Method for preparing organic acid by fed-batch-feeding carbon source substrate and base

Abstract

The present invention provides a fed-batch culture method comprising a step of fed-batch-feeding a carbon source base and a base in such a manner that the pH level can be maintained at a level suitable for the growth of microorganisms for fermentation of a carbon source. The present invention also provides a method for preparing organic acids using the fed-batch culture method. The present invention fed-batch-feeds a neutralizing agent such as ammonium bicarbonate, ammonium carbonate or alkali metal-containing weak base, and a carbon source substrate in preparing organic acids by microorganism fermentation. Thus, a pH level suitable for the survival of microorganisms for carbon source fermentation can be maintained, and the speed of injecting the carbon source base which is the source material can be appropriately adjusted. The present invention may improve productivity, yield rate and concentration of organic acids and may automatically inject a base and a carbon source substrate according to a variation in the pH level, thus improving reliability and convenience of a fermentation process operation.

Claims

1. A method for producing an organic acid by fed-batch culture, comprising: (i) preparing a culture medium containing a carbon source substrate, an organic acid-producing strain of bacteria, and a growth ingredient for said strain of bacteria; (ii) fermenting said culture medium to produce said organic acid; (iii) measuring a pH change in said culture medium; (iv) correlating said pH change to consumption of said carbon source substrate; (v) fed-batch feeding additional substrate-base mixture of carbon source substrate and an alkali metal containing weak base to said culture medium in an amount to maintain concentration of said carbon source substrate, and said alkali metal containing weak base in an amount to matain optimal pH for growth of said strain of bacteria, and (vi) removing any organic acid produced in said culture medium; wherein ratio of carbon source substrate to alkali metal containing weak base is 200300 g/L to 80120 g/L, wherein CO.sub.2 and H.sub.2 gases are generated during said fermenting, and when CO.sub.2 and H.sub.2 gases reach a generation rate of 1.5-2.5 L/L of fermenter/hr, terminating the feeding the substrate-base mixture so that said fermenting proceeds until said carbon source substrate is completely consumed.

2. The method of claim 1, wherein, after completion of the feeding of the substrate-base mixture, ammonia water, alkali metal hydroxide solution, alkaline earth metal hydroxide solution, or a combination thereof is supplied to said fermenter to allow the culture medium to have a pH value optimal for growth of the organic acid-producing strain until the carbon source substrate is completely fermented.

3. The method of claim 1, wherein the growth ingredient is at least one selected from the group consisting of a nitrogen source, a vitamin, a mineral, and a carbon source degrading enzyme.

4. A method for producing butyric acid by fed-batch culture, comprising; (i) preparing a culture medium containing a carbon source substrate, a butyric acid-producing strain of bacteria, and a growth ingredient for the strain of bacteria; (ii) fermenting said culture medium to produce said butyric acid; (iii) measuring a pH change in said culture medium; (iv) correlating said pH change to consumption of said carbon source substrate; (v) fed-batch feeding additional substrate-base mixture of carbon source substrate and at least one base selected from the group consisting of ammonium bicarbonate, sodium bicarbonate, potassium bicarbonate, ammonium carbonate, sodium carbonate, potassium carbonate and mixture thereof, in an amount to matain a pH of said culture medium to have a pH of 4.5 to 7; and (vi) removing any butyric acid produced in said culture medium; wherein ratio of carbon source substrate to said at least one base is 200300 g/L to 80120 g/L, wherein CO.sub.2 and H.sub.2 gases are generated during said fermenting, and when CO.sub.2 and H.sub.2 gases reach a generation rate of 1.5-2.5 L/L of fermenter/hr, terminating feeding said substrate-base mixture so that said fermenting proceeds until the carbon source substrate is completely consumed.

5. The method of claim 4, wherein said butyric acid-producing strain of bacteria is a Clostridium sp. microorganism.

6. The method of claim 1, wherein said carbon source substrate is selected from the group consisting of glucose, fructose, sucrose, galactose, xylose, arabinose, sugar cane, molasses, and starch hydrolysate.

7. The method of claim 1, wherein the organic acid is at least one selected from the group consisting of butyric acid, lactic acid, acetic acid, formic acid, citric acid, adipic acid, succinic, acid, fumaric acid, malic acid, 3-hydroxypropionic acid, glutamic acid, glutaric acid, glucaric acid, itaconic acid, acrylic acid, and muconic acid.

8. The method of claim 1, wherein the organic acid-producing strain is selected from the group consisting of Clostridium spp., Pseudomonas spp., Rhizopus spp., Aspergillus spp., Corynebacterium spp., Actinobacillus spp., yeast, Candida yeast, Pichia yeast, E. coli, and lactic acid producing bacteria.

9. The method of claim 1, comprising fermenting said culture medium in a fermenter equipped with a pH control sensor, a gas meter or both.

Description

DESCRIPTION OF DRAWINGS

(1) FIG. 1 is a schematic view of a system in which an organic acid is produced by fed-batch culture in accordance with an embodiment of the present invention.

(2) FIG. 2 shows production profiles of the product butyric acid and the by-product acetic acid.

MODE FOR INVENTION

(3) The present invention is based on the fact that there is direct correlation between the consumption of carbon source by microorganisms and the content of produced organic acids (e. g. lowered pH). A culture for producing an organic acid becomes low in the content of a carbon source and in pH as the organic acid is produced. In the present invention, a substrate-base mixture of a carbon source and at least one base selected from among ammonium bicarbonate and an alkali metal-containing weak base is supplied in a fed-batch type to supplement the lowered content of a carbon source and to increase the lowered pH value due to production of the organic acid, thereby improving the productivity of the organic acid.

(4) Strong bases such as NaOH, KOH, and Ca(OH).sub.2 may be employed to neutralize organic acids produced in a culture, but they, inter alia, calcium (Ca)-containing bases, are highly apt to denature and precipitate proteins. Entering a medium, such strong bases denature a nitrogen source to inhibit the utility of the nitrogen source by microorganisms, resulting in a decrease in fermentation efficiency. Hence, a weak base, particularly, ammonium bicarbonate, or an alkali metal-containing weak base such as sodium bicarbonate, potassium bicarbonate, etc., or both are used in neutralizing organic acids in the present invention. Ammonium bicarbonate is advantageous because it can act as a nutrient source of ammonium ions necessary for the growth of microorganisms, as well.

(5) Below, a detailed description will be given of the present invention.

(6) An aspect of the present invention addresses a method for producing an organic acid through fermentation of a carbon source substrate, comprising feeding a substrate-base mixture containing i) a carbon source substrate; and ii) at least one base selected from among ammonium bicarbonate, ammonium carbonate, and an alkali metal-containing base in a fed-batch manner to a bioreactor containing a carbon source substrate and an organic acid-producing strain to maintain pH suitable for growth of microorganisms fermenting the carbon source substrate.

(7) According to one embodiment thereof, the present invention provides a method for producing an organic acid by fed-batch culture, comprising:

(8) preparing a culture medium containing a carbon source substrate, an organic acid-producing strain, and an essential ingredient for growth of the strain (strain growth ingredient);

(9) fermenting the carbon source substrate in an optimal condition established by feeding a substrate-base mixture of a carbon source substrate and at least one base selected from ammonium bicarbonate, ammonium carbonate, and alkali metal-containing weak base in a fed-batch manner to the culture medium to allow the culture medium to have a pH value optimal for growth of the organic acid-producing strain; and

(10) recovering the organic acid from the culture medium, the organic acid being produced with the fermentation of the carbon source substrate.

(11) The term weak base is meant as a base containing an alkali metal of Group 1 in the Periodic Table, as exemplified by sodium bicarbonate and potassium bicarbonate.

(12) In one embodiment of the present invention, the carbon source substrate may be a sugar that may in the form of monosacharrides, disaccharides, polysaccharides, and a combination thereof. Examples include, but are not limited to, glucose, fructose, sucrose, galactose, mannose, xylose, arabinose, sugar cane, molasses, and starch hydrates.

(13) Content ratios between carbon source substrate and base in the substrate-base mixture to be supplied during fermentation may be adjusted in concert with fermentation characteristics in consideration of the solubility of the base and the production rate of the organic acid. Under the assumption that the carbon source substrate and the base are maintained aseptically, the content ratio between carbon source substrate and base may be adjusted even while the fermentation process is running.

(14) The carbon source substrate fed in the fed-batch manner may be the same or different from the carbon source substrate initially contained in the culture medium the bioreactor.

(15) Within the scope of the ingredient essential for the growth of the microorganism strain, a nitrogen source, a vitamin, an inorganic salt, and/or a carbon source decomposing enzyme such as an invertase in addition to the carbon source substrate may fall. A person of ordinary skill in the art may readily determine ingredients necessary for the growth according to the strain.

(16) Among the range of the organic acid that can be produced in the fed-batch culture method of the present invention are butyric acid, lactic acid, acetic acid, formic acid, citric acid, adipic acid, succinic acid, fumaric acid, malic acid, 3-hydroxypropionic acid, glutamic acid, glutaric acid, glucaric acid, itaconic acid, acrylic acid, and muconic acid, which are known to be useful as biofuels and biochemicals.

(17) So long as it produces an organic acid, any microorganism may be used as the organic acid-producing strain in the present invention. The organic acid-producing strain may be selected from among Clostridium spp., Pseudomonas spp., Rhizopus spp., Aspergillus spp., Corynebacterium spp., Actinobacillus spp., yeast, Candida spp., Pichia spp., E. coli, and lactic acid bacteria. Concrete examples of the organic acid-producing strain include Clostridium tyrobutyricum, C. butyricum, C. acetobutyricum, Pseudomonas aeruginosa, P. putida, P. fluorescens, Rhizopus arrhizus, R. oryzae, Aspergillus oryzae, Corynebacterium glutamicum, and Lactobacillus acidophilus.

(18) Fermentation conditions proper for individual strains are known in the art.

(19) As used herein, the term optimal condition in context with strain growth means an environment, including an anaerobic condition, a temperature range, and a pH range, under which a microorganism strain grows, with the concomitant maximal production of the organic acid. The optimal condition may be changed depending on the strain used. The person having ordinary skill of the art may adjust the environment of the bioreactor into an optimal condition depending on the growth stage of the microorganism strain. For example, the bioreactor may be set to be heated or cooled to a temperature of 20 to 50 C. while the culture medium may have a pH of 4 to 7.

(20) Also, contemplated in one embodiment of the present invention is a method for producing butyric acid by fermenting sugars in the presence of a Clostridium strain, with the supply of sugars and at least one base selected from among sodium bicarbonate and potassium bicarbonate in a fed-batch manner As needed for fermentation, a carbon source substrate, a nitrogen source, vitamins and minerals and/or an enzyme such as invertase may be added to the culture medium.

(21) More particularly, the present invention provides a method for producing butyric acid by fed-batch culturing, comprising:

(22) preparing a culture medium containing a carbon source substrate, a butyric acid-producing microorganism strain, and an essential ingredient for growth of the strain (growth essential ingredient);

(23) fermenting the carbon source substrate in an optimal condition established by feeding a substrate-base mixture of a carbon source substrate and at least one base selected from ammonium bicarbonate, sodium bicarbonate, and potassium bicarbonate in a fed-batch manner to the culture medium to allow the culture medium to have a pH of 4.5 to 7; and

(24) recovering butyric acid from the culture medium, the butyric acid being produced with the fermentation of the carbon source substrate.

(25) The butyric acid-producing microorganism strain may be a Clostridium sp., and may be selected from the group consisting of C. tyrobutyricum, C. butyricum, and C. acetobutyricum.

(26) With reference to FIG. 1, an embodiment of the present invention is explained.

(27) The present invention is configured to feed a neutralizing solution containing a carbon source substrate and a base (e g., ammonium bicarbonate) in a fed-batch manner from a feeding tank to a fermenter where a carbon source substrate is fermented in the presence of a microorganism to produce an organic acid.

(28) The fermenter may be equipped with a pH control sensor and/or a gas meter.

(29) The pH control sensor aims to establish an optimal pH for the growth of the organic acid-producing microorganism in the culture medium in the fermenter. Within the fermenter, typical ingredients necessary for microorganism growth, such as a nitrogen source, may exist along with the carbon source substrate. When the pH of the culture medium deviates from a predetermined range as fermentation proceeds, the system is designed to automatically feed a mixture of a carbon source substrate and a base (e.g., ammonium bicarbonate). pH values suitable for the growth of individual organic acid-producing microorganisms are known in the art. For instance, when butyric acid is produced, an optimal pH value for the growth of butyric acid-producing microorganism is in the range of 4.5 to 7.

(30) Together with or separately from the pH control sensor, a gas meter may be installed in the fermenter to measure the generated amount and generation rate of gas in the fermenter. The generation rate of gas provides information on the feeding rate of the substrate-base mixture or the time to terminate the feeding.

(31) As described above, the time at which the feeding of the substrate-base mixture is terminated may be readily determined in consideration of the gas generation rate and the fed amount of the mixture by a person having ordinary skill.

(32) As a rule, fermentation is inhibited by its end product (product inhibition). As the fermentation is carried out, the activity of the microorganism strain is decreased by the organic acid product. Often, fermentation may stop even when the carbon source substrate is not fully consumed. In this case, the carbon source substrate is wasted. In the present invention, a weak base such as ammonium bicarbonate is used as a neutralizer to prevent the microorganism strain from being influenced by high pH. The base neutralizes an organic acid such as butyric acid, with the concomitant generation of carbon dioxide (CO.sub.2) and hydrogen (H.sub.2) gas. The generation rate of the gas may be utilized to monitor the activity of the microorganism strain, providing the information of a proper time until the carbon source substrate is supplied. In the present invention, therefore, fermentation can be performed with the complete consumption of the carbon source substrate. Accordingly, since the supply of a carbon source substrate can be stopped at a proper time point to avoid the loss of remaining carbon source substrate, the fermentation process can be effectively operated with the maintenance of optimal activity in the microorganism. After completion of the feeding of the carbon source substrate and the base, the pH of the fermenter can be adjusted in a method known in the art, for example, by feeding a pH adjusting agent, such as ammonia water, alkali metal hydroxide solution, alkaline earth metal hydroxide solution a mixture thereof, e. g. sodium hydroxide, calcium hydroxide, potassium hydroxide, etc. at a constant rate.

(33) In addition, when the fed-batch culture method according to the present invention is applied to fermentation for organic acid production, the culture medium described in the present invention can be used, instead of an expensive culture medium for the seed cultivation of bacterial fermentation, in the last stage of the culture for a seed train, thus greatly improving the economy of fermentation. Conventional butyric acid fermentation employs an RCM (Reinforced Clostridial Medium) or a similar nutrient-rich medium for a seed culture to improve the efficiency of the main culture. However, this expensive seed culture medium is a cause of increasing the production cost, degrading the economy of fermentation. In contrast, the fed-batch cultivation according to the present invention allows the culture medium for the last seed train to be employed in the main culture without a decrease in the activity of the microorganisms.

(34) A better understanding of the present invention may be obtained through the following examples which are set forth to illustrate, but are not to be construed as limiting the present invention.

EXAMPLES

Comparative Example 1

Batch Culture

(35) Sugar cane liquid and minerals (sugar concentration 150200 g/L, 30 L) were placed in a 50 L anaerobic fermenter that was purged with nitrogen. Under this anaerobic condition, Clostridium tyrobutyricum was inoculated in a volume of 1%20% of the broth to which ammonia water was then added so as to adjust the pH to 6.0. As fermentation proceeded at 37 C., carbon dioxide (CO.sub.2) and hydrogen (H.sub.2) were generated, maintaining the anaerobic condition.

EXAMPLE 1

Fed-Batch Culture

(36) In a 50 L anaerobic fermenter, the same microorganism as in Comparative Example 1 was inoculated into sugar cane liquid and minerals (sugar concentration 2040 gIL, 1015 L), and then cultured at 37 C. while feeding a mixture of ammonium bicarbonate and sugar cane liquid (ammonium bicarbonate 80120 g/L, sugar concentration 200300 g/L, 1520 L) to maintain the broth at a pH of 6.0. The fed-batch cultivation started with a smaller volume of a culture medium, compared to the batch cultivation, but the final volume of each culture medium was identical. Alternatively, the final volume could be adjusted. With the progress of the fermentation, CO.sub.2 and H.sub.2 gases were generated. When the generation rate of the gas was monitored to reach 1.52.5 L/L of fermenter/hr, the feeding of the mixture of ammonium bicarbonate and sugar cane liquid was terminated so that the fermentation proceeded until the sugar, fed up until that point, was completely consumed.

(37) Both the cultivation methods of Comparative Example 1 and Example 1 produced butyric acid at a concentration of 6% or higher. For comparison, the two methods were examined for efficiency at the time point when the same concentration of butyric acid was achieved. Measurements of cell concentration (OD.sub.600-MAX), productivity of butyric acid (P.sub.BA), production yield of butyric acid (Y.sub.BA), and production yield of acetic acid (Y.sub.AA) for Comparative Example 1 (batch culture) and Example 1 (fed-batch culture) are given in Table 1, below.

(38) TABLE-US-00001 TABLE 1 P.sub.BA Y.sub.BA Y.sub.AA OD.sub.600-MAX (g/L/hr) (g BA/g sugar) (g AA/g sugar) Comparative 56.6 1.31 0.376 0.051 example 1 example 1 59 1.4 0.454 0.004

(39) As is understood from data of Table 1, the fed-batch cultivation was superior in all indices to the batch cultivation. Particularly, the production of the by-product acetic acid (AA) was greatly inhibited in Example 1, with the consequent significant improvement of butyric acid in production yield. This increase in fermentation performance is understood to result from the maintenance of sugar at such a concentration as not to inhibit the growth of the microorganism. In contrast, the batch cultivation of Comparative Example 1 could not further ferment the sugar even when it maintained the initial concentration because the microorganism state differed from one batch to another. As a result, the sugar was not consumed completely, but remained In the fed-batch culture, the sugar could be completely consumed without loss because the time to stop supplying sugar could be controlled under the monitoring of the CO.sub.2 and H.sub.2 gas generation according to fermentation progress. The production yield of butyric acid (BA) according to the present invention was greatly increased, compared to the conventional batch culture or the stepwise addition of sugar in aliquots (refer to Comparative Example 2, below), demonstrating that the feeding of the sugar in mixture with ammonium bicarbonate for adjusting pH is highly reliable and efficient.

Example 2

Fed-Batch Culture by Feeding Mixture of Ammonium Bicarbonate and Medium

(40) In this Example, fed-batch culture was demonstrated to greatly improve the concentration butyric acid (BA). Because BA itself is toxic to the microorganism that produces BA, it inhibits the activity of the microorganism (product inhibition), which results in no further production of the product even when the substrate sugar is present. Accordingly, the production yield of the acid is limited or the sugar is wasted. This Example was designed to maintain the activity of microorganism by controlling a proper concentration of sugar to minimize an osmotic change on the microorganism, thereby producing BA at a high concentration.

(41) In this Example, a bioreactor system composed of a feeding tank and a fermenter was employed. In the fermenter, fermentation started with a culture medium having a volume of 20%50% of a desired final volume while the remaining volume was fed at a rate depending on pH change from the feeding tank filled with a substrate-base mixture (a pH adjusting agent containing a carbon source substrate and a base).

(42) The culture medium of the fermenter had the following composition: 14 L of a solution of sugar cane syrup 0.8 L, organic nitrogen source CSP(Corn Steep Powder) 180 g, and FeSO.sub.4.7H.sub.2O 1.8 g in water was added with 1.5 ml of an antifoaming agent, and autoclaved to give a medium. Separately, 1 L of an aqueous solution containing 54 g of KH.sub.2PO.sub.4 was autoclaved and completely cooled. This was fed, together with the medium, into the fermenter. For a medium reservoir in the feeding tank, 19.5 L of an aqueous solution containing 7.4 L of sugar cane syrup was mixed with 2 ml of an antifoaming agent. After autoclaving, the solution was added with 2 kg of ammonium bicarbonate (NH.sub.4HCO.sub.3), introduced into the feeding tank, and stirred for 12 hrs to completely dissolve ammonium bicarbonate.

(43) A seed culture of Clostridium tyrobutyricum was inoculated in an amount of 3 L into the fermenter. Optionally, an enzyme (invertase) was added at a concentration of several ppm.

(44) Immediately after the inoculation, the pH of the culture medium was adjusted to 6.3 with ammonia water. Fermentation was carried out in the following condition: pH : 6.3, Temp.: 37 C., stiffing speed: 200 rpm.

(45) While the fermentation proceeded, a suitable amount of CSP might be additionally introduced into the fermenter. When the gas generation rate was monitored to reach 1.52.5 L/L of fermenter/hr, the feeding was stopped. Since then, the pH of the medium was adjusted with ammonia water until the fermentation was completed.

Comparative Example 2

(46) For comparison with Example 2, fermentation was performed in a batch manner The culture medium of the fermenter had the following composition: 27 L of a solution of sugar cane syrup 8 L, organic nitrogen source CSP(Corn Steep Powder) 330 g, and FeSO.sub.4.7H.sub.2O 1.6 g in water was added with 3 ml of an antifoaming agent, and autoclaved to give a medium. Separately, 1 L of an aqueous solution containing 49 g of KH.sub.2PO.sub.4 was autoclaved and completely cooled. This was fed, together with the medium, into the fermenter. After autoclaving, a seed culture of Clostridium tyrobutyricum was inoculated in an amount of 3 L into the fermenter. Optionally, an enzyme (invertase) was added at a concentration of several ppm.

(47) Immediately after the inoculation, the pH of the culture medium was adjusted to 6.3 with ammonia water. Fermentation was carried out in the following condition: pH : 6.3, Temp. : 37 C., stiffing speed: 200rpm.

(48) Fermentation results of Example 2 and Comparative Example 2 are summarized in Table 2, below. It can be understood from the data of Table 2 that the fed-batch culture according to the present invention (Example 2) greatly improved in all indices accounting for fermentation performance and BA titer, compared to the conventional batch culture (Comparative Example 2). FIG. 2 shows production profiles of the product BA and the by-product acetic acid (AA). As can be seen, a decrease in AA production was detected in the fed-batch culture, making contribution to an improvement in fermentation yield and BA productivity.

(49) TABLE-US-00002 TABLE 2 BA Titer AA Titer BA Yield BA Productivity (g/L) (g/L) (g/g sugar) (g/L/hr) Fed-batch culture 72.8 0 0.465 1.37 Batch culture 63.9 9.58 0.386 1.301

Comparative Example 3

(50) In this Comparative Example, sugar was fed in an intermittent manner, together with various bases, so as to confirm the effect of the fed-batch culture on the production of organic acids. The initial pH of the fermenter prior to the initiation of fermentation was adjusted with ammonia water to establish an environment proper for an organic acid-producing strain. After fermentation started, the base solutions listed in Table 3, below, were automatically added under monitoring with a pH probe while a solution composed solely of sugar was intermittently fed. The intermittent introduction of sugar was carried out in such a way that sugar was fed at regular time intervals or on the basis of analysis sugar data continuously measured, as shown in Table 3.

(51) Sugar cane liquid, an organic nitrogen ingredient (RCM: Reinforced Clostridial Medium), and minerals (sugar concentration 30100 g/L, 30 L) were placed in a 50 L anaerobic fermenter that was purged with nitrogen. Under this anaerobic condition, Clostridium tyrobutyricum was inoculated in a volume of 1%20% of the broth to which ammonia water was then added so as to adjust the pH to 6.0. As fermentation proceeded at 37 C., carbon dioxide (CO.sub.2) and hydrogen (H.sub.2) were generated, maintaining the anaerobic condition.

(52) Table 3 summarizes data of the final concentration, productivity, production yield and selectivity of butyric acid (BA) produced under the fermentation condition after the fermentation

(53) Fed-batch #1: A total amount of sugar required for the overall fermentation was fed in three equal aliquots when the sugar concentration measured 110 g/L. As a base, a dilution of ammonia was used in an amount shown in Table 3.

(54) Fed-batch #2: A total amount of sugar required for the overall fermentation was fed in six equal aliquots when the sugar concentration measured 20 g/L. Thus, the total concentration of sugar was maintained at 2040 g/L. As a base, a dilution of ammonia was used in an amount shown in Table 3.

(55) Fed-batch #3: A total amount of sugar required for the overall fermentation was fed in to three equal aliquots when the sugar concentration measured 110 g/L. This was the same as in #1, but the base was changed from ammonia to Ca(OH).sub.2 to examine the effect of bases change.

(56) Fed-batch #4: A total amount of sugar required for the overall fermentation was continually fed in multiple portions (10 times) to maintain a sugar concentration of 30 g/L. This was similar to the condition of #2, but the frequency of feeding was more so that the sugar concentration fluctuated to a less extent during the fermentation.

(57) TABLE-US-00003 TABLE 3 Final Medium Conc. Producti-vity Yield Selecti-vity (base) (%) (g/L .Math. hr) (g/g) (%) Note.sup.1) Fed-Batch RCM 3.5 0.36 0.32 84 Acetate #1 (ammonia: 7-7.5%, 0.67% 4.9 L) Lactate 0% Fed-Batch RCM 3.4 0.68 0.34 60 Lactate 1.3% # 2 (ammonia: 7-7.5%, Acetate 1% 4.9 L) Fed-Batch RCM 3.0 0.27 0.33 88 Acetate # 3 (Ca(OH).sub.2; 20% 2.2 L) 0.42% Lactate 0% Fed-Batch RCM 3.5 0.35 0.33 78 Acetate # 4 (ammonia: 7-7.5%, 1.01% 4.9 L) Lactate 0% .sup.1)Concentrations of different organic acids other than BA of the product (%)

(58) As shown in Table 3, there was no strategy that predominated over the other strategies in terms of productivity, production concentration, and yield. For example, fed batch #2 was observed to increase in productivity, but decrease in selectivity.

(59) In addition, the intermittent sugar feeding strategy is difficult to apply to practical processes not only because it is highly prone to failing in controlling a proper sugar concentration, but because it is labor intensive, and is likely to cause difficulty in automation and is prone to contamination due to frequent analysis.