WO2009025547A1 (fr) * 2007-08-23 2009-02-26 Wageningen Universiteit Prétraitement alcalin doux et saccharification et fermentation simultanées de biomasse lignocellulosique en acides organiques
WO2011098843A2 (fr) 2010-02-10 2011-08-18 Sveučilište u Zagrebu Production d'acide lactique à partir de matières à base d'amidon par des bactéries lactiques amylolytiques
US10426181B2 (en) 2011-03-21 2019-10-01 The Quaker Oats Company Method for preparing high acid RTD whole grain beverages
US10913963B2 (en) 2016-03-22 2021-02-09 The Quaker Oats Company Method and apparatus for controlled hydrolysis
US11172695B2 (en) 2016-03-22 2021-11-16 The Quaker Oats Company Method, apparatus, and product providing hydrolyzed starch and fiber
US11136602B2 (en) * 2016-11-29 2021-10-05 Purac Biochem Bv Fermentation process
WO2018226358A1 (fr) * 2017-05-10 2018-12-13 The Quaker Oats Company Matière d'origine végétale hydrolysée et fermentée
CN110621167A (zh) * 2017-05-10 2019-12-27 桂格燕麦公司 发酵的水解的植物来源的材料

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