EP0250407A1 - CONVERSION DE SUCROSE EN ETHANOL ET AUTRES PRODUITS EN UTILISANT LE $i(ZYMOMONAS MOBILIS) - Google Patents

CONVERSION DE SUCROSE EN ETHANOL ET AUTRES PRODUITS EN UTILISANT LE $i(ZYMOMONAS MOBILIS)

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Publication number
EP0250407A1
EP0250407A1 EP86901306A EP86901306A EP0250407A1 EP 0250407 A1 EP0250407 A1 EP 0250407A1 EP 86901306 A EP86901306 A EP 86901306A EP 86901306 A EP86901306 A EP 86901306A EP 0250407 A1 EP0250407 A1 EP 0250407A1
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EP
European Patent Office
Prior art keywords
fructose
zymomonas mobilis
fermentation
sucrose
strain
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP86901306A
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German (de)
English (en)
Other versions
EP0250407A4 (fr
Inventor
Horst Werner Doelle
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University of Queensland UQ
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University of Queensland UQ
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Publication date
Application filed by University of Queensland UQ filed Critical University of Queensland UQ
Publication of EP0250407A1 publication Critical patent/EP0250407A1/fr
Publication of EP0250407A4 publication Critical patent/EP0250407A4/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
    • C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
    • C12P7/06—Ethanol, i.e. non-beverage
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
    • C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
    • C12P7/06—Ethanol, i.e. non-beverage
    • C12P7/065—Ethanol, i.e. non-beverage with microorganisms other than yeasts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Definitions

  • Field of the Invention relates to a method for converting sucrose and/or glucose-fructose syrup mixtures to ethanol in combination with other products in a single- stage fermention process using parent or mutant strains of Zymomonas mobilis in micr ⁇ aerophilic conditions.
  • the sugar industry has become concerned following the announcements by many major food and drink manufacturing companies that they intend replacing sugar (sucrose) with fructose obtained from corn syrup, fructose/sorbitol or fructose/glucose (dextrose) mixtures to cater for the dietary, health and diabetics market.
  • sugar sucrose
  • fructose/sorbitol or fructose/glucose dextrose
  • Fructose is nearly twice as sweet as sugar and so only half the amount is required for the same level of sweetness, which reduces the calorific value, an important aspect of this health-conscious world.
  • sorbitol and fructose are safe sweeteners for diabetics in contrast to sucrose.
  • corn syrup to fructose is energy-dependent as the corn mash must first be converted to glucose, which is normally carried out using the enzymes amylase and glucoamylase. The glucose must then be further converted to fructose using the enzyme glucose isomerase. This enzymic conversion results in approximately 50/50 mixtures of glucose and fructose. In order to obtain higher fructose values, glucose must be removed by chromatographical methods, which are very expensive and still do not completely remove glucose from the mixture.
  • the production of ethanol from sugar cane is well-known and in Brazil the ethanol is mixed with petrol to produce "gasohol", or is solely used as car fuel.
  • the ethanol is produced mainly from corn and to a lesser degree from sugar cane feedstocks whereby the ethanol is primarily used as octane enhancer in unleaded petrol with the mix being referred to as "super unleaded gasoline".
  • the traditional process of ethanol production is carried out in a two-stage batch process using yeast, whereby the first stage involves an aerobic propagation of the yeast referred to as the growth stage and the second stage involves the anaerobic process of ethanol production in the presence or absence of small amounts of oxygen.
  • the first stage involves an aerobic propagation of the yeast referred to as the growth stage
  • the second stage involves the anaerobic process of ethanol production in the presence or absence of small amounts of oxygen.
  • a slight addition of air or oxygen is required.
  • the latter is required if the efficiency of the total process is to be increased using the occasional recycling of yeast cells by systems such as sedimentation or centrifugation.
  • yeast fermentation is inherently dependent on coupling of growth with rate of ethanol production, to optimize ethanol production the medium must either be supplemented with growth enhancing substances or with finely controlled aeration.
  • stage 2 The traditional yeast fermentation process (stage 2) is therefore dependent on large inoculum size of approximately 5 to 10 million cells per ml.
  • the preferred optimal temperature of fermentation is 30oC and heat produced has to be controlled through the use of cooling equipment.
  • the fermentation time for obtaining between 9 and 11% (v/v) ethanol is 30 to 70 hours with stage 2 batch fermentation. The time of this fermentation can be reduced to 10 hours by increasing the inoculum density by 80-100 fold through cell recycling.
  • a second process for ethanol production is known, which utilizes the bacterium Zymomonas mobilis (see European Patent No. 0047641 - George Westori Ltd.).
  • This process is also a two-stage process as was described above for yeast, but the bacterium does not require the addition of air for its growth stage (stage 1). Instead, an adequate supply of nitrogen is required to keep conditions anaerobic.
  • the sugar concentration must never exceed 6% (w/v) and thus the stage requires a stepwise or continuous addition of a concentrated sugar solution.
  • the preferred temperature is 28°C to 33°C and the preferred pH is about 5.5. This process may also require a supply of nitrogen as well as additional nutrients.
  • a third process for ethanol production has been described, which utilizes immobilized yeast or strains of Zymomonas in a two-stage process, each with a limited amount of sugar (i.e. 10% w/v) present (see British Patent No. 2055121 - Tanabe Sugaku Co. Ltd.).
  • the examples for carbon source conversion are known to be sucrose, glucose, molasses and sugar cane juice, whereas in the case of the two-stage process utilizing Zymomonas the examples are limited to glucose, and in the case of the immobilized cells, to glucose and molasses.
  • Two processes are known to use glucose as substrate for ethanol production.
  • One is a recycling process, whereby after fermentation the biomass is separated from the beer and recycled back to the fermentation system (see U.S. Patent No. 4,403,034 (Rogers et al ; and Australian Patent Application No. 78199/81 (Unisearch Ltd.)).
  • the second process is a continuous process using the glucose derived from starch hydrolysis for ethanol production. Both processes operate at 30°C and pH 5.0.
  • sucrose-based materials e.g. sugar cane juice or syrup, sugar beet juice or syrup, molasses, palm sugar juice or syrup, raw or refined sugar
  • glucose-fructose mixtures e.g. high fructose corn syrup, artificial mixtures, high test molasses or invert sugar solutions.
  • the present invention resides in a method for the production of ethanol in combination with fructose and/or sorbitol from a sucrose-based material and/or a glucose-fructose mixture in a fermentation characterized by fermenting the sucrose-based material and /or glucose-fructose mixture with the micro-organism Zymomonas mobilis in a single-stage process under microaerophilic conditions wherein the sucrose-based material and/or glucose-fructose mixture is contained in a fermentation medium as the substrate.
  • a "single-stage process” is defined as a process whereby growth and the production phase occur in the same fermentation vessel.
  • Initiation of the process can be done either by a seed culture containing Zymomonas mobilis added to the fermenter vessel containing the fermentation medium or by adding the fermentation medium to the fermenter which contains a portion of the fermented medium from a previous fermentation run, the fermented medium containing Zymomonas mobilis.
  • "Microaerophilic conditions" are defined as conditions whereby no gas (oxygen, air, nitrogen, etc.) is added to the fermenter and the surface of the fermentation medium is exposed to at.m ⁇ sphere.
  • the Zymomonas mobilis organism does not require air or oxygen (aerobic) or nitrogen (anaerobic) for growth and production of ethanol, but can tolerate the presence of air on the surface of the fermentation medium.
  • the fermentation may be carried out using free or immobilized form of the micro-organism.
  • Sucrose-based materials include sugar cane juice or syrup, sugar beet juice or syrup, molasses, palm sugar juice or syrup, raw or refined sugar.
  • the glucose and/or fructose mixture include high fructose corn syrup, artificial mixtures, high test molasses or invert sugar solutions.
  • the base medium includes yeast extract, casein hydrolysate, ammonium sulfate, urea or magnesium sulfate, potassium dihydrogen phosphate and/or glucose.
  • yeast extract casein hydrolysate
  • ammonium sulfate ammonium sulfate
  • urea or magnesium sulfate potassium dihydrogen phosphate
  • glucose preferably all the constituents in this base medium are in the range of 0.01 to 1.0%, more preferably. 0.2 to0.5%
  • the incubation steps are carried out at approximately 30°C for a period of e.g. 2 to 15 hours.
  • the fructose and glucose are added to the medium in the range of 0.5 to 3%, more preferably 1 to 2% (w/v).
  • One preferred parent strain of the microorganism Zymomonas mobilis has been deposited in the Culture Collection of the University of Queensland, Microbiology Department, St. Lucia, Queensland, Australia under Deposit No. UQM 2716 and deposited in the American Type Culture Collection (ATCC), 12301 Parklawn Drive, Rockville, Maryland, 20852, U.S.A. on 24th April, 1984 under Deposit No. 39676.
  • This strain has been developed from the Zymomonas mobilis strain ATCC Deposit No. 29191 which is a second preferred parent strain suitable for use with the present invention.
  • the parentbstrain has also been deposited under Deposit No. NCIB 11199 at the National Collection of Industrial Bacteria, Torry Research Station, Abbey Road, Aberdeen, United Kingdom AB9 8DG.
  • strain ATCC 39676 was carried out using the chemostat cultivation technique for increased substrate uptake i.e. improved performance and metabolic rate of sucrose conversion and these features are the only difference in the taxonomic description of the parent strain ATCC No. 29191 set out at pages 576-580 of "Bergy's Manual of Determinative Bacteriology" (8th Edition) (1975).
  • the fructose utilization negative (Fru-) mutant strains have been developed from the Zymomonas mobilis parent strains ATCC 29191 and 39676, respectively, by treatment using ethylmethane sulphonate (EMS).
  • EMS ethylmethane sulphonate
  • the taxonomic description for each strain is as for its parent with the exception of the fructose negative nature and each has a plump gram negative rod.
  • the method of production of the fructose utilization negative strains is set out in Example I.
  • sucrose concentration in the sucrose-based substrates is in the range of 10 to 40% (w/v) and the glucose and fructose concentration in the corresponding mixtures is in the range of 5 to 20% (w/v) of each.
  • the fermentation medium includes only one or more of the following components: peptone (caesin hydrolysate), yeast extract, calcium panjsothenate, potassium dihydrogen phosphate, ammonium sulfate, urea, and magnesium sulfate.
  • peptone caesin hydrolysate
  • yeast extract yeast extract
  • calcium panjsothenate calcium panjsothenate
  • potassium dihydrogen phosphate potassium dihydrogen phosphate
  • ammonium sulfate urea
  • magnesium sulfate Preferably the components are provided in the concentration range of 0.01 to 0.5% each with approximately 0.2% being preferred.
  • the pH of the fermentation process is maintained in the range of 4.0 to 7.0.
  • the pH is initially set in the range of 6.5 to 7.0.
  • the pH is maintained in the range of 5.0 to 6.2.
  • the pH range may be controlled by the addition of NaOH or other suitable alkali.
  • the temperature is maintained in the range of 34°C to 4 ⁇ °C. This temperature range appears to produce the best growth and product yields and alleviates or markedly reduces the production of slime in the fermenter.
  • the micro-organism is separated from the fermentation products, the ethanol is distilled off and the product is concentrated or crystallized.
  • the present invention resides in a method for the production of a fructose utilization negative mutant strain of the micro-organism Zymomonas mobilis comprising mutating a fructose utilization negative strain of Zymomonas mobilis.
  • the present invention resides in a method for the production of a fructose utilization negative mutant strains of Zymomonas mobilis including the steps of: growing Zymomonas mobilis in a basic medium to form a first cell culture; adding ethylmethane sulphonate and/or nitrosoguanidine to the first ceil culture and incubating the mixture; removing the cells from the first cell culture suspending the cells in the basic medium and incubating the mixture to generate a second cell culture; harvesting the cells from the second cell culture and suspending the cells in the base medium to generate a third cell culture; and obtaining the fructose utilization negative cells of Zymomonas mobilis by plating the cells of the third cell culture in the base medium combined with glucose and/or fructose.
  • the present invention resides in fructose utilization negative strains of Zymomonas mobilis produced by the above method. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS
  • the parent strain was grown in a medium containing 0.2% (w/v) yeast extract, 0.2% (w/v) casein hydrolysate, 0.2% (w/v) ammonium sulfate, 0.2% (w/v) MgSO 4 7H 2 O, 0.2% (w/v) KH 2 PO 4 with 1% (w/v) glucose to approximately 109 cfu/mL, whereby cfu represents colony forming units.
  • EMS ethylmethane sulphonate
  • NTG nitrosoguanidine
  • the cells were washed in above basic medium and suspended in 10 mL of above medium. After 18 hours incubation at 30°C, 2 ML of the culture were transferred to 10 mL of the above medium containing 2% (w/v) fructose and 1,000 U/mL penicillin G. After 5 hours incubation at 30°C the cells were harvested and suspended in the above medium and left overnight at 30oC. Surviving colonies were obtained on plating the culture in the above medium containing 1% (w/v) glucose. The isolated colonies were patched on the same medium containing either 1% (w/v) glucose or 1% (w/v) fructose.
  • Fructose utilization negative behaviour was confirmed using heavy inocula into above culture medium containing 1% and 10% (w/v) fructose. If no growth occurred after 7 days, a fructose utilization negative mutant was obtained. (For mutant strain E 977, the penicillin step may be omitted.)
  • the parent strains ATCC 39676 and ATCC 29191 grew on both 1% (w/v) and 10% (w/v) sucrose, 18% (w/v) and 10% (w/v) glucose, and 1% (w/v) and 10% (w/v) fructose, but their mutant derivatives E 4381 and E 977, while being able to grow on 1% (w/v) and 10% (w/v) sucrose and 1% (w/v) and 10% (w/v) glucose, did not grow on either 1% (w/v) or 10% (w/v) fructose.
  • sucrose fermentation was carried out using the Fru- mutants and their parent strains. Using 125 mL bottles and x medium containing 10% (w/v) sucrose, the broth was inoculated with a seed culture grown on glucose and incubated statically for 48 hours at 37°C. Samples were taken after 15 minutes and at the end of incubation, centrifuged and analyised.
  • 2,500 mL of a sucrose solution containing 192 g/L (w/v) of sucrose are transferred into an open 3.5 L fermentation vessel.
  • 200 mL of a medium is added aseptically containing any one or more of peptone, yeast extract, potassium dihydrogen phosphate, ammonium sulfate or urea, and magnesium sulfate, with each component having a concentration of 0.2% or less, whereby peptone and yeast extract can be replaced by 0.5% (w/v) calcium pantothenate or the total medium can be replaced by 2,700 mL of sucrose containing sugar cane syrup, sugar beet syrup or a proportional addition of molasses.
  • 2,500 mL of a sucrose solution containing 217.1 g/L (w/v) of sucrose are transferred into an open 3.5 L fermentation vessel.
  • 200 mL of a medium is added aseptically containing any one or more of peptone, yeast extract, potassium dihydrogen phosphate, ammonium sulfate or urea, and magnesium sulfate, with each component having a concentration of 0.2% or less, whereby peptone and yeast extract can be replaced by 0.5% (w/v) calcium pantothenate or the total medium can be replaced by 2,700 mL of sucrose containing sugar cane syrup, sugar beet syrup or a proportional addition of molasses.
  • 2,500 mL of a sucrose solution containing 390 g/L (w/v) of sucrose are transferred into a 3.5 L fermenter vessel. If required, 200 mL of a medium is added aseptically containing one or more of peptone
  • casein hydrolysate casein hydrolysate
  • yeast extract potassium dihydrogen phosphate, ammonium sulfate or urea, and magnesium sulfate, hydrated, with each component having a concentration of 0.2% (w/v), whereby peptone and yeast extract can be replaced by 0.5% calcium pantothenate or the total medium can be replaced using 2,700 mL of sucrose containing sugar cane syrup, sugar beet syrup or a proportional addition of molasses.
  • sucrose solution containing 400 g/L of sucrose are transferred into a 2 L fermentation vessel.
  • 300 mL of a medium is added aseptically containing any one or more of peptone, yeast extract, potassium dihydrogen phosphate, ammonium sulfate or urea and magnesium sulfate, with each component having a concentration of 0.2% (w/v), whereby peptone and yeast extract can be replaced by 0.5% (w/v) calcium pantothenate.
  • Zymomonas mobilis (ATCC No. 39676) grown in a medium containing 10% (w/v) sucrose, 0.2% (w/v) yeast extract, 0.2% (w/v) casein hydrolysate (peptone), 0.2% (w/v) potassium dihyrdogen phosphate, 0.2% (w/v) magnesium sulfate, hydrated and 0.2% (w/v) ammonium sulfate at
  • 35oC or 37°C was added to the fermentation vessel.
  • the initial pH was brought to 6.5 and was then maintained at 5.5 by the addition of 2 M NaOH (80 g/L).
  • Cultivation was carried out at a temperature of 35°C at a stirring rate of 100 rpm.
  • 5 L of a medium is added aseptically containing any one or more of peptone (casein hydrolysate), yeast extract, potassium dihydrogen phosphate, ammonium sulfate or urea, and magnesium sulfate, hydrated, with each component having a concentration of 0.2% (w/v), whereby peptone and yeast extract can be replaced by 0.5% calcium pantothenate or the total mediumcan be replaced using 90 L of sucrose containing sugar cane syrup, sugar beet syrup or a proportional addition of molasses.
  • peptone casein hydrolysate
  • yeast extract potassium dihydrogen phosphate
  • ammonium sulfate or urea urea
  • magnesium sulfate magnesium sulfate
  • 2,500 mL of a sucrose solution containing 400 g/L (w/v) of sucrose are transferred into a 3.5 L fermentation vessel.
  • 200 mL of a medium is added aseptically containing any one or more of peptone (casein hydrolysate), yeast extract, potassium dihydrogen phosphate, magnesium sulfate hydrated, ammonium sulfate or urea, with each component having a concentration of 0.2% (w/v), whereby peptone and yeast extract can be replaced by 0.5% (w/v) calcium pantothenate or the total medium can be replaced by 2,700 mL of sucrose containing sugar cane syrup, sugar beet syrup or a proportional addition of molasses.
  • EXAMPLE 8 Fermentation of Glucose-Fructose Mixtures with Fru- Mutants (Growth and production phases) 2,500 mL of a solution containing 102 g/L glucose and 105 g/L fructose are transferred into a 3.5 L fermentation vessel.
  • 200 mL of a medium is added aseptically containing any one or more of peptone (casein hydrolysate), yeast extract, potassium dihydrogen phosphate, magnesium sulfate, hydrated, ammonium sulfate or urea, with each component having a concentration of 0.2% (w/v), whereby peptone and yeast extract can be replaced by 0.5% (w/v) calcium pantothenate.
  • peptone casein hydrolysate
  • yeast extract potassium dihydrogen phosphate
  • magnesium sulfate magnesium sulfate
  • ammonium sulfate or urea a concentration of 0.2% (w/v)
  • peptone and yeast extract can be replaced by 0.5% (w/v) calcium pantothenate.
  • the fermented medium was centrifuged for 10 minutes at 4,000 rpm and was added to the fermentation medium of Examples 2 to 4 respectively, where the fermented medium contained the Fru- mutant strains, and to the fermentation medium of Examples 5 and 6 where the fermentation medium contained the parent strain ATCC 39676.
  • the pH and temperature conditions of the Examples were followed and in all cases fermentation occurred with results corresponding to those described for each respective Example.
  • the fermentation process using fermented medium from a preceding process as an inoculum for the Zymomonas mobilis was repeated several times and consistent results were achieved. It was observed that the Zymomonas mobilis cells grew rapidly in the fermentation medium and both growth and production phases occurred simultaneously after the initial growth phase on the addition of the fresh fermentation medium to the fermenter containing the fermented medium.
  • the parent strain ATCC 39676 may be replaced by other strains, including the second strain ATCC 29191 but. the best results are achieved using ATCC 39676.
  • Ethanol produced has commercial value as a component in gasoline or octane boosters in lead-free petrol or as a base product in the chemical industry, carbon dioxide may be used for dry ice or as a carbon source for the growth of algal biomass.
  • Fructose, sorbitol and mannitol are highly valuable nutritive sweeteners of different commercial value in dietary, health food, diabetic foods such as soft drinks, confectionery, and related industries.
  • the fermentation process requires only a low energy input as the organism produces a fair amount of heat during the fermentation process.
  • the fermentation is carried out in microaerophilic conditions, avoiding the need for aeration or addition of any other gas (and attendant equipment), the fermentation components and products requiring little mechanical stirring and pH control.
  • sucrose In the case of sucrose, experiments have shown that the success of the fermentation process is not wholly dependent on the quality of the substrate. Preliminary experiments with sugar cane juice and sugar cane syrup indicate that the process is particularly suited for industrial applications and the fermenter can be provided adjacent a sugar mill to reduce transport costs. As the sugar cane juice does not have to be sterilized, the energy input can be kept low.
  • glucose-fructose mixtures In the case of glucose-fructose mixtures, experiments have shown that the ratio of both sugars play an important role. It is preferred that the glucose-fructose mixtures be in the range of 1:4 to 4:1 glucose: fructose.
  • the method is clearly applicable to the fermentation of invert sugar solutions as this comprises a mixture of 50% glucose and 50% fructose (i.e. a ratio of 1:1) obtained by the hydrolysis of sucrose; invert sugar being prepared commercially from the inversion of 96% cane sugar solution. This indicates that the process is particularly suited for industrial applications when the fermenter can be provided adjacent to a fructose corn syrup or isomerization plant producing such mixtures to reduce transport costs.

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  • Organic Chemistry (AREA)
  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Zoology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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Abstract

Procédé de fermentation mono-étape dans des conditions micro-aérophiles pour la production commerciale d'éthanol avec du fructose et/ou du sorbitol à partir de substances à base de sucrose ou de mélanges de glucose-fructose, en utilisant des souches de Zymomonas mobilis. Des souches mutantes négatives de Zymomonas mobilis utilisant le fructose ont été développées, ce qui permet d'améliorer le rendement de la fermentation.
EP19860901306 1985-02-21 1986-02-20 CONVERSION DE SUCROSE EN ETHANOL ET AUTRES PRODUITS EN UTILISANT LE -i(ZYMOMONAS MOBILIS). Withdrawn EP0250407A4 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
AUPG939685 1985-02-21
AU9396/85 1985-02-21
AU1811/85 1985-08-06
AUPH181185 1985-08-06

Publications (2)

Publication Number Publication Date
EP0250407A1 true EP0250407A1 (fr) 1988-01-07
EP0250407A4 EP0250407A4 (fr) 1988-06-27

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EP19860901306 Withdrawn EP0250407A4 (fr) 1985-02-21 1986-02-20 CONVERSION DE SUCROSE EN ETHANOL ET AUTRES PRODUITS EN UTILISANT LE -i(ZYMOMONAS MOBILIS).

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EP (1) EP0250407A4 (fr)
KR (1) KR870700098A (fr)
BR (1) BR8607056A (fr)
ES (1) ES8708011A1 (fr)
GB (1) GB2191784A (fr)
HU (1) HUT45560A (fr)
NL (1) NL8600431A (fr)
NZ (1) NZ215231A (fr)
WO (1) WO1986004925A1 (fr)
ZW (1) ZW4586A1 (fr)

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US5102795A (en) * 1989-11-04 1992-04-07 Forschungszentrum Juelich Gmbh Process for obtaining sorbitol and gluconic acid or gluconate

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DE3528933A1 (de) * 1985-08-13 1987-02-19 Kernforschungsanlage Juelich Fermentationsverfahren zur fructosegewinnung oder -anreicherung gegenueber glucose und dafuer brauchbare zymomonas mobilis mutanten
DE3528932A1 (de) * 1985-08-13 1987-02-19 Kernforschungsanlage Juelich Verfahren zur gewinnung von sorbit durch enzymatische reaktion und dafuer geeignete mikroorganismen
WO1987002706A1 (fr) * 1985-10-25 1987-05-07 University Of Queensland Conversion d'hydrolysats d'amidon en ethanol par utilisation du zymomonas mobilis
ES2136553B1 (es) * 1997-08-07 2000-08-16 Consejo Superior Investigacion Proceso de obtencion de fructosa a partir de mostos de uva.
LV12576B (lv) * 1999-05-17 2001-04-20 Aivars Upenieks Cukurbiešu kompleksās pārstrādes paņēmiens

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US4350765A (en) * 1979-06-13 1982-09-21 Tanabe Seiyaku Co., Ltd. Method for producing ethanol with immobilized microorganism
AU537029B2 (en) * 1980-05-15 1984-05-31 Unisearch Limited Ethanol production
WO1982001563A1 (fr) * 1980-10-23 1982-05-13 Bo Mattiasson Procedes de conversion biologique et chimique dans un systeme a phase liquide
AU540186B2 (en) * 1980-12-08 1984-11-08 Unisearch Limited Semi batch ethanol production
AU573742B2 (en) * 1983-09-27 1988-06-23 University Of Queensland, The Conversion of sucrose to fructose and ethanol

Non-Patent Citations (2)

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CHEMICAL ABSTRACTS, vol. 102, no. 3, 21st January 1985, page 543, abstract no. 22777k, Columbus, Ohio, US; H.C. LEE et al.: "Comparison of ethanol production by different isolates of Zymomonas mobilis after nitrosoguanidine treatment", & CHUNG-KUO NUNG YEH HUA HSUEH HUI CHIH 1984, 22(1-2), 34-45 *
See also references of WO8604925A1 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5102795A (en) * 1989-11-04 1992-04-07 Forschungszentrum Juelich Gmbh Process for obtaining sorbitol and gluconic acid or gluconate

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WO1986004925A1 (fr) 1986-08-28
KR870700098A (ko) 1987-02-28
NZ215231A (en) 1989-01-06
ES8708011A1 (es) 1987-09-01
GB8718572D0 (en) 1987-09-09
ES552218A0 (es) 1987-09-01
BR8607056A (pt) 1988-02-23
GB2191784A (en) 1987-12-23
EP0250407A4 (fr) 1988-06-27
NL8600431A (nl) 1986-09-16
HUT45560A (en) 1988-07-28
ZW4586A1 (en) 1986-11-19

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