Chemostat production of pediocin SM‐1 by Pediococcus pentosaceus Mees 1934

Production of the bacteriocin pediocin SM‐1 by Pediococcus pentosaceus Mees 1934 was investigated in pH‐controlled batch and chemostat cultures using a complex medium containing glucose, sucrose or fructose. In chemostat cultures operated at 150 rpm, 30°C, 60% dissolved oxygen tension, pH 6.5, and D = 0.148 h^?1, the pediocin titer reached 185 AU/mL representing an increase of 32% compared with batch cultures in which glucose was used as the carbon source. Pediocin biosynthesis was markedly affected by the growth rate of the producer microorganism. For all carbon sources tested, pediocin production appeared to take place only at dilution rates lower than μ_max. However, only glucose supported production at the very low dilution rate of 0.05 h^?1 indicating a direct regulation of pediocin biosynthesis by the carbon source. Glucose supported higher biomass productivity and higher pediocin titers and yields compared with the other sugars used. © 2015 American Institute of Chemical Engineers Biotechnol. Prog., 31:1481–1486, 2015     

Effect of dilution rate and methanol‐glycerol mixed feeding on heterologous Rhizopus oryzae lipase production with Pichia pastoris Mut+ phenotype in continuous culture

The induction using substrate mixtures is an operational strategy for improving the productivity of heterologous protein production with Pichia pastoris. Glycerol as a cosubstrate allows for growth at a higher specific growth rate, but also has been reported to be repressor of the expression from the AOX1 promoter. Thus, further insights about the effects of glycerol are required for designing the induction stage with mixed substrates. The production of Rhizopus oryzae lipase (ROL) was used as a model system to investigate the application of methanol‐glycerol feeding mixtures in fast metabolizing methanol phenotype. Cultures were performed in a simple chemostat system and the response surface methodology was used for the evaluation of both dilution rate and methanol‐glycerol feeding composition as experimental factors. Our results indicate that productivity and yield of ROL are strongly affected by dilution rate, with no interaction effect between the involved factors. Productivity showed the highest value around 0.04–0.06 h^?1, while ROL yield decreased along the whole dilution rate range evaluated (0.03–0.1 h^?1). Compared to production level achieved with methanol‐only feeding, the highest specific productivity was similar in mixed feeding (0.9 UA g‐biomass^?1 h^?1), but volumetric productivity was 70% higher. Kinetic analysis showed that these results are explained by the effects of dilution rate on specific methanol uptake rate, instead of a repressor effect caused by glycerol feeding. It is concluded that despite the effect of dilution rate on ROL yield, mixed feeding strategy is a proper process option to be applied to P. pastoris Mut⁺ phenotype for heterologous protein production. © 2015 American Institute of Chemical Engineers Biotechnol. Prog., 31:707–714, 2015     

Effect of oxygen supply and dilution rate on the production of 2,3-butanediol in continuous bioreactor by Klebsiella pneumoniae

Kinetics of 2,3-butanediol production by Klebsiella pneumoniae (NRRL B199) from glucose have been studied in a continuous bioreactor. The effect of oxygen supply rate and dilution rate on the product output rate and yield of 2,3-butanediol were investigated. For a feed glucose concentration of 100 g l⁻¹, the optimum oxygen transfer rate is between 25.0–35.0 mmol l⁻¹ h⁻¹. Under these conditions, maximum product concentration obtained was 35 g l⁻¹ at a dilution rate of 0.1 h⁻¹ and the maximum product output rate obtained was 4.25 g l⁻¹ h⁻¹. The product yield based on the substrate utilized approached the theoretical value (50%) at low values of oxygen transfer rate but decreased with increasing oxygen transfer rate.     

Fermentative production of superoxide dismutase with <Emphasis Type="Italic">Kluyveromyces marxianus</Emphasis>

This work sought to develop a fermentative process for the microbial production of superoxide dismutase (SOD), to overcome extraction from animal tissues. Twenty-eight wild-type yeast strains were screened for SOD productivity. Kluyveromyces marxianus L3 showed the highest SOD activity (62 U mg⁻¹) and was used for process development. Oxidative stress conditions and parameters affecting oxygen transfer rate were exploited to improve production. The effects of dilution rate (0.067 vs 0.2 h⁻¹), aeration pressure (0.3 vs 1.2 bar) and H₂O₂ (0 vs 50 mM) were studied during chemostat experiments. Low dilution rate, high pressure and H₂O₂ resulted in an increase in CuZn–SOD up to 475 U mg⁻¹. When a regulation of oxygen saturation was applied during batch cultures, CuZn–SOD was progressively higher at 60, 80 and 90% dissolved oxygen tension (DOT) (250, 330 and 630 U mg⁻¹, respectively). Furthermore, the highest growth rate and biomass yield were achieved at 90% DOT, this being therefore the best DOT condition for high overall productivity. Growth and productivity on different carbon sources were compared. Specific activity was higher on glycerol than on lactose or glucose (496, 454 and 341 U mg⁻¹, respectively). The highest biomass yield was achieved on lactose. It may be therefore the best substrate for SOD production.     

Production of l-Methionine-enriched cells of a mutant derived from a methylotrophic yeast,Candida boidinii

l-Methionine-enriched cells production of an ethionine-resistant mutant of Candida boidinii no. 2201 was greatly improved by the control of pH and by feeding of methanol and other medium components during cultivation in a jar fermentor. Under the optimal conditions, 38.5 g (as dry weight)_of cells abd 282 mg of pool methionine (intracellular pool of free l-methionine) per l of culture broth were obtained after 11 d of cultivation.The culture conditions for production of l-methionine-enriched cells in continuous culture were investigated. With limited methanol in continuous cultivation, pool methionine productivity reached a maximum value of 1.14 mg·l⁻¹·h⁻¹ at a dilution rate of 0.05·h⁻¹. During methanol-limited growth in continuous cultivation, the pool methionine content of the mutant was about 20–35% higher than that in batch cultivation.     

Continuous cultivation of the yeast Candida utilis at different dilution rates on pineapple cannery effluent

Candida utilis was grown on a pineapple cannery effluent in a chemostat at dilution rates ranging between 0.05 and 0.65 h^–1 to establish optimal conditions for biomass production and chemical oxygen demand (COD) reduction. Sucrose, fructose and glucose were the main sugars in the effluent. Maximum value for cell yield coefficient and productivity were (0.686, g_x/g_s) and (2.96, g_x/l/h) at a dilution rate of 0.425 and 0.475 h^–1, respectively, while maximum COD reduction (98%) was attained at a dilution rate of 0.1 h^–1. The maintenance coefficient attained a value of (0.093, g_s/g_x/h). An increase in dilution rate produced a higher protein content of the biomass.     

Acetone–butanol–ethanol production with high productivity using Clostridium acetobutylicum BKM19

Conventional acetone–butanol–ethanol (ABE) fermentation is severely limited by low solvent titer and productivities. Thus, this study aims at developing an improved Clostridium acetobutylicum strain possessing enhanced ABE production capability followed by process optimization for high ABE productivity. Random mutagenesis of C. acetobutylicum PJC4BK was performed by screening cells on fluoroacetate plates to isolate a mutant strain, BKM19, which exhibited the total solvent production capability 30.5% higher than the parent strain. The BKM19 produced 32.5 g L^?1 of ABE (17.6 g L^?1 butanol, 10.5 g L^?1 ethanol, and 4.4 g L^?1 acetone) from 85.2 g L^?1 glucose in batch fermentation. A high cell density continuous ABE fermentation of the BKM19 in membrane cell‐recycle bioreactor was studied and optimized for improved solvent volumetric productivity. Different dilution rates were examined to find the optimal condition giving highest butanol and ABE productivities. The maximum butanol and ABE productivities of 9.6 and 20.0 g L^?1 h^?1, respectively, could be achieved at the dilution rate of 0.85 h^?1. Further cell recycling experiments were carried out with controlled cell‐bleeding at two different bleeding rates. The maximum solvent productivities were obtained when the fermenter was operated at a dilution rate of 0.86 h^?1 with the bleeding rate of 0.04 h^?1. Under the optimal operational condition, butanol and ABE could be produced with the volumetric productivities of 10.7 and 21.1 g L^?1 h^?1, and the yields of 0.17 and 0.34 g g^?1, respectively. The obtained butanol and ABE volumetric productivities are the highest reported productivities obtained from all known‐processes. Biotechnol. Bioeng. 2013; 110: 1646–1653. © 2013 Wiley Periodicals, Inc.     

Enhanced continuous production of lovastatin using pellets and siran supported growth of Aspergillus terreus in an airlift reactor

Lovastatin, a hypocholesterolemic agent, is a secondary metabolite produced by filamentous microorganism Aspergillus terreus in submerged batch cultivation. Lovastatin production by pellets and immobilized siran cells was investigated in an airlift reactor. The process was carried out by submerged cultivation in continuous mode with the objective of increasing productivity using pellet and siran supported growth of A terreus. The continuous mode of fermentation improves the rate of lovastatin production. The effect of dilution rate and aeration rate were studied in continuous culture. The optimum dilution rate for pellet was 0.02 h⁻¹ and for siran carrier was 0.025 h⁻¹. Lovastatin productivity using immobilized siran carrier (0.0255 g/L/h) was found to be greater than pellets (0.022 g/L/h). The productivity by both modes of fermentation was found higher than that of batch process which suggests that continuous cultivation is a promising strategy for lovastatin production.     

Productivity of Chlorella sorokiniana in a short light‐path (SLP) panel photobioreactor under high irradiance

Maximal productivity of a 14 mm light‐path panel photobioreactor under high irradiance was determined. Under continuous illumination of 2,100 µmol photons m^?2 s^?1 with red light emitting diodes (LEDs) the effect of dilution rate on photobioreactor productivity was studied. The light intensity used in this work is similar to the maximal irradiance on a horizontal surface at latitudes lower than 37°. Chlorella sorokiniana, a fast‐growing green microalga, was used as a reference strain in this study. The dilution rate was varied from 0.06 to 0.26 h^?1. The maximal productivity was reached at a dilution rate of 0.24 h^?1, with a value of 7.7 g dw m^?2 h^?1 (m² of illuminated photobioreactor surface) and a volumetric productivity of 0.5 g dw L^?1 h^?1. At this dilution rate the biomass concentration inside the reactor was 2.1 g L^?1 and the photosynthetic efficiency was 1.0 g dw mol photons. This biomass yield on light energy is high but still lower than the theoretical maximal yield of 1.8 g mol photons^?1 which must be related to photosaturation and thermal dissipation of absorbed light energy. Biotechnol. Bioeng. 2009; 104: 352–359 © 2009 Wiley Periodicals, Inc.     

Optimization of dilution rate for the production of value added product and simultaneous reduction of organic load from pineapple cannery waste

Candida utiilis NRRL Y-900 was grown on pineapple cannery waste as the sole carbon and energy source in a chemostat at dilution rates ranging between 0.05 and 0.65 h⁻¹ to determine the growth kinetics. The cell yield coefficient varied with dilution rate and a maximum value of 0.662 ± 0.002 g_x/g_carb was obtained at a dilution rate of 0.4 h⁻¹. At steady state, the concentrations of carbohydrate, reducing sugar, and chemical oxygen demand (COD) appeared to follow Monod kinetics. At maximum specific growth rate (μ_max) 0.65 h⁻¹, the saturation constants for carbohydrate, reducing sugar and COD were 0.51 ± 0.02 g_carb/1, 0.046 ± 0.003 g_rs/1, and 1.036 ± 0.001 g_COD/1, respectively. Maximum biomass productivity (Q _{x max}) 2.8 ± 0.03 g_x/1 h was obtained at a dilution rate of 0.5 h⁻¹. At this dilution rate, only 71.0 ± 0.41% COD was removed whereas at a dilution rate of 0.1 h⁻¹, 98.2 ± 0.35% reduction in COD was achieved. At a dilution rate of 0.4 h⁻¹, the optimal yeast productivity and reduction in COD were 2.7 ± 0.13 g_p/1 h, and 84.2 ± 0.42%, respectively. This revised version was published online in July 2006 with corrections to the Cover Date.     

L-Sorbose production in a continuous fermenter with and without cell recycle

The kinetics of continuous l-sorbose fermentation using Acetobacter suboxydans with and without cell recycle (100%) were investigated at dilution rates (D) of 0.05, 0.10, 0.15 and 0.3 h^–1. The biomass and sorbose concentrations for continuous fermentation without recycle increased as the dilution rate was increased from 0.05 to 0.10 h^–1. A maximum biomass concentration of 8.44 g l^–1 and sorbose concentration of 176.90 g l^–1 were obtained at D=0.10 h^–1. The specific rate of sorbose production and volumetric sorbose productivity at this dilution rate were 2.09 g g^–1 h^–1 and 17.69 g l^–1 h^–1. However, on further increasing the dilution rate to 0.3 h^–1, both biomass and sorbose concentrations decreased to 2.93 and 73.20 g l^–1 respectively, mainly due to washout of the reactor contents. However, the specific rate of sorbose formation and volumetric sorbose productivity at this dilution rate increased to 7.49 g g^–1 h^–1 and 21.96 g l^–1 h^–1 respectively. Continuous fermentation with 100% cell recycle served to further enhance the concentration of biomass and sorbose to 28.27 and 184.32 g l^–1 respectively (in the reactor at a dilution rate of 0.05 h^–1). Even though, there was a decline in the biomass and sorbose concentrations to 6.8 and 83.40 g l^–1 at a dilution rate of 0.3 h^–1, the specific rates of sorbose formation and volumetric sorbose productivity increased to 3.67 g g^–1h^–1 and 25.02 g l^–1 h^–1.     

Continuous nisin production with bioengineered <Emphasis Type="Italic">Lactococcus lactis</Emphasis> strains

Nisin production in continuous cultures of bioengineered Lactococcus lactis strains that incorporate additional immunity and regulation genes was studied. Highest nisin activities were observed at 0.2 h^–1 dilution rate and 12.5 g l^–1 fructose concentration for all strains. Recombinant strains were able to produce greater amounts of nisin at dilution rates below 0.3 h⁻¹ compared to the control strain. However, this significant difference disappeared at dilution rates of 0.4 and 0.5 h^–1. For the strains LL27, LAC338, LAC339, and LAC340, optimum conditions for nisin production were determined to be at 0.29, 0.26, 0.27, and 0.27 h^–1 dilution rates and 11.95, 12.01, 11.63, and 12.50 g l^–1 fructose concentrations, respectively. The highest nisin productivity, 496 IU ml^–1 h^–1, was achieved with LAC339. The results of this study suggest that low dilution rates stabilize the high specific nisin productivity of the bioengineered strains in continuous fermentation. Moreover, response surface methodology analysis showed that regulation genes yielded high nisin productivity at wide ranges of dilution rates and fructose concentrations.     

A physiological and enzymatic study of Debaryomyces hansenii growth on xylose- and oxygen-limited chemostats

The effect of changing growth rate and oxygen transfer rate (OTR) on Debaryomyces hansenii physiology was studied using xylose-limited and oxygen-limited chemostat cultures, respectively, and complemented with enzymatic assays. Under xylose-limited chemostat (oxygen-excess), neither ethanol nor xylitol was produced over the entire range of dilution rate (D). The maximal volumetric biomass productivity was 2.5 g l^–1 h^–1 at D =0.25 h^–1 and cell yield was constant at all values of D. The respiratory rates and xylose consumption rate increased linearly with growth rate but, above 0.17 h^–1, oxygen consumption rate had a steeper increase compared to carbon dioxide production rate. Enzymatic analysis of xylose metabolism suggests that internal fluxes are redirected as a function of growth rate. For values of D up to 0.17 h^–1, the xylose reductase (XR) titre is lower than the xylitol dehydrogenase (XDH) titre, whereas above 0.17 h^–1 XR activity is about twice that of XDH and the NADPH-producing enzymes sharply increase their titres indicating an internal metabolic flux shift to meet higher NADPH metabolic requirements. Moreover, the enzymes around the pyruvate node also exhibited different patterns if D was above or below 0.17 h^–1. Under oxygen-limited chemostat (xylose-excess) the metabolism changed drastically and, due to oxidative phosphorylation limitation, cell yield decreased to 0.16 g g^–1 for an OTR of 1.4 mmol l^–1 h^–1 and xylitol became the major extracellular product along with minor amounts of glycerol. The enzymatic analysis revealed that isocitrate dehydrogenase is not regulated by oxygen, whereas XR, XDH and the NADPH-producing enzymes changed their levels according to oxygen availability. Electronic Publication     

Formation of ethanol and higher alcohols by immobilized zymomonas mobilis in continuous culture

Cells of Zymomonas mobilis ATCC 10988 were immobilized in 1.5% calcium alginate and packed in a column bioreactor for a series of fermentations utilizing 10.0% glucose media with the addition of one of the following amino acids or keto acids: L-leucine, L-isoleucine, L-valine, α-ketoisocaproic acid, α-ketobutyric acid, or α-ketoisovaleric acid. This was done in order to study the rates of production of higher alcohols during ethanolic fermentations at varying dilution rates while under the influence of amino acids or keto acids. Results indicate that the EHRLICH mechanism is operative in Zymomonas sp. α-Ketobutyrate enhanced the production of n-propanol and act-amyl alcohol. α-Ketoisocaproic acid stimulated the production of isoamyl alcohol. α-Ketoisovaleric acid increased the levels of isobutanol. The amino acids also gave rise to their corresponding alcohols but to a far lesser degree than did the keto acids. During high glucose utilization, ethanol yields ranged from 87% to 94% of theoretical with productivity ranging from 60.08 g/l/h in one fermentation (at a dilution rate of 1.35 h^?1) to 70.42 g/l/h in another (at a dilution rate of 1.58 h^?1). At dilution rates of 1.58 h^?1, higher alcohol productivity rose to as high as 4,313 mg/l/h in the presence of α-ketoisocaproic acid, 1,734.49 mg/l/h using α-ketoisovaleric acid, and 1,618.05 mg/l/h in α-ketobutyric acid. The concomitant production of ethanol and higher alcohols in all of the fermentations indicates that glucose is required for the production of the higher alcohols from their corresponding amino acids or keto acids.     

Continuous 2-keto-<Emphasis Type="SmallCaps">l</Emphasis>-gulonic acid fermentation from <Emphasis Type="SmallCaps">l</Emphasis>-sorbose by <Emphasis Type="Italic">Ketogulonigenium vulgare</Emphasis> DSM 4025

A single-stage continuous fermentation process for the production of 2-keto-l-gulonic acid (2KGA) from l-sorbose using Ketogulonigenium vulgare DSM 4025 was developed. The chemostat culture with the dilution rate that was calculated based on the relationship between the 2KGA production rate and the 2KGA concentration was feasible for production with high concentration of 2KGA. In this system, 112.2 g/L of 2KGA on the average was continuously produced from 114 g/L of l-sorbose. A steady state of the fermentation was maintained for the duration of more than 110 h. The dilution rate was kept in the range of 0.035 and 0.043 h⁻¹, and the 2KGA productivity was 3.90 to 4.80 g/L/h. The average molar conversion yield of 2KGA from l-sorbose was 91.3%. Under the optimal conditions, l-sorbose concentration was kept at 0 g/L. Meanwhile, the dissolved oxygen level was changing in response to the dilution rate and 2KGA concentration. In the dissolved oxygen (DO) range of 16% to 58%, it was revealed that the relationship between DO and D possessed high degree of positive correlation under the l-sorbose limiting condition (complete consumption of l-sorbose). Increasing D closer to the critical value for washing out point of the continuous fermentation, DO value tended to be gradually increased up to 58%. In conclusion, an efficient and reproducible continuous fermentation process for 2KGA production by K. vulgare DSM 4025 could be developed using a medium containing baker’s yeast without using a second helper microorganism.     

The influence of H2, CO2 and dilution rate on the continuous fermentation of acetone-butanol

Summary The effect of product gases, H₂ and CO₂, on solvent production was studied using a continuous culture of alginate-immobilized Clostridium acetobutylicum. Initially, in order to find the optimum dilution rate for aceton--butanol production in this system, fermentations were carried out at various dilution rates. With 10% H₂ and 10% CO₂ in the sparging gas, a dilution rate of 0.07 h^–1 was found to maximize volumetric productivity (0.58 g·l^–1·h^–1), while the maximum specific productivity of 0.27 g^–·h^–1 occured at 0.12 h^–1. Continuous cultures with vigorous sparging of N₂ produced only acids. It was concluded that in the case of continuous fermentation H₂ is essential for good solvent production, although good solvent production is possible in an H₂-absent environment in the case of batch fermentations. When the fermentation was carried out at atmospheric pressure under H₂-enriched conditions, the presence of CO₂ in the sparging gas did not slow down glucose metabolism; rather it changed the direction of the phosphoroclastic reaction and as a result increased the butanol/acetone ratio.     

The isolation and characterisation of a salicylate-hydroxylase-producing strain of Pseudomonas putida

Summary A salicylate-hydroxylase-producing strain of Pseudomonas putida with an unusual capability to grow at toxic levels of salicylate up to 10 g l^–1 has been isolated. It grew well under continuous culture conditions, with optimum growth at pH 6.5 and a temperature of 25° C. The use of an ammonium salt as a nitrogen source, instead of nitrate, resulted in a 30–40% increase in its biomass yield coefficient. Optimum growth under continuous culture conditions was achieved using 4 g l^–1 salicylate at 25° C, pH 6.5 and 0.2 h^–1 dilution rate. High salicylate hydroxylase enzyme activity [236 units (U) l^–1] and productivity (424.8 U h^–1) were obtained at a dilution rate of 0.45 h^–1 using a mineral medium containing 4 g l^–1 of salicylate. Operating under continuous culture conditions with oxygen limitation and a slight accumulation of residual salicylate (0.2 g l^–1) resulted in a decrease in culture performance and enzyme productivity. Correspondence to: R. Marchant     

2,3-Butanediol production by Enterobacter aerogenes in continuous culture: role of oxygen supply

Summary The influence of oxygen on growth and production of 2,3-butanediol and acetoin by Enterobacter aerogenes was studied in continuous culture. At all dilution rates (D) studied cell mass increased steadily with increasing oxygen uptake rate (OUR), hence the micro-aerobic cultivation was energy-limited. The biomass yield on oxygen increased with D which suggests that cells need more energy for maintenance functions at lower D. At each D an optimal OUR giving highest volumetric productivity for the sum of butanediol and acetoin was found. The optimal OUR increased with D. The occurrence of optimal OURs results from the various effects of O₂ on growth and specific productivity. The latter was found to be a linear function of the specific OUR irrespective of D. At optimal OUR the cells proved to have equal specific OURs and equal specific productivities representing a fixed relationship between fermentative and respiratory metabolism. The product yield based on glucose and corrected for biomass formation was 80%. A product concentration as high as 43 g/l was obtained at D =0.1 h^–1 while the volumetric productivity was the highest at D =0.28 h^–1 (5.6 g/l and hour). The findings further indicate that growth and product generation are obviously non-associated phenomena. Hence, high productivities may be achievable by cell recycling and cell immobilisation systems. Offprint requests to: W.-D. Deckwer     

Factors affecting l-arginine production in the continuous culture of an l-arginine producer of Corynebacterium acetoacidophilum

The effects of culture conditions on l-arginine production by continuous culture were studied using a stable l-arginine hyperproducing strain of Corynebacterium aceto-acidophilum, SC-190. Strain SC-190 demonstrated a volumetric productivity of 35 g l⁻¹·h⁻¹ at a dilution rate of 0.083h⁻¹ and feeding sugar concentration of 8%, and a product yield of 29.2% at a dilution rate 0.021h⁻¹ and feeding sugar concentration of 15%. The corresponding values for fed-batch culture are 0.85 g·l⁻¹·h⁻¹ and 26%. However, the product yield decreased with an increase in the volumetric productivity. To achieve stable l-arginine production, aeration and agitation conditions sufficient to maintain an optimal level of redox potential (>−100 mV) were necessary. The addition of phosphate to the feeding medium led to a decrease in l-arginine production. It was confirmed in the steady state that growth and l-arginine formation were inhibited by a high concentration of l-arginine.     

Continuous acetone-butanol-ethanol fermentation using SO2-ethanol-water spent liquor from spruce

SO₂–ethanol–water (SEW) spent liquor from spruce chips was successfully used for batch and continuous production of acetone, butanol and ethanol (ABE). Initially, batch experiments were performed using spent liquor to check the suitability for production of ABE. Maximum concentration of total ABE was found to be 8.79 g/l using 4-fold diluted SEW liquor supplemented with 35 g/l of glucose. The effect of dilution rate on solvent production, productivity and yield was studied in column reactor consisting of immobilized Clostridium acetobutylicum DSM 792 on wood pulp. Total solvent concentration of 12 g/l was obtained at a dilution rate of 0.21 h⁻¹. The maximum solvent productivity (4.86 g/l h) with yield of 0.27 g/g was obtained at dilution rate of 0.64 h⁻¹. Further, to increase the solvent yield, the unutilized sugars were subjected to batch fermentation.