Factors affecting the growth and the oil accumulation of marine microalgae, Tetraselmis suecica

Biomass production and oil productivity in microalgae culture are the most important key factors for algal biodiesel production. However, proper culture condition for the biomass production of microalgae is different from that for the oil production of microalgae. A study on the biomass production of Tetraselmis suecica using various light intensities and nitrate concentrations as growth factors was carried out to evaluate proper culture conditions in 20-L batch culture. The effect of nitrate depletion on the oil accumulation was also evaluated with two-stage culture. It took 5 days to reach the stationary phase for the cultures of T. suecica on the light intensities of 108.9 and 133.1 μmol m(-2 )s(-1) with biomass of 0.89 and 0.88 g dcw L(-1), respectively. Biomass productions of 1.07 and 1.00 g dcw L(-1) were obtained with the nitrate concentrations of 18.6 and 24.7 mg L(-1), respectively. The two-stage culture increased oil contents from 7.6 to 17.3% (w/w) and contents of C(16)-C(18) fatty acids from 540.2 to 720.5 mg g(-1) oil. The predominant fatty acid was palmitic acid (C(16:0)) in nitrate depletion group, however, oleic acid (C(18:1)) was predominated in nitrate added groups. The two-stage culture enhanced overall oil productivity of 18.7 mg g(-1) day(-1) which is higher than that of 12.2 mg g(-1) day(-1) in single-stage culture.     

Statistical optimization of culture media for growth and lipid production of <Emphasis Type="Italic">Botryococcus braunii</Emphasis> LB572

Botryococcus braunii has an outstanding ability to produce lipid; however, it is a slow-growing green microalgae. Statistical optimization of growth media was performed to faster growth and to increase lipid concentration. The effect of media composition on the growth of B. braunii LB572 was examined using fractional factorial design and central composite design. The media components examined include sodium carbonate, potassium phosphate, calcium chloride, magnesium sulfate, ferric citrate, and sodium nitrate. The results indicated that potassium phosphate and magnesium sulfate were major impact factors. The optimum concentrations of potassium phosphate and magnesium sulphate were found to be 0.058 and 0.09 g/L, respectively, for growth and 0.083 and 0.1 g/L, respectively, for lipid production. These values were validated using bubble column photobioreactors. Lipid productivity increased to 0.19 g/L/day in lipid-optimized media, with an average biomass productivity of 0.296 g/L/day and 64.96% w/w. In growth-optimized media, lipid productivity was 0.18 g/L/day, with an average biomass productivity of 0.304 g/L/day and 59.56% w/w.     

Optimization of carbohydrate fatty acid ester synthesis in organic media by a lipase from Candida antarctica

The effect of solvents and solvent mixtures on the synthesis of myristic acid esters of different carbohydrates with an immobilized lipase from C. antarctica was investigated. The rate of myristyl glucose synthesized by the enzyme was increased from 3.7 to 20.2 micromol min(-1) g(-1) by changing the solvent from pure tert-butanol to a mixture of tert-butanol:pyridine (55:45 v/v), by increasing the temperature from 45 degrees C to 60 degrees C, and by optimizing the relative amounts of glucose, myristic acid, and the enzyme preparation. Addition of more than 2% DMSO to the tert-butanol:pyridine system resulted in a reduction of enzyme activity. Lowering the water content of the enzyme preparation below 0.85% (w/w) resulted in significant decreases in enzyme activity, while increasing the water content up to 2.17% (w/w) did not significantly affect the enzyme activity. The highest yields of myristyl glucose were obtained when an excess of unsolubilized glucose was present in the reaction system. In this case, all of the initially solubilized and a significant amount of the initially unsolubilized glucose was converted to the ester within 24 h of incubation, resulting in a myristyl glucose concentration of 34 mg/mL(-1). Myristic acid esters of fructose (22.3 micromol min(-1) g(-1)), alpha-D-methyl-glucopyranoside (26.9 micromol min(-1) g(-1)) and maltose (1.9 micromol min(-1) g(-1)) could also be prepared using the tert-butanol:pyridine solvent system. No synthesis activity was observed with maltotriose, cellobiose, sucrose, and lactose as substrate.     

Synthesis of galacto-oligosaccharides by β-galactosidase from Aspergillus oryzae using partially dissolved and supersaturated solution of lactose

The effect of enzyme to substrate ratio, initial lactose concentration and temperature has been studied for the kinetically controlled reaction of lactose transgalactosylation with Aspergillus oryzae β-galactosidase, to produce prebiotic galacto-oligosaccharides (GOS). Enzyme to substrate ratio had no significant effect on maximum yield and specific productivity. Galacto-oligosaccharide syntheses at very high lactose concentrations (40, 50 and 60%, w/w, lactose monohydrate) were evaluated at different temperatures (40, 47.5 and 55°C). Within these ranges, lactose could be found as a supersaturated solution or a heterogeneous system with precipitated lactose, resulting in significant effect on GOS synthesis. An increase in initial lactose concentration produced a slight increase in maximum yield as long as lactose remained dissolved. Increase in temperature produced a slight decrease in maximum yield and an increase in specific productivity when supersaturation of lactose occurred during reaction. Highest yield of 29 g GOS/100 g lactose added was obtained at a lactose monohydrate initial concentration of 50% (w/w) and 47.5°C. Highest specific productivity of 0.38 g GOSh(-1) mg enzyme(-1) was obtained at lactose monohydrate initial concentration of 40% (w/w) and 55°C, where a maximum yield of 27 g GOS/100 g lactose added was reached. This reflects the complex interplay between temperature and initial lactose concentration on the reaction of synthesis. When lactose precipitation occurred, values of yields and specific productivities lower than 22 g GOS/100 g lactose added and 0.03 gGOSh(-1) mg enzyme(-1) were obtained, respectively.     

Production of 8,11‐dihydroxy and 8‐hydroxy unsaturated fatty acids from unsaturated fatty acids by recombinant Escherichia coli expressing 8,11‐linoleate diol synthase from Penicillium chrysogenum

Hydroxy unsaturated fatty acids can be used as antimicrobial surfactants. 8,11‐Linoleate diol synthase (8,11‐LDS) catalyzes the conversion of unsaturated fatty acid to 8‐hydroperoxy unsaturated fatty acid, and it is subsequently isomerized to 8,11‐dihydroxy unsaturated fatty acid by the enzyme. The optimal reaction conditions of recombinant Escherichia coli expressing Penicillium chrysogenum 8,11‐LDS for the production of 8,11‐dihydroxy‐9,12(Z,Z)‐octadecadienoic acid (8,11‐DiHODE), 8,11‐dihydroxy‐9,12,15(Z,Z,Z)‐octadecatrienoic acid (8,11‐DiHOTrE), 8‐hydroxy‐9(Z)‐hexadecenoic acid (8‐HHME), and 8‐hydroxy‐9(Z)‐octadecenoic acid (8‐HOME) were pH 7.0, 25°C, 10 g/L linoleic acid, and 20 g/L cells; pH 6.0, 25°C, 6 g/L α‐linolenic acid, and 60 g/L cells; pH 7.0, 25°C, 8 g/L palmitoleic acid, and 25 g/L cells; and pH 8.5, 30°C, 6 g/L oleic acid, and 25 g/L cells, respectively. Under these optimized conditions, the recombinant cells produced 6.0 g/L 8,11‐DiHODE for 60 min, with a conversion of 60% (w/w) and a productivity of 6.0 g/L/h; 4.3 g/L 8,11‐DiHOTrE for 60 min, with a conversion of 72% (w/w) and a productivity of 4.3 g/L/h; 4.3 g/L 8‐HHME acid for 60 min, with a conversion of 54% (w/w) and a productivity of 4.3 g/L/h; and 0.9 g/L 8‐HOME for 30 min, with a conversion of 15% (w/w) and a productivity of 1.8 g/L/h. To best of our knowledge, this is the first report on the biotechnological production of 8,11‐DiHODE, 8,11‐DiHOTrE, 8‐HHME, and 8‐HOME. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:390–396, 2017     

Experimental optimization of fed-batch culture for poly-beta-hydroxybutyric acid production

The optimal feed rate profiles of glucose and ammonium hydroxide were calculated using a proposed model, and implemented for the production of poly-beta-hydroxybutyric acid (PHB) by Alcaligenes eutrophus. By implementing these optimal feed rates with a high glucose feed concentration of 700 g/L and an ammonium hydroxide concentration of 7%(w/w), it was possible to achieve a high final cell concentration of 141 g/L and a high PHB concentration of 105 g/L in 40 h of fed-batch operation. The PHB productivity was as high as 2.63 g/(L hr). (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 56: 697-705, 1997.     

Enzymatic synthesis of isoamyl acetate using immobilized lipase from Rhizomucor miehei

The effects of important reaction parameters for enhancing isoamyl acetate formation through lipase-catalyzed esterification of isoamyl alcohol were investigated in this study. Increase in substrate (acid) concentration led to decrease in conversions. A critical enzyme concentration of 3 g l(-1) was detected for a substrate concentration of 0.06 M (each of alcohol and acid). Solvents with partition coefficient higher than 1000 (log P>3.0) supported enzyme activity to give high conversions. Acetic acid at higher concentrations could not be esterified easily probably owing to its role in lowering the microaqueous pH of the enzyme. Extraneous water/buffer addition decreased the isoamyl acetate yields slightly ( approximately 10%) at 0.005-0.01% v/v of the reaction mixture and drastically (>40%) at above 0.01% v/v. Buffer saturation of the organic solvent employed improved esterification (upto two-fold), particularly at moderately higher substrate concentrations (>0.18 M). Employing acetic anhydride instead of acetic acid resulted in a two-fold increase in the yields (at 0.25 M substrate). Use of excess nucleophile (alcohol) concentration by increasing the alcohol/acid molar ratio resulted in higher conversions in shorter duration (upto eight-fold even at 1.5 M acetic acid). Yields above 80% were achieved with substrate concentrations as high as 1.5 M and more than 150 g l(-1) isoamyl acetate concentrations were obtained employing a relatively low enzyme concentration of 10 g l(-1). The operational stability of lipase was also observed to be reasonably high enabling ten reuses of the biocatalyst.     

Candida krusei produces ethanol without production of succinic acid; a potential advantage for ethanol recovery by pervaporation membrane separation

The development of fermentative yeasts secreting no organic acids is highly desirable for ethanol production coupled with membrane separation processes, because the acidic byproduct, succinic acid, significantly inhibits the membrane permeation of ethanol. Of the Pichia and Candida yeasts tested, Candida krusei IA-1 showed the highest ethanol productivity [55 g L(-1) day(-1) from 150 g L(-1) (w/v) of glucose], comparable to the strains of Saccharomyces cerevisiae, and produced much less of the acid (0.6 g L(-1) day(-1)) than the Saccharomyces strains (1.5-1.8 g L(-1) day(-1)) under semi-aerobic conditions. Interestingly, under aerobic conditions, strain IA-1 showed no production of the acid. Stain IA-1 exhibited a good assimilation of the acid, while S. cerevisiae NBRC 0216 showed no assimilation. The activity of succinate dehydrogenase (SDH) in strain IA-1 was 37.5 mU mg(-1), and 7.8-fold higher than that in S. cerevisiae strain NBRC 0216. More significantly, SDH1 was abundantly transcribed in strain IA-1, different from that in strain NBRC 0216, regardless of the culture conditions. From these results, C. krusei IA-1 efficiently takes up succinic acid and metabolizes it in the Krebs cycle, producing an extremely low level of byproducts in the culture medium. Therefore, C. krusei is not only a promising alternative to S. cerevisiae but also a suitable model for metabolic engineering of S. cerevisiae.     

Production of 10-hydroxystearic acid from oleic acid by whole cells of recombinant Escherichia coli containing oleate hydratase from Stenotrophomonas maltophilia

A putative fatty acid hydratase from Stenotrophomonas maltophilia was cloned and expressed in Escherichia coli. The recombinant enzyme showed the highest hydration activity for oleic acid among the fatty acids tested, indicating that the enzyme is an oleate hydratase. The optimal conditions for the production of 10-hydroxystearic acid from oleic acid using whole cells of recombinant E. coli containing the oleate hydratase were pH 6.5, 35°C, 0.05% (w/v) Tween 40, 10 g l(-1) cells, and 50 g l(-1) oleic acid. Under these conditions, whole recombinant cells produced 49 g l(-1) 10-hydroxystearic acid for 4 h, with a conversion yield of 98% (w/w), a volumetric productivity of 12.3 g l(-1) h(-1), and a specific productivity of 1.23 g g-cells(-1) h(-1), which were 18%, 2.5-, and 2.5-fold higher than those of whole wild-type S. maltophilia cells, respectively. This is the first report of 10-hydroxystearic acid production using recombinant cells and the concentration and productivity are the highest reported thus far among cells.     

Continuous cultivation of the diatom Nitzschia laevis for eicosapentaenoic acid production: physiological study and process optimization

The continuous cultures of the diatom Nitzschia laevis were performed at different dilution rates (D) and feed glucose concentrations (S(0)) to investigate cellular physiological responses and its production potential of eicosapentaenoic acid (EPA). Steady-state cell dry weight, residual glucose concentration, cell growth yield, specific glucose consumption rate, and fatty acid profiles were investigated within the range of D from 0.1 to 1.0 day(-1) (S(0) fixed at 20 g/L) and the range of S(0) from 5 to 35 g/L (D fixed at 0.3 day(-1)), respectively. The highest EPA productivity of 73 mg L(-1) day(-1) was obtained at D = 0.5 day(-1) and S(0) = 20 g/L. However, when the continuous culture achieved high productivities of EPA at certain dilution rates and feed glucose concentrations, glucose in the feed could not be consumed completely. Accordingly, the continuous culture was evaluated in terms of both EPA productivity (P) and glucose assimilation efficiency (E). The parameter eta, defined as the product of P and E, was used as an overall performance index. Since eta is a function of the two independent variables D and S(0), we employed a central composite design to optimize D and S(0) for the highest eta value. Based on the experimental results of the design, a second-order polynomial equation was established to represent the relationship between eta and D and S(0). The optimal values of D and S(0) were subsequently determined as 0.481 day(-1) and 15.56 g/L, respectively by the empirical model. The verification experiment confirmed the validity of the model. Under the optimal conditions, eta value reached 46.5 mg L(-1) day(-1), suggesting a considerably high efficiency of the continuous culture of N. laevis in terms of EPA production and glucose utilization.     

Genome shuffling of Lactobacillus delbrueckii mutant and Bacillus amyloliquefaciens through protoplasmic fusion for L-lactic acid production from starchy wastes

Current study was focused on the development of a non-fastidious lactic acid producing strain having better growth rate, low pH tolerance and good productivity by genome shuffling of a mutant strain of Lactobacillus delbrueckii NCIM 2025 and an amylase producing non-fastidious Bacillus amyloliquefaciens ATCC 23842. After the third cycle of the protoplast fusion, lactic acid production by few fusants was monitored and the best fusant was selected for further studies. Optimization of the important process parameters for lactic acid production was conducted using Plackett-Burman design and response surface methodology. Selected fusant could utilize the liquefied cassava bagasse starch directly with minimum nutrient supplementation for lactic acid production. During validation, 40g/L of lactic acid was obtained ( approximately 96% conversion of starch to lactic acid) by using fusant inoculum (3%, v/v) from 83g/L cassava bagasse (starch content 50% w/w) supplemented with yeast extract and peptone (0.2% each, w/v) and the buffering agent (2% CaCO(3), w/v).     

A new combined approach to improved lipid production using a strictly aerobic and oleaginous yeast

Microbial lipids have potential applications in energy, and food industry, because most of those lipids are triacylglycerol with long‐chain fatty‐acids that are comparable to conventional vegetable oils and can be obtained without arable land requirement. Rhodosporidium toruloides is a strictly aerobic strain, where oxygen plays a crucial role in growth, maintenance, and metabolite production, such as lipids and carotenoids. Dissolved oxygen concentration is one of the major factors affecting yeast physiological and biochemical characteristics. In this context, different approaches have been developed to increase available oxygen by the increasing the aeration and the addition of an oxygen‐vector. The growth of R. toruloides in 2‐L mechanical stirred tank reactor equipped with 1 or 2 porous spargers and a 70 C/N ratio, revealed a lipid content of 0.47 and 0.52 g/g and a lipidic productivity of 0.16 and 0.17 g/L day, respectively. The oxygen‐vector addition, increased the lipidic productivity for 0.20 g/L day and a lipid contend of 0.51 g of lipids/g of biomass. The combined approach, combining high aeration (AA), and 1% of n‐dodecane addition (DA), produced a significant improvement in the lipid accumulation (62%, w/w), when compared with the DA (51%, w/w) and the AA (52%, w/w) approaches. The increasing of lipids accumulation and smaller culture time are key factors for the success of scale‐up and profitability of a bioprocess.     

Extractive lactic acid fermentation using ion-exchange resin

Lactic acid fermentation is an end-product-inhibited reaction. The restriction imposed by lactic acid on its fermentation can be avoided by extractive fermentation techniques. Studies were performed by attaching an ion-exchange resin packed column with a 2-L fermentor for separation of lactic acid. The fermentation, in a conventional batch mode, resulted in a lactic acid yield of 0.828 g . g(-1) and a lactic acid productivity of 0.313 g . L(-1) . h(-1). However, these could be further enhanced to 0.929 g . g(-1) and 1.665 g . L(-1) . h(-1) by extractive fermentation techniques. The effect of temperature on extractive fermentation was remarkable and has been included in this work.     

Efficient preparation of (R)-alpha-monobenzoyl glycerol by lipase catalyzed asymmetric esterification: optimization and operation in packed bed reactor

Optically active (R)-alpha-monobenzoyl glycerol (MBG) was synthesized by Candida antarctica lipase B (CHIRAZYME L-2) catalyzed asymmetric esterification of glycerol with benzoic anhydride in organic solvents. Various conditions, such as the type and composition of the organic solvent, water content of the system, reaction temperature, and concentrations of the substrates were systematically examined and optimized in screw-capped test tubes with respect to both the reaction rate and the enzyme selectivity. 1,4-Dioxane was found to be the best solvent and no additional water was needed for the system. The optimum temperature was around 30 degrees C, while the most suitable substrate concentrations were 100 mM each for glycerol and benzoic anhydride, respectively. However, when excessive anhydride (e.g., 200 mM) was used, the produced MBG could be further transformed into 1,3-dibenzoyl glycerol (DBG) by the same enzyme with a priority to (S)-MBG, resulting in a significant improvement of the product optical purity from ca. 50-70% e.e. Under optimal conditions (100 mM glycerol, 100-200 mM benzoic anhydride, dioxane, 25-30 degrees C), the enzymatic synthesis of (R)-MBG was successfully operated in a packed-bed reactor for about 1 week, with an average productivity of 0.79 g MBG/day/g biocatalyst in the case of continuous operation and 0.94 g MBG/day/g biocatalyst in the case of semicontinuous operation. After refinement and preferential crystallization of the crude product, (R)-MBG could be obtained in an almost optically pure form (>98% e.e.).     

Continuous D-tagatose production by immobilized thermostable L-arabinose isomerase in a packed-bed bioreactor

D-Tagatose was continuously produced using thermostable L-arabinose isomerase immobilized in alginate with D-galactose solution in a packed-bed bioreactor. Bead size, L/D (length/diameter) of reactor, dilution rate, total loaded enzyme amount, and substrate concentration were found to be optimal at 0.8 mm, 520/7 mm, 0.375 h(-1), 5.65 units, and 300 g/L, respectively. Under these conditions, the bioreactor produced about 145 g/L tagatose with an average productivity of 54 g tagatose/L x h and an average conversion yield of 48% (w/w). Operational stability of the immobilized enzyme was demonstrated, with a tagatose production half-life of 24 days.     

Simultaneous saccharification and fermentation of acid-pretreated rapeseed meal for succinic acid production using Actinobacillus succinogenes

Rapeseed meal was evaluated for succinic acid production by simultaneous saccharification and fermentation using Actinobacillus succinogenes ATCC 55618. Diluted sulfuric acid pretreatment and subsequent hydrolysis with pectinase was used to release sugars from rapeseed meal. The effects of culture pH, pectinase loading and yeast extract concentration on succinic acid production were investigated. When simultaneous saccharification and fermentation of diluted acid pretreated rapeseed meal with a dry matter content of 12.5% (w/v) was performed at pH 6.4 and a pectinase loading of 2% (w/w, on dry matter) without supplementation of yeast extract, a succinic acid concentration of 15.5 g/L was obtained at a yield of 12.4 g/100g dry matter. Fed-batch simultaneous saccharification and fermentation was carried out with supplementation of concentrated pretreated rapeseed meal and pectinase at 18 and 28 h to yield a final dry matter content of 20.5% and pectinase loading of 2%, with the succinic acid concentration enhanced to 23.4 g/L at a yield of 11.5 g/100g dry matter and a productivity of 0.33 g/(Lh). This study suggests that rapeseed meal may be an alternative substrate for the efficient production of succinic acid by A. succinogenes without requiring nitrogen source supplementation.     

Direct bioconversion of rice residue from canteen waste into lipids by new amylolytic oleaginous yeast Sporidiobolus pararoseus KX709872

The new amylolytic oleaginous red yeast, Sporidiobolus pararoseus KX709872, produced both α-amylase (540?±?0.09?mU/mL) and amyloglucosidase (23?±?0.00?mU/mL) and showed good ability to directly convert rice residue from canteen waste to biomass and lipids. Effects of medium composition and cultivation conditions on growth and lipid accumulation for strain KX709872 were investigated under shaking flask and upscaling levels. At C?:?N ratio of 25?:?1, pH 5.45, 22.36°C, and 199.40?rpm for 7 days, volumetric production of biomass and lipids, lipid content, and lipid productivity reached 17.69?±?0.44, 8.35?±?0.19?g/L, 49.48?±?0.41% (w/w), and 1.67?±?0.11?g/L/day, respectively. Production of lipids was also implemented in 5.0-L stirred tank bioreactor with 2.5?L of optimized medium at 300?rpm and 3.0 vvm for 5 days. Volumetric production of biomass and lipids, lipid content, and lipid productivity were 16.33?±?0.49, 8.75?±?0.13?g/L, 56.61?±?0.04% (w/w), and 2.19?±?0.03?g/L/day, respectively. Meanwhile, the fatty acids of lipids from strain KX709872 had high oleic acid content (60?62%) which was similar to those of vegetable oils, indicating that these lipids are promising as an alternative biodiesel feedstock. Moreover, the biodiesel derived from lipids of strain KX709872 had properties satisfying the criteria of ASTM D6751 and EN 14214 standards.     

Oxygen uptake and citric acid production by Candida lipolytica Y 1095

The rates of oxygen uptake and oxygen transfer during cell growth and citric acid production by Candida lipolytica Y 1095 were determined. The maximum cell growth rate, 1.43 g cell/L . h, and volumetric oxygen uptake rate, 343 mg O(2)/L . h, occurred approximately 21 to 22 h after inoculation. At the time of maximum oxygen uptake, the biomass concentration was 1.3% w/v and the specific oxygen uptake rate was slightly greater than 26 mg O(2)/g cell . h. The specific oxygen uptake rate decreased to approximately 3 mg O(2)/g cell . h by the end of the growth phase.During citric acid production, as the concentration of dissolved oxygen was increased from 20% to 80% saturation, the specific oxygen uptake and specific citric acid productivity (mg citric acid/g cell . h) increased by 160% and 71%, respectively, at a biomass concentration of 3% w/v. At a biomass concentration of 5% w/v, the specific oxygen uptake and specific citric acid productivity increased by 230% and 82%, respectively, over the same range of dissolved oxygen concentrations.The effect of dissolved oxygen on citric acid yields and productivities was also determined. Citric acid yields appeared to be independent of dissolved oxygen concentration during the initial production phase; however, volumetric productivity (g citric acid/L . h) increased sharply with an increase in dissolved oxygen. During the second or subsequent production phase, citric acid yields increased by approximately 50%, but productivities decreased by roughly the same percentage due to a loss of cell viability under prolonged nitrogen-deficient conditions. (c) 1994 John Wiley & Sons, Inc.     

High-rate continuous production of lactic acid by Lactobacillus rhamnosus in a two-stage membrane cell-recycle bioreactor

It is important to produce L(+)-lactic acid at the lowest cost possible for lactic acid to become a candidate monomer material for promising biodegradable polylactic acid. In an effort to develop a high-rate bioreactor that provides high productivity along with a high concentration of lactic acid, the performance of membrane cell-recycle bioreactor (MCRB) was investigated via experimental studies and simulation optimization. Due to greatly increased cell density, high lactic acid productivity, 21.6 g L(-1) h(-1), was obtained in the reactor. The lactic acid concentration, however, could not be increased higher than 83 g/L. When an additional continuous stirred tank reactor (CSTR) was attached next to the MCRB a higher lactic acid concentration of 87 g/L was produced at significant productivity expense. When the two MCRBs were connected in series, 92 g/L lactic acid could be produced with a productivity of 57 g L(-1) h(-1), the highest productivity among the reports of L(+)-lactic acid that obtained lactic acid concentration higher than 85 g/L using glucose substrate. Additionally, the investigation of lactic acid fermentation kinetics resulted in a successful model that represents the characteristics of lactic acid fermentation by Lactobacillus rhamnosus. The model was found to be applicable to most of the existing data with MCRBs and was in good agreement with Levenspiel's product-inhibition model, and the Luedeking-Piret equation for product-formation kinetics appeared to be effective in representing the fermentation kinetics. There was a distinctive difference in the production potential of cells (cell-density-related parameter in Luedeking-Piret equation) as lactic acid concentration increases over 55 g/L, and this finding led to a more precise estimation of bioreactor performance.     

Potential inhibitors from wet oxidation of wheat straw and their effect on ethanol production of Saccharomyces cerevisiae: wet oxidation and fermentation by yeast

Alkaline wet oxidation (WO) (using water, 6.5 g/L sodium carbonate and 12 bar oxygen at 195 degrees C) was used as pretreatment method for wheat straw (60 g/L), resulting in a hydrolysate and a cellulosic solid fraction. The hydrolysate consisted of soluble hemicellulose (8 g/L), low-molecular-weight carboxylic acids (3.9 g/L), phenols (0.27 g/L = 1.7 mM) and 2-furoic acid (0.007 g/L). The wet oxidized wheat straw hydrolysate caused no inhibition of ethanol production by Saccharomyces cerevisiae ATCC 96581. Nine phenols and 2-furoic acid, identified to be present in the hydrolysate, were each tested in concentrations of 50-100 times the concentration found in the hydrolysate for their effect on fermentation by yeast. At these high concentrations (10 mM), 4-hydroxybenzaldehyde, vanillin, 4-hydroxyacetophenone and acetovanillone caused a 53-67% decrease in the volumetric ethanol productivity in S. cerevisiae compared to controls with an ethanol productivity of 3.8 g/L. The phenol acids (4-hydroxy, vanillic and syringic acid), 2-furoic acid, syringaldehyde and acetosyringone were less inhibitory, causing a 5-16% decrease in ethanol productivity. By adding the same aromatic compounds to hydrolysate (10 mM), it was shown that syringaldehyde and acetovanillone interacted negatively with hydrolysate components on the ethanol productivity. Fermentation in WO hydrolysate, that had been concentrated 6 times by freeze-drying, lasted 4 hours longer than in regular hydrolysate; however, the ethanol yield was the same. The longer fermentation time could not be explained by an inhibitory action of phenols alone, but was more likely caused by inhibitory interactions of phenols with carboxylic acids, such as acetic and formic acid.