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WO2008086595A1 - Procédé de production d'hydrogène et de glutamate monosodique - Google Patents

Procédé de production d'hydrogène et de glutamate monosodique Download PDF

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Publication number
WO2008086595A1
WO2008086595A1 PCT/CA2008/000047 CA2008000047W WO2008086595A1 WO 2008086595 A1 WO2008086595 A1 WO 2008086595A1 CA 2008000047 W CA2008000047 W CA 2008000047W WO 2008086595 A1 WO2008086595 A1 WO 2008086595A1
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WO
WIPO (PCT)
Prior art keywords
brevibacterium
monosodium glutamate
corynebacterium
process according
solution
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.)
Ceased
Application number
PCT/CA2008/000047
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English (en)
Inventor
Blaine Creston Froats
Sean Creston Froats
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Alternate Energy Corp
Original Assignee
Alternate Energy Corp
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Filing date
Publication date
Application filed by Alternate Energy Corp filed Critical Alternate Energy Corp
Publication of WO2008086595A1 publication Critical patent/WO2008086595A1/fr
Anticipated expiration legal-status Critical
Ceased 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
    • C12P13/00—Preparation of nitrogen-containing organic compounds
    • C12P13/04—Alpha- or beta- amino acids
    • C12P13/14—Glutamic acid; Glutamine
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/08—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents with metals
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C227/00—Preparation of compounds containing amino and carboxyl groups bound to the same carbon skeleton
    • C07C227/38—Separation; Purification; Stabilisation; Use of additives
    • C07C227/40—Separation; Purification
    • 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
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis

Definitions

  • the present disclosure relates to the preparation, purification and recovery of monosodium glutamate useful as a food additive and recovery of hydrogen gas, by an improved process.
  • Monosodium glutamate is an amino acid salt which is widely used as a flavour additive.
  • Methods for obtaining monosodium glutamate generally involve the preparation of L-glutamic acid by fermentation, e.g., starch, beets, sugar cane or molasses and which is consequently converted to monosodium glutamate.
  • Some methods involve the intermediate step of forming magnesium di-glutamate which is then converted to monosodium glutamate.
  • the intermediate step of preparing magnesium di-glutamate from L-glutamic acid concurrently generates hydrogen gas.
  • the hydrogen gas which is generated during the preparation of monosodium glutamate has, in the past, been treated as a by-product. Hydrogen gas is itself useful as a fuel and as a chemical ingredient.
  • a process for the concurrent generation of hydrogen gas and monosodium glutamate comprising: (a) reacting magnesium and L-glutamic acid solution in a reactor vessel to provide hydrogen and magnesium di-glutamate solution; (b) evacuating and bottling the hydrogen; (c) combining the magnesium di-glutamate solution with sodium carbonate, trisodium phosphate, or sodium hydroxides to produce a secondary byproduct precipitate and a monosodium glutamate enriched solution; (d) draining, siphoning, and/or filtering the monosodium glutamate enriched solution; and (e) utilizing an evaporator or dryer to recover a dry monosodium glutamate powder.
  • the L-glutamic acid is provided by the fermentation of glucose.
  • the L-glutamic acid is fermented by Corynebacterium glutamicum.
  • L-glutamic acid is fermented by is fermented by a bacteria selected from a group consisting of: Corynebacterium acetoacidophilum, Corynebacterium acetoglutomicum, Corynebacterium alkanolyticum, Corynebacterium callunae, Corynebacterium glutamicum (Brevibacterium lactofermentum) , Corynebacterium lilium, Corynebacterium melassecola, Corynebacterium thermoaminogenes (Corynebacterium efficiens),
  • Corynebacterium herculis Brevibacterium divaricatum, Brevibacterium flavum, Brevibacterium imma ⁇ ophilum, Brevibacterium roseum, Brevibacterium sacchorolyticum, Brevibacterium thiogenitalis, Brevibacterium ammoniagenes, Brevibacterium album, Brevibacterium cerinum, Microbacterium ammoniaphilum, Brevibacterium cerinum, and Microbacterium ammoniaphilium.
  • the glucose is in the form of cassava starch or sweet corn.
  • the secondary byproduct is precipitated as a solid phase.
  • the monosodium glutamate enriched solution is extracted by siphoning off or passing through a filter, leaving the precipitate behind.
  • the reactor vessel is about 10000 to about 15000 liters.
  • the reactor vessel is maintained at a temperature above ambient temperature.
  • the reactor vessel is maintained at a temperature of about 95 0 C.
  • the reactants are fed to the reactor vessel at ambient temperatures.
  • the evaporator is a decompression evaporator.
  • the monosodium glutamate enriched solution is concentrated prior to the step of utilizing an evaporator or dryer to recover a dry monosodium glutamate powder.
  • the monosodium glutamate enriched solution is concentrated by heating.
  • FIG.l is a diagram depicting an exemplary process for preparing monosodium glutamate and generating hydrogen gas.
  • Monosodium glutamate a widely used flavour additive, is depicted by the chemical formula NaC 5 H 8 NO 4 .
  • An exemplary chemical structure of monosodium glutamate is illustrated below.
  • the production of monosodium glutamate is a known process.
  • L-glutamic acid is reacted with magnesium to form magnesium di- glutamate and hydrogen gas.
  • a typical chemical reaction is illustrated below.
  • the magnesium di-glutamate is then typically reacted with sodium hydroxide, trisodium phosphate, or sodium carbonate to obtain monosodium glutamate, as illustrated below.
  • FIG.l shows an exemplary process for the concurrent preparation of monosodium glutamate and generation of hydrogen gas.
  • Glutamic acid specifically L-glutamic acid, used in the preparation of monosodium glutamate can be prepared by fermentation using bacteria, e.g.; strains of Corynebacterium glutamicum and other bacterium, including but not limited to the following : Corynebacterium acetoacidophilum, Corynebacterium acetoglutomicum, Corynebacterium alkanolyticum, Corynebacterium callunae, Corynebacterium glutamicum, Corynebacterium lilium, Corynebacterium melassecola, Corynebacterium thermoaminogenes (Corynebacterium efficiens), Corynebacterium herculis, Brevibacterium diva ⁇ catum, Brevibacterium flavum, Brevibacterium immariophilum, Brevibacterium lactofermentum (Corynebacterium glutamicum), Brevibacterium roseum, Brevibacterium sacchorolyticum, Brevibacterium thiogen
  • coryneform bacteria include but are not limited to the following : Corynebacterium acetoacidophilum ATCC 13870, Corynebacterium acetoglutamicum ATCC 15806, Corynebacterium alkanolyticum ATCC 21511, Corynebacterium glutamicum ATCC 13020, ATCC 13032, ATCC 13060, ATCC 13896, Corynebacterium lilium ATCC 15990, Corynebacterium melassecola ATCC 17965, Corynebacterium thermoaminogenes A3 12340 (FERM BP-1539), Corynebacterium herculis ATCC 13868, Brevibacterium divaricatum ATCC 14020, Brevibacterium flavum, ATCC 13826, ATCC 14067, AJ 12418 (FERM BP-2205), Brevibacterium immariophilum ATCC 14068, Brevibacterium lacofermentum (Corynebacterium glutamicum) ATCC 138
  • the strains identified with an ATCC accession number are available from the American Type Culture Collection (ATCC, Address: P.O. Box 1549, Manassas, Va. 20108, United States of America).
  • the AJ 12340 strain was deposited at National Institute of Bioscience and Human Technology, Agency of Industrial Science and Technology, Ministry of International Trade and Industry (currently International Patent Organism Depositary, National Institute of Advanced Industrial Science and Technology at Tsukuba-shi, Ibaraki-ken 305-5466, Japan) on Oct. 27, 1989 under the provisions of the Budapest Treaty and given an accession number of FERM BP-1539.
  • the AJ 12418 strain was deposited at National Institute of Bioscience and Human Technology, Agency of Industrial Science and Technology, Ministry of International Trade
  • Fermentation ingredients may include cassava starch, sweet corn, and glucose.
  • glucose is used for fermentation as it is relatively inexpensive and abundant.
  • L-glutamic acid For obtaining L-glutamic acid, glucose or another suitable fermentation ingredient is added to a fermentation tank 100 containing a fermentation broth inoculated with Corynebacterium glutamicum or another suitable bacterium. Greater than 50% conversion of glucose to L-glutamic acid will typically require a total fermentation time of about 48 hours. For an output of about 50 grams of L- glutamic acid per liter of fermentation broth, the fermentation tank volume is preferably about 140 cubic meters per kilogram of hydrogen per hour. Following fermentation, the L-glutamic acid is extracted from the fermentation broth and separated from the secondary byproducts by conventional separation methods.
  • a first step in the preparation of monosodium glutamate is to react magnesium with a solution of L-glutamic acid.
  • a first reaction vessel 110 is provided in which magnesium and a L-glutamic acid solution are reacted.
  • the first reaction vessel may be a batch reactor. It is preferable to react the magnesium metal and L-glutamic acid via a series of batch reactors.
  • the batch reactors typically have a total volume of 3 to 5 cubic meters per kilogram of hydrogen per hour.
  • the reaction provides an enriched solution of magnesium di-glutamate and the generation of hydrogen gas.
  • the reaction mixture bubbles actively and hydrogen is expelled from the reaction mixture along with some water vapor.
  • the hydrogen gas is evacuated from the reactor vessel during the reaction and is bottled.
  • the hydrogen is evacuated, scrubbed, dehydrated and bottled to provide clean hydrogen gas suitable for use in the food industry or as a fuel.
  • the reaction between magnesium and L-glutamic acid is slightly exothermic.
  • the reaction is relatively slow at normal temperature and pressure (NTP, 20 degrees Celsius and one atmosphere pressure).
  • NTP normal temperature and pressure
  • the reaction rate can be increased by at least five times by increasing the reaction temperature to approximately 95°C.
  • L-glutamic acid has a fairly low solubility at NTP. Increasing the reaction temperature not only increases the reaction rate, but also the solubility of the L- glutamic acid, thus additionally increasing the reaction rate. As L-glutamic acid is converted to magnesium di-glutamate in solution, the non-dissolved L-glutamic acid begins to dissolve into the solution as well. As the L-glutamic acid conversion to magnesium di-glutamate begins to level off at approximately 80%, preferably, this step does not exceed 60 minutes.
  • the magnesium di-glutamate enriched solution can be reacted with sodium hydroxide, trisodium phosphate, or sodium carbonate in a second reaction vessel 120 to form monosodium glutamate in solution and a precipitate of magnesium hydroxide, magnesium phosphate, or magnesium carbonate respectively.
  • this step can be executed in a series of batch reactors having a total volume of approximately 3 to 5 cubic meters per kilogram of hydrogen per hour.
  • sodium carbonate is the preferred reactant as it is less expensive than sodium hydroxide.
  • trisodium phosphate is the preferred reactant as its byproduct precipitates more rapidly reducing the processing time.
  • the solubilities of the secondary byproducts magnesium hydroxide (9.63xlO "3 g/L) and magnesium carbonate (0.106 g/L) are both typically no greater than 0.01%, allowing for a preparation of 100 g/L having a maximum monosodium glutamate concentration of 99.9%.
  • magnesium carbonate can be precipitated most efficiently at high temperatures. Moderate agitation for approximately 45-60 minutes can further reduce the time required for precipitation.
  • the solubility of the secondary byproduct magnesium phosphate (at most 10 g/L) allows for a preparation of 100 g/L having a maximum monosodium glutamate concentration of 90%.
  • the magnesium is utilized in the form of 1 A inch granules. Utilization of granules increases the surface area of the magnesium and increases the speed of the reaction, while also maintaining the safety of the reaction.
  • other forms of magnesium may also be utilized.
  • magnesium in the form of plates, rods, powder, or alternative sized granules are also contemplated as being useful and are within the scope of the present disclosure.
  • the exemplary utilization of magnesium granules also allows for easier handling of the metal feed.
  • the magnesium is in the form of granules to facilitate easier automatic handling for feed systems to provide the magnesium to the reactor vessel than with larger forms of the magnesium.
  • the remaining water is evaporated or removed by utilizing an evaporator 140 or other means such as a dryer to provide dry monosodium glutamate powder. This may be done in a series of concentration steps.
  • a decompression method is used. This decompression effects a partial vaporization of the water present in the monosodium glutamate solution.
  • the geometry of the vessel only needs to permit the separation of the vapor phase from the liquid phase.
  • the reaction product is advantageously heated during decompression to assist the evaporation of the excess water.
  • the decompression stage incorporates a vacuum condenser which typically comprises a filter, condenser, vacuum pump and condensate receiving vessel.
  • the pump may be a Coanda effect pump, steam ejector or any other suitable pump.
  • alternative concentrating methods may also be utilized. Exemplary heating methods include solar and electrical. It is also contemplated that other drying methods may be used, alone or in combination with these.
  • the monosodium glutamate enriched solution may be concentrated using conventional methods prior to using an evaporator or dryer to remove any remaining water to provide the dry monosodium glutamate powder.
  • the monosodium glutamate enriched solution may be concentrated by heating prior to the step of utilizing an evaporator or dryer to recover the dry monosodium glutamate powder.
  • a crystallization vessel may be used to crystallize pure monosodium glutamate.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Zoology (AREA)
  • General Health & Medical Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Microbiology (AREA)
  • Biotechnology (AREA)
  • Combustion & Propulsion (AREA)
  • Biochemistry (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • General Engineering & Computer Science (AREA)
  • Genetics & Genomics (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)

Abstract

La présente invention concerne un procédé perfectionné pour la production simultanée d'hydrogène gazeux et de glutamate monosodique. Ledit procédé consiste : (a) à faire réagir du magnésium et une solution d'acide L-glutamique dans une cuve de réacteur pour obtenir de l'hydrogène et une solution de diglutamate de magnésium; (b) à évacuer l'hydrogène et le mettre en bouteille; (c) à combiner la solution de diglutamate de magnésium avec un carbonate de sodium, un phosphate trisodique ou un hydroxyde de sodium pour produire un sous-produit et une solution enrichie en glutamate monosodique; (d) à drainer, siphonner, et/ou filtrer la solution enrichie en glutamate monosodique; et (e) à utiliser un évaporateur ou un séchoir pour récupérer une poudre sèche de glutamate monosodique.
PCT/CA2008/000047 2007-01-18 2008-01-15 Procédé de production d'hydrogène et de glutamate monosodique Ceased WO2008086595A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US88552807P 2007-01-18 2007-01-18
US60/885,528 2007-01-18

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WO2008086595A1 true WO2008086595A1 (fr) 2008-07-24

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101942486A (zh) * 2010-09-07 2011-01-12 南京工业大学 一种利用味精发酵废弃菌体生产有机酸的方法
CN103039935A (zh) * 2012-12-17 2013-04-17 福建省建阳武夷味精有限公司 大米浸泡水用于味精生产的工艺
CN104211610A (zh) * 2014-07-31 2014-12-17 新疆阜丰生物科技有限公司 一种谷氨酸钠提取新工艺
CN115135767A (zh) * 2020-02-12 2022-09-30 大象株式会社 具有提高的l-谷氨酸生产能力的谷氨酸棒状杆菌突变体菌株，以及用于使用其生产l-谷氨酸的方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5907059A (en) * 1995-04-07 1999-05-25 Amylum Belgium N.V. Process for the preparation of monosodium glutamate
JP2003020201A (ja) * 2001-07-06 2003-01-24 Yoshiro Tanaka 水素発生装置及び水素発生体
CA2566475A1 (fr) * 2004-05-28 2005-12-08 Basf Aktiengesellschaft Production de produits chimiques fins par fermentation

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5907059A (en) * 1995-04-07 1999-05-25 Amylum Belgium N.V. Process for the preparation of monosodium glutamate
JP2003020201A (ja) * 2001-07-06 2003-01-24 Yoshiro Tanaka 水素発生装置及び水素発生体
CA2566475A1 (fr) * 2004-05-28 2005-12-08 Basf Aktiengesellschaft Production de produits chimiques fins par fermentation

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101942486A (zh) * 2010-09-07 2011-01-12 南京工业大学 一种利用味精发酵废弃菌体生产有机酸的方法
CN101942486B (zh) * 2010-09-07 2012-09-05 南京工业大学 一种利用味精发酵废弃菌体生产有机酸的方法
CN103039935A (zh) * 2012-12-17 2013-04-17 福建省建阳武夷味精有限公司 大米浸泡水用于味精生产的工艺
CN104211610A (zh) * 2014-07-31 2014-12-17 新疆阜丰生物科技有限公司 一种谷氨酸钠提取新工艺
CN115135767A (zh) * 2020-02-12 2022-09-30 大象株式会社 具有提高的l-谷氨酸生产能力的谷氨酸棒状杆菌突变体菌株，以及用于使用其生产l-谷氨酸的方法
CN115135767B (zh) * 2020-02-12 2024-03-15 大象株式会社 具有提高的l-谷氨酸生产能力的谷氨酸棒状杆菌突变体菌株，以及用于使用其生产l-谷氨酸的方法

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