WO2012021955A1 - Sistema e processo de correção de acidez a volume constante de meios fermentativos para produção de ácidos orgânicos - Google Patents
Sistema e processo de correção de acidez a volume constante de meios fermentativos para produção de ácidos orgânicos Download PDFInfo
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- WO2012021955A1 WO2012021955A1 PCT/BR2011/000287 BR2011000287W WO2012021955A1 WO 2012021955 A1 WO2012021955 A1 WO 2012021955A1 BR 2011000287 W BR2011000287 W BR 2011000287W WO 2012021955 A1 WO2012021955 A1 WO 2012021955A1
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- fermenter
- fermentative
- stream
- medium
- fermenters
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Classifications
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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
- 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
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M23/00—Constructional details, e.g. recesses, hinges
- C12M23/58—Reaction vessels connected in series or in parallel
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/02—Percolation
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/18—External loop; Means for reintroduction of fermented biomass or liquid percolate
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/26—Means for regulation, monitoring, measurement or control, e.g. flow regulation of pH
-
- 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
Definitions
- the present invention pertains to the field of systems and processes for obtaining organic acids by fermentation, more specifically to the constant volume acidity correction system and process of fermentative media.
- US Patent 4,882,277 claims a process in which glucose is continuously fermented to lactate and the resulting lactic acid is Subsequently extracted from the solution by electrodialysis where the pH within the fermenter is controlled by the removal of lactic acid at the same rate as it is formed as the fermenter content is recirculated in the electrodialysis unit.
- the disadvantage of this process refers to the fact that the bacteria present in the fermenter are absorbed in the ion exchange membranes present in the electrodialysis unit, causing the electrical resistance in the unit to increase and, consequently, increasing the energy consumption of the electrodialysis unit. process.
- cell death must be taken into account so that the total process productivity must be affected by the decrease in the number of producing cells.
- US 2006/0094093 claims the process of producing lactic acid at low pH by the use of an acid tolerant maize-derived homolactic bacterium which is capable of producing high levels of free lactic acid.
- Acid tolerant bacteria are capable of producing at least about 25 g / l free lactic acid. This type of bacteria can also generally produce about 50 g / l lactate in the fermentation medium at an average incubation pH of no more than 4.2.
- the productivity of the process described is such that the process is normally performed to produce about 1.0 to 3.0 gL -1 .h -1 in a medium whose average incubation pH is less than 4.0.
- lactate in salt form may return to the fermentation vessel and act as a pH buffer of the solution and prevent the pH of the reaction medium from falling below desired values.
- lactate salt reflux does not rule out the addition of other neutralizing agents such as calcium carbonate, sodium hydroxide and / or sodium bicarbonate which, in addition to increasing the cost, can significantly decrease overall process productivity.
- the cost of bacteria is higher than Lactobacillus sp. , commonly used for fermentative production of lactic acid.
- the present invention relates to a system for constant volume acidity correction in fermentative media
- a system for constant volume acidity correction in fermentative media comprising at least one fermenter (1) having at least one sensor for real time determination of the pH of the fermentative medium (PI). ), a filtration module (2), a base addition vessel (3), a first pump for pumping fermenter broth into said filtration module (BI), a second pump for pumping the basified fermentation broth fraction return to the fermenter (B2) and a heat exchanger (5), the volumetric proportions of alkaline solution for pH correction to be added to the removed fermenter fraction being established by a controller connected to said at least one sensor (PI), said first pump (BI), said second pump (B2), said heat exchanger (5) and defined herein as base doser (4), so as to enable the outlet flow from the fermenter (1) , the amount base age added to the solution in said addition vessel (3) and the return flow rate of the alkaline solution to said fermenter (1) are appropriate and in accordance with the need to adjust the pH of the medium
- the present invention provides a system for constant volume acidity correction in fermentative media, the system comprising at least one fermenter having at least one sensor, a base addition vessel and a base doser, a first pump for pumping fermenter broth for a filtration module, a second pump for pumping the fraction of the fermenter back basified fermentation broth and a heat exchanger, the volumetric proportions of alkaline solution for pH correction to be added to the fraction removed from the fermenter being established by a controller connected to said at least one sensor, said first pump, said second pump, said heat exchanger and the base metering element.
- the invention further provides a constant volume acidity correction process in fermentative media, said process being optimized by a reflux system of the culture medium under appropriate pH conditions such that when the culture medium returns to the fermenter an adjustment occurs. acidity of the reaction medium with higher productivity without causing an increase in reaction volume.
- An advantage of said constant volume acidity correction process in fermentative media of the present invention is that it provides significant energy savings in the process as a whole.
- the process of the present invention provides a reduction of the environmental impact by the input and energy saving.
- FIG. 1 is a simplified flow diagram of the process of the invention for acidity correction of fermentative media at constant volume.
- the attached Figure 2 is a simplified flowchart of the process control layout of the invention.
- FIG. 3 is a simplified flowchart of the process of the invention adapted for a reactor assembly so that the permeate alkalinization process can operate continuously.
- the present invention is based on the fact that the addition of alkaline substances to fermentative means of organic acid production causes a significant increase in the volume of the fermentative medium, which necessarily implies an increase in the amount of energy required to separate the lactic acid synthesized from its reaction medium.
- part of the fermentative medium may be removed from the fermentation vessel, filtered to retain microorganisms, added with alkalizing element and then returned to the defined volume fermentative medium to adjust the pH of the culture medium. at values within the optimal operating limits.
- Most microorganisms have an optimal range of pH values in which their metabolism is optimized and thus the pH of a given fermentative medium is a variable that greatly affects process productivity.
- Microorganisms such as Lactobacillus sp. they are conventionally used as lactic acid producers and, in a fermentation process conducted by these microorganisms, pH values fall rapidly with lactic acid production to levels that may inhibit cell metabolism or even cause cell death.
- alkaline agents to the fermentative medium is capable of maintaining pH values at appropriate levels for maximum lactic acid production.
- Recommended pH values of the reaction medium for good lactic acid productivity are between 5.0 and 7.0 (see US Patent 5,510,526).
- Equation 1 The theory of chemical equilibrium, when applied to weak acids, such as lactic acid, and others obtained in fermentative processes, defines that, in solution, lactic acid dissociates according to the following equation (equation 1):
- the pH of the solution will be kept at a constant value, which may be adjusted, preferably between 4.0 and 7.0, to maximize acid production. organic by microorganisms.
- compositions of fermentative media for culturing various types of microorganisms are proposed in the technical and scientific literature and already commercially available.
- MRS from its inventors of Man, Rogosa and Sharpe
- MRS composition of fermentative media for culturing various types of microorganisms
- polysorbate 80 also known as Tween
- This composition is recommended for cultures of microorganisms such as: Lactobacillus acidophilus, Lactobacillus casei, Lactobacillus fermentum, Escherichia coli, Pseudomonas aeruginosa, among others.
- Modifications and adaptations of MRS medium are also already available in the market, aiming to cover the types of micro ⁇ organisms to be cultivated.
- the typical fermentation process takes place in an appropriate temperature-controlled fermenter in which microorganisms are maintained by adjusting the broth composition under optimal conditions for the production of organic acid over periods of 18 to 36 h.
- the process temperature is maintained between 25 ° C and 42 ° C.
- the fermenter is also equipped with a pH measuring probe so that the monitoring of the acidity of the medium can be done continuously. Once the pH values at which lactic acid production decreases, a certain volume of basic solution should be added to the medium in order to raise the pH values to working levels.
- An aspect of the present invention is a system for constant volume acidity correction in fermentative media comprising at least one fermenter having at least one sensor for real time determination of the pH of the fermentative medium, a filtration module, a vessel for addition base and a base doser, a first pump for pumping fermenter broth from the fermentation to said filtration module, a second pump for pumping the fermenter return basified fermentation broth fraction and a heat exchanger, the volumetric proportions of solution alkaline for pH correction to be added to the fraction removed from the fermenter being set by a controller.
- Another aspect of the invention is the acidity correction process of fermentative media using the inventive system.
- the fermenter (1) is connected to a system for withdrawing, alkalizing and returning a certain volume of medium, as shown in Figure 1.
- a flow pump which is responsible for bringing part of the broth (stream (A)) to a filtration module (2) containing a filter element (not represented).
- the current (A) may have an identical concentration or close to that of the fermentation broth with pH values equal to or lower than ideal for the cultivation of microorganisms and temperature close to the values found inside the fermentation tank.
- (B) contains all elements of the reaction medium present in the fermenter (1) except non-permeated solids with pH values between 4.0 and 7.0 and temperature between 25 ° C and 42 ° C.
- the retained solids can be returned to the reaction medium, giving rise to stream (C), so as to keep the concentration of the microorganisms constant in the fermentative medium and, in turn, ensuring the highest possible production of organic acid.
- Stream (C) contains essentially Lactobacillus sp. Cells, cell debris, and may also contain inorganic solid residues inherent in the fermentation process and medium composition.
- the filtration module (2) shall be provided with a pore diameter filter media between 0,5 and 5 ⁇ and more preferably 1 ⁇ .
- a pore diameter filter media between 0,5 and 5 ⁇ and more preferably 1 ⁇ .
- filter elements can be used in the filtration system such as bag filters, preferably composed of microstructural membranes with tangential filtration system, in order to promote the retention of most solids present in the fermentative medium and especially of the micro-filters. enabling the eventual return of same to the culture medium without causing major losses to the fermentation process.
- the stream (B) is fed to a mixing tank (3), where a certain amount of base is added via a dosing element (4).
- a certain amount of base is added via a dosing element (4).
- the bases added to the broth permeate can be both organic and inorganic, preferably KOH, NaOH, Ca (OH) 2 or NH 4 0H.
- the base in liquid form may be added manually or preferably by means of metering equipment (4) positioned at the top of said mixing tank (3).
- the alkaline solution (stream (D)) with the same composition as stream (B) plus base added to the mixing tank (3), with temperatures between 30 ° C and 60 ° C and pH values. between 6 and 9, preferably larger than 7, may be transported via a heat exchanger (5) which will be responsible for conditioning the alkaline solution at the working temperature of the process so as not to interfere with the fermentation process.
- heat drawn from the solution through the heat exchanger coolant (5) can be brought to the fermentation tank (1) so as to maintain the temperature of said fermentation tank (or said tanks) at values suitable for the production of organic acids.
- reactor current (D)
- pH of the medium at a given point in the organic acid production process.
- FIG 2 schematically illustrates the control layout employed in the process described so that pumps (BI) and (B2) can provide sufficient flow rates for the fermentation process to take place within the recommended or empirically defined pH range. for maximum organic acid production.
- the system of the invention as illustrated in Figure 2 is generally designated by numeral 100.
- the sensor element (PI) is positioned within the fermenter medium of the fermenter (1) to monitor the change in pH value in real time during the process, and may also be an arrangement or set of sensor elements (not shown) which lead to greater measurement accuracy. Sensor elements (PI) are commercially available pH sensors.
- the element (PI) is connected via line (ll) to the controller element (CT).
- the controller element (CT) is also responsible for controlling: i) the flow of fermentative media solution, current (A), through connection to the pump (BI) via (L2); ii) the basic solution flow rate through line (L3); iii) the flow of alkaline solution of fermentative medium, current (D), through connection to the pump (B2) via (L4) and iv) the flow of the refrigerant in the heat exchanger (5) via (L5), of keep the temperature within the working range of the process.
- the controller element consists of a commercially available equipment widely used in the industrial process control segment, which is equipped with a dedicated software (called supervisory system) in order to offer an easy-to-operate interface as well as a real-time control of the process as a whole.
- the CT receives and interprets all information from the sensors installed throughout the process and, through instructions programmed in its memory, performs specific actions (pump flow control, temperature control, pH control, valve opening and closing). ) according to the conditions of the sensors in real time, allowing a high level of automation in the control of the various process steps in question.
- Figure 3 represents the process described above adapted for a set of reactors so that the permeate alkalinization process, represented by stream (B), can operate continuously while different batches in different fermentation tanks (tanks (1.1), (1.2 ), (1.3), (1.4)) are performed alternately.
- the system of Figure 3 is generally designated by numeral 200.
- FIG 3 represents an arrangement of two sets of two fermenters in series.
- Streams (Cl), (C2), (C3) and (C4) are formed by the flow divider equipment (DV2) from stream (C) which can essentially be formed by Lactobacillus sp cells. or cell debris, and may also contain inorganic solid residues inherent in the fermentation process and the composition of said media.
- Said flow divider equipment is also connected to the central control element (CT) via a line (L7) in order to control the inlet flow of retained solids (Lactobacillus sp. Cells or cell debris, inorganic solid waste ) in said fermenters (1.1), (1.2), (1.3) and (1.4).
- Said flow divider equipment (DV3) is also connected to the central control element (CT) via a line (L8) in order to control the flow of the entry of the basic juice into said fermenters (1.1), (1.2), (1.3) and (1.4).
- streams (Al), (A2), (A3) and (A) are essentially composed of the fermentation broth contained in the respective tanks with temperature and pH values close to the optimum production values of Organic acid.
- the fermenters (1.2), (1.3) and (1.4) may be inactive or at another time. process that does not require correction by adding alkaline solution.
- (DV1) is restricted to the control of the output flow rates of the reaction media in operation at a given point in the process.
- the stream (A2) can be directed to said module (2) without the need for all of the process is completed before starting a new batch. Thus, the same can be done continuously.
- the described system can operate continuously, 24 hours a day, by alternating the presented fermenters. It should be clear to those skilled in the art that more fermenters may be added to the process without departing from the scope of the invention, such a procedure being within the skill of the art.
- a typical MRS fermentation broth consisting of:
- polysorbate 80 also known as Tween
- This Example is illustrative of the process of the invention.
- An MRS-type fermentation broth as set forth in Example 1 herein, composed as described in Example 1 and incubated with the same cell type in a volume of 1000 L under agitation for 18 hours at 39 ° C and pH 7.2 to maintain production in the 3.0 kg / h range required an amount equivalent to 120 l of the reaction volume to be removed, filtered and made alkaline with 36 kg of NaOH and then fed back into the medium. reaction, occurring with a energy expenditure equivalent to 0.67 KW / h including all stages of transport (pumps), filtration, dosing, monitoring and process control.
- the overall amount of energy saved in a plant to produce 72 kg of organic acid per day will be approximately 74.7 kW / h, leading to an energy consumption of 1.03 kW / h per kilogram of acid produced. That is, with 11.8% savings in energy consumption in a subsequent process of separation and purification of the production medium.
- This Example illustrates the substantial energy savings provided by the process of the invention when applied to a multi-reactor system.
- the fermentation broth withdrawal, filtration and alkalization system was connected to a set of 4 (four) fermentative reactors (1.1, 1.2, 1.3 and 1.4) as shown in Figure 3 of this report.
- the reactors were put into operation with a difference of 6 hours between the start of each process, so that the broth removed from one fermenter could be used in another fermenter, leading to a proportional decrease of the circulating volume in the alkalinization process equivalent to 7 , 5% of the total volume incubated in the four reactors, compared to 12% used in the single reactor system.
- the total process energy expenditure was equivalent to 1.65 KW / h including all stages of transport (pumps), filtration, dosing, monitoring and process control.
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Abstract
Description
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Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP11817591.8A EP2607472A4 (en) | 2010-08-19 | 2011-08-17 | A SYSTEM AND METHOD FOR THE CORRECTION OF THE ACID IN A CONSTANT VOLUME OF A FERMENTATION MEDIUM FOR THE PRODUCTION OF ORGANIC ACIDS |
US13/817,751 US20130157329A1 (en) | 2010-08-19 | 2011-08-17 | System and process for correcting constant volume acidity of fermentative media for producing organic acids |
JP2013524311A JP2013535224A (ja) | 2010-08-19 | 2011-08-17 | 有機酸生産用発酵培地の酸性度を定容で補正するためのシステム及び方法 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
BRPI1004963-0 | 2010-08-19 | ||
BRPI1004963-0A BRPI1004963A2 (pt) | 2010-08-19 | 2010-08-19 | Sistema e processo de correção de acidez a volume constante de meios fermentativos para a produção de ácidos orgânicos |
Publications (1)
Publication Number | Publication Date |
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WO2012021955A1 true WO2012021955A1 (pt) | 2012-02-23 |
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Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/BR2011/000287 WO2012021955A1 (pt) | 2010-08-19 | 2011-08-17 | Sistema e processo de correção de acidez a volume constante de meios fermentativos para produção de ácidos orgânicos |
Country Status (5)
Country | Link |
---|---|
US (1) | US20130157329A1 (pt) |
EP (1) | EP2607472A4 (pt) |
JP (1) | JP2013535224A (pt) |
BR (1) | BRPI1004963A2 (pt) |
WO (1) | WO2012021955A1 (pt) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
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JP7231355B2 (ja) * | 2018-08-22 | 2023-03-01 | 日機装株式会社 | 細胞培養方法および細胞培養装置 |
CN114317241B (zh) * | 2021-12-29 | 2023-01-31 | 江苏集萃中科纳米科技有限公司 | 一种重组基因工程菌试发酵平台 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2686897A1 (fr) * | 1992-02-05 | 1993-08-06 | Sonertec | Procede en continu de fabrication d'acides organiques. |
US6596521B1 (en) * | 1999-04-13 | 2003-07-22 | Korea Advanced Institute Of Science And Technology | Method for manufacturing organic acid by high-efficiency continuous fermentation |
EP1496108A1 (en) * | 2002-03-26 | 2005-01-12 | New Century Fermentation Research Ltd. | Method of continuous culture of anaerobic bacterium |
WO2009006909A1 (en) * | 2007-07-10 | 2009-01-15 | Nordbiochem OÜ | Process for producing organic acids by continuous fermentation |
Family Cites Families (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS62146595A (ja) * | 1985-12-20 | 1987-06-30 | Daicel Chem Ind Ltd | 醗酵による有機酸の連続製造方法 |
EP0239272B1 (en) * | 1986-03-19 | 1993-03-03 | Biotechna Limited | Improvements relating to biomass production |
JP2643314B2 (ja) * | 1988-06-13 | 1997-08-20 | 株式会社日立製作所 | pH調整,アンモニア除去機能を有する生物細胞培養方法及びその培養装置 |
US5766439A (en) * | 1996-10-10 | 1998-06-16 | A. E. Staley Manufacturing Co. | Production and recovery of organic acids |
US6475759B1 (en) * | 1997-10-14 | 2002-11-05 | Cargill, Inc. | Low PH lactic acid fermentation |
CA2414012A1 (en) * | 2000-05-30 | 2001-12-06 | Birgir Norddahl | Method for producing lactic acid |
JP2002085049A (ja) * | 2000-09-07 | 2002-03-26 | Chiyoda Manufacturing Co Ltd | 複合培養装置 |
JP2007215427A (ja) * | 2006-02-14 | 2007-08-30 | Musashino Chemical Laboratory Ltd | 乳酸の製造方法 |
JP5082496B2 (ja) * | 2006-02-24 | 2012-11-28 | 東レ株式会社 | 連続発酵による化学品の製造方法および連続発酵装置 |
BRPI0707027B1 (pt) * | 2006-02-24 | 2022-08-16 | Toray Industries, Inc | Método de fabricação de um produto químico e aparelho de fermentação contínua |
DE102008015386B4 (de) * | 2008-03-20 | 2015-10-01 | Sartorius Stedim Biotech Gmbh | Bioreaktor |
-
2010
- 2010-08-19 BR BRPI1004963-0A patent/BRPI1004963A2/pt not_active IP Right Cessation
-
2011
- 2011-08-17 EP EP11817591.8A patent/EP2607472A4/en not_active Withdrawn
- 2011-08-17 US US13/817,751 patent/US20130157329A1/en not_active Abandoned
- 2011-08-17 JP JP2013524311A patent/JP2013535224A/ja active Pending
- 2011-08-17 WO PCT/BR2011/000287 patent/WO2012021955A1/pt active Application Filing
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2686897A1 (fr) * | 1992-02-05 | 1993-08-06 | Sonertec | Procede en continu de fabrication d'acides organiques. |
US6596521B1 (en) * | 1999-04-13 | 2003-07-22 | Korea Advanced Institute Of Science And Technology | Method for manufacturing organic acid by high-efficiency continuous fermentation |
EP1496108A1 (en) * | 2002-03-26 | 2005-01-12 | New Century Fermentation Research Ltd. | Method of continuous culture of anaerobic bacterium |
WO2009006909A1 (en) * | 2007-07-10 | 2009-01-15 | Nordbiochem OÜ | Process for producing organic acids by continuous fermentation |
Non-Patent Citations (1)
Title |
---|
See also references of EP2607472A4 * |
Also Published As
Publication number | Publication date |
---|---|
BRPI1004963A2 (pt) | 2015-03-24 |
US20130157329A1 (en) | 2013-06-20 |
EP2607472A4 (en) | 2015-07-29 |
JP2013535224A (ja) | 2013-09-12 |
EP2607472A1 (en) | 2013-06-26 |
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