- Original article
- Open Access
Lactic acid production by Enteroccocus faecium in liquefied sago starch
© Nolasco-Hipolito et al.; licensee Springer. 2012
- Received: 19 August 2012
- Accepted: 17 September 2012
- Published: 28 September 2012
Enterococcus faecium No. 78 (PNCM-BIOTECH 10375) isolated from puto, a type of fermented rice in the Philippines was used to produce lactic acid in repeated batch fermentation mode. Enzymatically liquefied sago starch was used as the sole carbon source, since sago (Metroxylon spp) is a sustainable crop for industrial exploitation. Liquefied sago starch was inoculated with E. faecium to perform the saccharification and fermentation processes simultaneously. Results demonstrated that E. faecium was reused for 11 fermentation cycles with an average lactic acid yield of 36.3 ± 4.71 g/l. The lactic acid production was superior to that of simple batch mode and continuous fermentation in terms of lactic acid concentration. An un-dissociated lactic acid concentration of 1.15 mM affected the productivity of the cells. Work is in progress to maintain and increase the usability of the cells over higher fermentation cycles.
- Enteroccus faecium
- Lactic acid
- Repeated batch fermentation
- Liquefied sago starch
- Cell reuse
Lactic acid is an important commodity because it is a multi-functional versatile organic acid having a wide range of applications. One of the most important factors that affect the overall production cost in Lactic Acid Fermentation (LAF) is the raw material. The consortium CSM () reported that the raw material costs for lactic acid (LA) production, as a percentage of sales, increased from 52.9% in 2009 to 53.2% in 2010. For a long time, it has been stated that lignocellulosic materials are very promising for bio-refinery applications, but this technology is still problematic (Zhou et al.). Recently Ou et al. (), reported a process using Bacillus coagullans to produce LA from non food carbohydrates, and interestingly, an indigenous Clostridium phytofermentans was found as a potential microorganism for the efficient use of lignocellulosic materials to produce ethanol, hydrogen and organic acids ([Leschine and Warnick 2010]). Among starchy materials, sago starch is being considered as an attractive raw material for food and industrial exploitation due to the fact that it is produced abundantly in the agricultural plant Metroxylon spp (Karim et al.). In 2008, Malaysia exported 37,365.3 metric tons of sago flour, thereby earning RM44, 091.0 million (Malaysia Dept[Statistics 2011]). The sago palm efficiently fixes carbon dioxide to synthesize starch in large quantities in its trunk. Sago starch granules are generally bigger than those of rice, (3–10 μm), corn (5–20 μm), wheat (22–36 μm), or cassava (5–25 μm), but smaller than those of potato (15–85 μm) (Nor-[Nadiha 2010]). Sago starch contains approximately 74-80% of amylopectine and 24-31% of amylose (Karim et al.) and has a crystalline structure (Yetti et al.). These properties of sago starch make difficult its hydrolysis. Uthumporn et al. () reported that the relative order in the hydrolysis of the starchy materials studied was as follows: corn starch > mung bean starch > cassava starch > sago starch. These findings demonstrated that sago is a difficult substrate for raw starch degrading enzymes (Yetti et al.). On the other hand, an improvement in the industrial production and efficiency of enzymes has decreased their cost in the market (Novozymes and BBI[International 2005]). Nevertheless, to improve the economics of LAF, the use of microorganisms with amylolytic activity could be preferred because it saves in terms of enzymes and energy in the liquefaction/saccharification process. Some strains of fungi and bacteria capable of producing LA directly from starchy materials by using different strategies have been reported in the literature (Lu et al.;[Petrova and Petrov 2012]; Shibata et al.; Xiao et al.). For instance, the amylolytic bacterium L. amylovorus NRRL B4542 is reported to be capable of fully converting liquefied corn starch to LA, with a productivity of 25 g/lh in continuous culture through the use of a yeast extract concentration as high as 30 g/l as nitrogen source ([Zhang and Cheryan 1994]). On the other hand, Shibata et al. () reported the use of Enteroccus faecium 78 as a promising microorganism to produce L-(+)-LA directly from raw sago starch (RSS) in continuous culture by using a hollow fibre cartridge to recycle the cells. It was reported that E. faecium 78 performed well at 30°C and pH 6.5 with a productivity of 3.04 g/lh at a LA concentration as low as 16.6 g/l (Shibata et al.). In their research the fermentation mode was of capital importance to enhance the productivity of the system. In this regard the repeated batch fermentation (RBF) process combines the advantage of batch and fed-batch fermentation processes mainly making possible to conduct the process by long periods and improving the productivity compared to batch process (Treichel et al.). RBF reduces the cost of fermentation process and enhance the productivity through the use of high cell density (Yamakawa et al.). Moreover, from an industrial point of view by using the RBF mode the production period can be shortened, compared to standard fed-batch or batch processes resulting in a significant increase of the final product yield (Russ et al.). Therefore, in this study we used the RBF for LA production with the strain E. faecium 78 (PNCM-BIOTECH 10375) in liquefied sago starch (LSS) as the only carbon source. In general, the main objective was to improve the productivity of the system, which includes the use of LSS, recycling of the yeast to speed-up the fermentation process.
Sago starch hydrolysis
Industrial grade sago starch was obtained from Nitsei Sago Industries, Kampung Teh, Mukah, Sarawak. The hydrolysis of sago starch has been reported elsewhere (Carvajal et al.). Briefly and just for the LSS, 400 g of sago starch (dry basis) were suspended in tap water and the final volume was adjusted to 1 litre. The pH of the suspension was adjusted to 4.5. A thermostable α-amylase (1,4-α-D-glucan glucanohydrolase) (EC 18.104.22.168). from Bacillus licheniformis, 240 KNU-S/g of starch, (10 μl, 3000 U/ml) (Novozyme Co.) was added to liquefy the starch at 95-100°C for 2 hours. This LSS was cooled and further treated with 0.5 μl (0.23 amyloglucosidase units AGU) of enzyme dextrozyme DX (Novozyme, Co) at pH 6.5, heated at 60°C, for 24 h and agitated at 300 rpm to produce the hydrolysed sago starch (HSS). The gelatinised sago starch (GSS) was prepared by heating at 65°C a slurry of raw sago starch at concentration of 20 g/l and agitated at 300 rpm. The raw sago starch (RSS) used as substrate was prepared just by suspending 20 g of sago starch in 1 l of tap water. Previously the sago starch was dried at 105°C for 1 hour.
Enterococcus faecium No. 78 (PNCM-BIOTECH 10375) was used throughout this study. Stock cultures were maintained in PDA media at −84°C. One vial containing the frozen strain was thawed and used to inoculate 10 ml broth containing 20 g/l LSS and 5 g/l of yeast extract (YE), and the broth was incubated for 24 h at 36°C in static conditions.
The media for LA production was prepared with LSS and supplemented with YE at a concentration of 5 g/l (Difco, USA). The YE was dissolved in 100 ml of water and sterilized separately at 121°C, for 15 min and added to the hot LSS sterilized at 121°C for 15 min.
Dry cell weight
The dry cell weight (DCW) was determined by a pre-established calibration curve of optical density (OD) against DCW. To determine DCW, samples of 200 ml of fermented broth at different OD were centrifuged at 10000 rpm for 10 min. The harvested cells were washed with 0.2 M hydrochloride acid and centrifuged again under the same conditions. This procedure was applied three times. The harvested cells were dried at 60°C for three days, then the weight was registered and the OD plotted against the DCW. It was determined that one OD unit was equivalent to 6.4 g/l DCW.
The fermentations were carried out in a 3 litre Jar fermenter fully controlled by a computer system. Parameters such as temperature, pH, agitation, cell concentration, and sodium hydroxide consumption were monitored on-line in real time. The OD was monitored by a laser sensor, model LA 300-LT (Automatic Research System, Tokyo, Japan) at 780 nm. The temperature was controlled at 30°C and the pH was controlled at 6.5 (Shibata et al.). The agitation was controlled at 200 rpm. The media used contained LSS at 20 g/l and 5 g/l of YE. The pH was controlled with 10 M sodium hydroxide.
Repeated batch fermentation
The medium containing LSS at a level of 20 g/l was maintained until the fourth fermentation cycle. Then, it was increased to 40, 60, 80, and 100 g/l for the subsequent fermentation cycles. The operating conditions were: temperature 30°C, agitation 150 rpm, and pH controlled at 6.5 by direct titration with 10 M NaOH. The YE was maintained at a level of 5 g/l in all the fermentation cycles. The cells were harvested by centrifugation at 8,000 rpm for 10 min. The process of harvesting and re-suspending the cells was repeated for the subsequent cycles to perform the RBF mode.
Glucose and lactate were determined by an HPLC (LC-10 AD, RID-6A Refractive Index Detector, Shimadzu, Kyoto, Japan) using an Aminex HPX-87 H column (Biorad, CA., USA) at 50°C, with 0.6 ml/min flow rate of 5 mM H2SO4 as a mobile phase. Total organic acid was measured by direct titration in the fermenter through the addition of 10 M NaOH with a density of 1.3 g/l. The weight of NaOH used to neutralize the LA was recorded on-line in real time by a software in a computer and reported as LA by using the factor 0.69.
Scanning electron microscopy
Air-dried sago powder was scattered on the specimen stub, then coated with OsO4 and platinum to strengthen the contrast for observation. The specimens were observed with a scanning electron microscope (JSM6360A, JEOL, Tokyo).
Data from two replicate experiments and three repetitions of the analysis for each sample were expressed as the mean ± standard deviation (± SD). All analyses were conducted with PASW 18.0 software.
Effect of sago starch in different forms on biomass production
Effect on biomass production
Lactic acid production in repeated batch fermentation
Overall productivity of the repeated batch fermentation process in two stages during eleven cycles for the production of lactic acid in liquefied sago starch by E. faecium
Cycle (6–11 )
LA concentration (g/l)
19.2 ± 8.5
Volumetric productivity (g/lh)
1.28 ± 0.24
Specific Productivity ()
9.86 ± 0.35
11.45 ± 1.13
0.47 ± 0.021
0.57 ± 0.14
4.8 ± 4.01
3.17 ± 1.86
Dry Cell weight (g/l)
1.95 ± 0.54
3.17 ± 0.19
Overall productivity of the repeated batch fermentation after eleven cycles for the production of lactic acid in liquefied sago starch by E. faecium
Working volume (l)
Total fermentation time (h)
Total Starch used dry basis(g)
Total NaOH used in the titration of LA (g)
Total Lactic acid produced (g)
Final Dry Cell weight (g/l)
Volumetric productivity (g/lh)
Figure6 shows that E. faecium can keep the trend of LA production and that longer fermentation time did not improve the productivity of LA in terms of volumetric productivity. The cells were growing in each subsequent fermentation cycle until the sixth cycle and then the trend was asymptotic. At the end of the sixth cycle, the cells (3.9 g/l) were recovered and almost 33% of the pellet was not recycled with the aim to stimulate the cell growth having more availability of nitrogen source. Therefore, a decrease in the cell population was observed at the beginning of the seventh cycle up to 2.6 g/l. However, E. faecium very soon recovered its ability to grow again, and in a shorter time the same concentration as in the sixth cycle was reached again by the eighth cycle. Thereafter, the cells maintained the same level of low but active growth to produce LA. In this fermentation and in the previous one, the substrate consumption is indirectly measured as the production of lactic acid. The releasing of fermentable sugars, in this case, mainly glucose, immediately was consumed by the microorganism. The substrate was not the same since it was continuously changing due to the enzymatic hydrolysis performed by the amyloglucosidase in the fermentation media. Therefore, the glucose consumption rate was a function of the lactic production rate.
It was thought that glucose and hydrolysed sago starch (HSS) could promote the growth of the cells better than raw sago starch (RSS) and gelatinized sago starch (GSS). However, the trends obtained in all cases were similar, although it was observed that in the log phase the uptake of the GSS and RSS forms was slightly faster than that of the glucose and HSS. Similar observation was reported by Shibata et al. (). They found that the performance of E. faecium using RSS was better than with corn, potato and wheat starches. It could be desirable to have RSS as the most appropriate form of starch to be used as direct substrate for the fermentation process; however, it is problematic to manage the RSS slurry at high concentration. Although Shibata et al. () did not reported how they prepared the raw sago starch, and if they sterilized the sago slurry, then; the form of starch used perhaps was the gelatinised sago starch. The gelatinised sago starch can be used as substrate but a very low concentration because when the concentration of starch is increased the viscosity of the media is very high. The viscosity of the slurry increases proportionally with the concentration of the starch. In general, when the starch concentration increased, sedimentation occurred due to saturation or insolubility. This situation was visualized by[Zhang and Cheryan (1994]); therefore, these researchers used liquefied starch to avoid these problems and they improved the process by using the amylolytic Lactobacillus amylovorus strain. Shibata et al. used E. faecium No. 78 cultivated in RSS at a concentration no higher than 20 g/l, which is very low for an industrial application. Therefore, it could be reasoned that using batch and its extension RBF might be advantageous to produce higher LA concentration at a similar production rate.
The RBF mode was applied with the aim to reuse the cells in order to improve the overall productivity of the fermentation. One of the key points in fermentation technology is to maintain the cells in a stable and perpetual state of productivity and to avoid damage to the cells, the aim being to increase their reusability for longer periods. This pattern is well observed in ethanol fermentation where the yeast can be reused 400–600 times, but only if the concentration of ethanol is 7-10%. As reported by Amorim et al. () higher ethanol concentration affects the viability of the cells and their reusability falls notably. Similarly, longer exposition of E faecium to a high concentration of LA resulted in lowered productivity. This fact was observed as the behaviour of the specific growth rate, which was affected by the LA. In Figure4 it was observed that the maximum specific growth (μmax) was found at a low concentration of starch and higher availability of a nitrogen source; for instance, in the first cycle to synthesize the necessary proteins for the metabolism of E. faecium; especially, the synthesis of amylases to produce glucose for growth was observed as biomass production. In addition, due to the low concentration of glucose the effect of osmotic stress was avoided, which could help in the productivity of the cells. In subsequent cycles, the growth rate decreased, and contrary to the first cycle, less availability of nitrogen source for a higher population of microorganisms decelerated the growth. Although the nitrogen source could affect the growing of the cells the general trend was a slow growing rate and maintained LA productivity.
On the other hand, as other studies have found, there is an optimum concentration of starch around 20–60 g/l, where the fermentation can go faster but is not limited by this concentration (Narita et al.; Naveena et al.; Okano et al.;[Petrova and Petrov 2012]; Yun et al.). It is true that a higher concentration of starch to produce higher LA titter is possible, but the time process will also increase proportionately. To produce the highest concentration of 42.5 g/l of LA using E faecium and LSS it took 30 h, approximately (Figure5). Using raw starch, ([Petrova and Petrov 2012]) reported the highest amount of LA (37.3 g/l) from 40 g/l of raw starch during 48 h of fermentation using Lactobacillus paracasei B41. In our study it was observed that this concentration of LA has a strong effect on the growth of E. faecium, because after this concentration the production of LA was very limited. After the said concentration, the productivity decreased and the fermentations stopped with an asymptotic trend. Although using LSS form had some advantages because the effect of osmotic stress that could impair the cells as a result of glucose being used directly was avoided, the productivity production of LA was only around 36.3 g/l (Table1). The fact that E. faecium has a faster glucose uptake compared with other microorganisms, especially those having amylolytic abilities such L amylovorus, L. manihotivorans (Shibata et al.), could be valid only at a low starch concentration (less than 20 g/l).
On the other hand, if it is possible to increase the biomass by increasing the nitrogen source to improve the productivity; then it is possible to reduce the fermentation time and increase the LSS concentration. Here, the key point is to decrease the exposure time of the cells to LA. This same situation applies also for ethanol fermentation (Amorim et al.); when ethanol concentration increases, the yeast starts to lose activity due to a high percentage of the active biomass dying. Then, the numbers of cycles to reuse the cells becomes reduced and the overall productivity of the system fails. Shibata et al. (). only used a concentration of no more than 20 g/l and the dilution rate was low, because increasing the dilution rate is probably a way to wash out the amylolytic enzymes produced by E. faecium, although there are reports that amylase enzymes could bind to the cell membrane ([Walker 1965]; Anderson et al.). Then, the system becomes inefficient at a high dilution rate and a high concentration of sago starch and, even worse, because of the clogging of the membrane system at a high concentration of suspended solids ([Zhang and Cheryan 1994]).
The characteristics of sago starch can be overcome with the use of Termamyl® SC to liquefy the sago starch with the aim of facilitating the subsequent attack of the amylase produced by E. faecium. The enzyme termamyl can only produce oligosaccharides and not glucose. In doing so and taking into account that the liquefaction process takes less than 2 h, and that the actual cost of Termamyl® SC is reasonably cheap, it can be used for this purpose.
For instance, the cost of Termamyl is around US$ 6715.60/ton and the dose of enzymes per ton of starch is around 0.625 kg, which means $4.20 US/ton of starch (Alagaratnum 2011, personal communication). Through a simple calculation and taking into account the price forecasted by Energetics[Incorporated (2003]) of about 550.0-1100.0 $US/ton, and an efficiency of 90% of conversion from starch to LA, as the percentage of the enzyme cost in the total cost of LA production could be considered as low (0.60%). Yet, this percentage in the total cost could be even lower if we consider the higher price for the LA food grade produced by Purac.
where [L-] is the dissociated and the non-dissociated LA, the fermentation was controlled at pH 6.5, and the concentration of non-dissociated LA that produced the growth inhibition of E. faecium was calculated at approximately 1.15 mM. This critical concentration of LA which affects the growth of E. faecium was lower compared to those reported for Lactobacillus rhamnosus (4.7 mM) and Lactobacillus helveticus (5 mM) (Gonçalves et al.;[Timmer and Kromkamp 1994]). Therefore, it is suggested that E. faecium lowered the rate of LA production when it starts to reach a concentration close to 45 g/l and then modified its metabolism to synthesize exo-polysaccharide. E. faecium was able to grow at a rate as high as 0.4 h-1 in the first fermentation cycle. In the second cycle μ decreased to 0.27, then to 0.11, and from the fourth to eleventh cycle μ was almost constant at level of 0.028-0-0.02 h-1 (Figure4). Even at low growth rate the strain maintained its LA production rate at a level of 1 g/lh.
In conclusion, Enterococcus faecium No. 78 (PNCM-BIOTECH 10375) isolated from puto, a type of fermented rice in the Philippines, was able to produce LA in RBF mode. The cells retained their metabolic activity during 566 h of fermentation. However, the growth of this strain was affected strongly by non-dissociated LA at a concentration of around 1.15 mM, by lowering the productivity of the system.
This work was financially supported by the Ministry of Science, Technology and Innovation of Malaysia (grant MOSTI(S)180.010.R 053/004-59).
- Amorim HV, Lopes ML, De Castro Oliveira JV, Buckeridge MS, Goldman GH: Scientific challenges of bioethanol production in Brazil. Appl Microbiol Biotechnol 2011, 91: 1267–1275. 10.1007/s00253-011-3437-6View ArticlePubMedGoogle Scholar
- Anderson KL, Salyers AA: Biochemical evidence that starch breakdown by bacteroides thetaiotaomicron involves outer membrane starch-binding sites and periplasmic starch-degrading enzymes. J Bacteriol 1989, 171: 3192–3198.PubMed CentralPubMedGoogle Scholar
- Carvajal-Zarrabal O, Nolasco-Hipólito C, Bujang KB, Ishizaki A: Production of nisin Z using Lactococcus lactis IO-1 from hydrolyzed sago starch. J Ind Microbiol Biotechnol 2009, 36: 409–415. 10.1007/s10295-008-0511-xView ArticlePubMedGoogle Scholar
- CSM Annual Report: CSM Annual Report. CSM Annual Report: CSM Annual Report; 2010:38. . Accessed 17 Sept 2012 http://www.csmannualreport2010.com/Google Scholar
- Energetics Incorporated: Industrial Bioproducts: Today and tomorrow. U.S. Department of Energy, Office of Energy Efficiency and Renewable Energy. Washington, D.C: Office of the Biomass Program; 2003.Google Scholar
- Gonçalves LMD, Ramos A, Almeida JS, Xavier AMRB, Carrondo MJT: Elucidation of the mechanism of lactic acid growth inhibition and production in batch cultures of Lactobacillus rhamnosus. Appl Microbiol Biotechnol 1997, 48: 346–350. 10.1007/s002530051060View ArticleGoogle Scholar
- Karim AA, Tie AP, Manan DMA, Zaidul ISM: Starch from the sago (Metroxylon sagu) palm tree properties, prospects, and challenges as a new industrial source for food and other uses. Com Rev Food Sci Food Safety 2008, 7: 215–228. 10.1111/j.1541-4337.2008.00042.xView ArticleGoogle Scholar
- Leschine S, Warnick TA: Systems and methods for producing biofuels and related materials. US Patent 7,682, 811 B2. 2010.Google Scholar
- Lu Z, Lu M, He F, Yu L: An economical approach for D-lactic acid production utilizing unpolished rice from aging paddy as major nutrient source. Biores Technol 2009, 100: 2026–2031. 10.1016/j.biortech.2008.10.015View ArticleGoogle Scholar
- Malaysia Department of Statistics: Sarawak export of sago starch, SITC Code: 592–150–100. 2011.Google Scholar
- Narita J, Nakahara S, Fukuda H, Kondo A: Efficient production of L-(+)-Lactic acid from raw starch by Streptococcus bovis 148. J Biosci Bioeng 2004, 97: 423–425. 10.1263/jbb.97.423View ArticlePubMedGoogle Scholar
- Naveena BJ, Altaf M, Bhadrayya K, Madhavendra SS, Reddy G: Direct fermentation of starch to L(+) lactic acid in SSF by Lactobacillus amylophilus GV6 using wheat bran as support and substrate: Medium optimization using RSM. Proc Biochem 2005, 40: 681–690. 10.1016/j.procbio.2004.01.045View ArticleGoogle Scholar
- Nitta Y, Matsuda T, Mizuma S, Yamamoto Y, Yoshida T, Miyazaki A, et al.: Starch accumulation in sago palm stems. In Sago: Its potential in food and industry. Edited by: Toyoda Y. Tokyo: TUAT Press; 2008:23–28.Google Scholar
- Nor Nadiha MZ, Fazilah A, Bhat R, Karim AA: Comparative susceptibilities of sago, potato and corn starches to alkali treatment. Food Chem 2010, 121: 1053–1059. 10.1016/j.foodchem.2010.01.048View ArticleGoogle Scholar
- Novozymes and BBI International: Fuel ethanol: A technological evolution. Novozymes and BBI, Colorado, USA; 2005. . Accessed 18 Sept 2012 http://www.energiasrenovables.ciemat.es/adjuntos_documentos/FuelEthanol-lr-05.pdfGoogle Scholar
- Okano K, Zhang Q, Shinkawa S, Yoshida S, Tanaka T, Fukuda H, Kondo A: Efficient production of optically pure D-lactic acid from raw corn starch by using a genetically modified L-lactate dehydrogenase gene-deficient and α-amylase-secreting Lactobacillus plantarum strain. Appl Environ Microbiol 2009, 75: 462–467. 10.1128/AEM.01514-08PubMed CentralView ArticlePubMedGoogle Scholar
- Ou MS, Ingram LO, Shanmugam KT: L(+)-Lactic acid production from non-food carbohydrates by thermotolerant Bacillus coagulans. J Ind Microbiol Biotechnol 2011, 38: 599–605. 10.1007/s10295-010-0796-4View ArticlePubMedGoogle Scholar
- Petrova P, Petrov K: Direct starch conversion into L-(+)-lactic acid by a novel amylolytic strain of Lactobacillus paracasei B41. Starch/Staerke 2012, 64: 10–17. 10.1002/star.201100074View ArticleGoogle Scholar
- Russ K, Schlenke P, Huchler H, Hofer H, Kuchenbecker M, Fehrenbach R: Repeated batch fermentation using a viafuge centrifuge. Cell Technol Cells Prod 2007, 10: 523–526. 10.1007/978-1-4020-5476-1_88View ArticleGoogle Scholar
- Shibata K, Flores DM, Kobayashi G, Sonomoto K: Direct L-lactic acid fermentation with sago starch by a novel amylolytic lactic acid bacterium, Enterococcus faecium. Enz Microb Technol 2007, 41: 149–155. 10.1016/j.enzmictec.2006.12.020View ArticleGoogle Scholar
- Timmer JMK, Kromkamp J: Efficiency of lactic acid production by Lactobacillus helveticus in a membrane cell recycle reactor. FEMS Microbiol Rev 1994, 14: 29–38. 10.1111/j.1574-6976.1994.tb00069.xView ArticleGoogle Scholar
- Treichel H, Oliveira D, Mazutti MA, Luccio MD, Oliveira JV: A review on microbial lipases production. Food Bioproc Technol 2010, 3: 182–196. 10.1007/s11947-009-0202-2View ArticleGoogle Scholar
- Uthumporn U, Zaidul ISM, Karim AA: Hydrolysis of granular starch at sub-gelatinization temperature using a mixture of amylolytic enzymes. Food Bioprod Process 2010, 88: 47–54. 10.1016/j.fbp. 2009.10.001View ArticleGoogle Scholar
- Walker GJ: The Cell-Bound α-Amylases of Streptococcuts bovis. Biochem J 1965, 94: 289–298.PubMed CentralView ArticlePubMedGoogle Scholar
- Xiao Z, Wu M, Beauchemin M, Groleau D, Lau PCK: Direct fermentation of triticale starch to lactic acid by Rhizopus oryzae. Ind Biotechnol 2011, 7: 129–135. 10.1089/ind.2011.7.129View ArticleGoogle Scholar
- Yamakawa S, Yamada R, Tanaka T, Ogino C, Kondo A: Repeated batch fermentation from raw starch using a maltose transporter and amylase expressing diploid yeast strain. Applied Microbiol Biotechnol 2010, 87: 109–115. 10.1007/s00253-010-2487-5View ArticleGoogle Scholar
- Yetti M, Nazamid BS, Roselina K, Abdulkarim SM: Improvement of glucose production by raw starch degrading enzyme utilizing acid-treated sago starch as substrate. ASEAN Food 2007, J14: 83–90.Google Scholar
- Yun J-A, Wee Y-W, Kim J-N, Ryu H-W: Fermentative production of DL-lactic acid from amylase-treated rice and wheat brans hydrolyzate by a novel lactic acid bacterium, lactobacillus sp. Biotechnol Lett 2004, 26: 1613–1616. 10.1023/B:BILE.0000045826.97010.82View ArticlePubMedGoogle Scholar
- Zhang DX, Cheryan M: Starch to lactic acid in a continuous membrane bioreactor. Process Biochem 1994, 29: 145–150. 10.1016/0032-9592(94)80008-1View ArticleGoogle Scholar
- Zhou C-H, Xia X, Lin C-X, Tong D-S, Beltramini J: Catalytic conversion of lignocellulosic biomass to fine chemicals and fuels. Chem Soc Rev 2011, 40: 5588–5617. 10.1039/C1CS15124JView ArticlePubMedGoogle Scholar
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