Challenges in enzymatic hydrolysis and fermentation of pretreated Arundo donax revealed by a comparison between SHF and SSF

The perennial herbaceous crop Arundo donax is a potential feedstock for second-generation bioethanol production. In the present work, two different process options were investigated for the conversion of two differently steam-pretreated batches of A. donax. The pretreated raw material was converted to ethanol with a xylose-consuming Saccharomyces cerevisiae strain, VTT C-10880, by applying either separate hydrolysis and fermentation (SHF) or simultaneous saccharification and fermentation (SSF). The highest overall ethanol yield and final ethanol concentration were achieved using SHF (0.27 g g^?1 and 20.6 g L^?1 compared to 0.24 g g^?1 and 19.0 g L^?1 when SSF was used). The performance of both SHF and SSF was improved by complementing the cellulolytic enzymes with hemicellulases. The higher amount of acetic acid in one of the batches was shown to strongly affect xylose consumption in the fermentation. Only half of the xylose was consumed when batch 1 (high acetic acid) was fermented, compared to that 94% of the xylose was consumed in fermentation of batch 2 (lower acetic acid). Furthermore, the high amount of xylooligomers present in the pretreated materials considerably inhibited the enzymatic hydrolysis. Both the formation of xylooligomers and acetic acid thus need to be considered in the pretreatment process in order to achieve efficient conversion of A. donax to ethanol.     

Production of gluconic acid from glucose by Aspergillus niger: growth and non-growth conditions

Batch fermentation of glucose to gluconic acid was conducted using Aspergillus niger under growth and non-growth conditions using pure oxygen and air as a source of oxygen for the fermentation in 2 and 5 l stirred tank reactors (batch reactor). Production of gluconic acid under growth conditions was conducted in a 5 l batch reactor. Production and growth rates were higher during the period of supplying pure oxygen than that during supplying air, and the substrate consumption rate was almost constant. For the production of gluconic acid under non-growth conditions, conducted in the 2 l batch reactor, the effect of the pure oxygen flow rate and the biomass concentration on the gluconic acid production was investigated and an empirical equation suggested to show the dependence of the production rate r_p on the biomass concentration C_x and oxygen flow rate Q, at constant operating conditions (30 °C, 300 rpm and pH 5.5). Biomass concentration had a positive effect on the production rate r_p, and the effect of Q on r_p was positive at high biomass concentrations.     

Aerobiosis–anaerobiosis transition has a significant impact on organic acid production by Corynebacterium glutamicum

Corynebacterium glutamicum is known to produce organic acids under anaerobic culture conditions, in particular, lactic, succinic, and acetic acids. Our study is focused on acetic and succinic acid production using a lactate dehydrogenase-deficient strain of C. glutamicum. Usually, with this bacterium, the organic acid production process is based on an initial aerobic growth phase, followed by a rapid deoxygenation and an anaerobic production phase. In our study, we demonstrated that this strategy was unfavorable for the production of organic acids. Conversely, we showed that applying the best transition strategy based on progressive deoxygenation significantly increased the concentration of organic acids up to 640%. This was observed either by applying controlled dissolved oxygen concentrations or by decreasing the steps of gas flow rates. Our results also showed that applying constant oxygen transfer flux throughout the culture, and thus in the absence of the anaerobic phase, promoted constant production yields (approximately 0.5 mol of succinate or acetate per mole of glucose). In this case, acetate production (120 mM) was favored over succinate production (132 mM), resulting in a decrease in the molar ratio of products (succinate/acetate) from 4.8 to 1.1 between progressive deoxygenation and constant OTR cultures.     

Ethanol and acetate synthesis from waste gas using batch culture of Clostridium ljungdahlii

Single inorganic carbon source was used for production of chemicals and fuels via fermentation processes. Clostridium ljungdahlii, a strictly anaerobic autotrophic bacterium, was grown on synthesis gas to produce acetate and ethanol from gaseous substrates. C. ljungdahlii was grown on a various concentrations of carbon monoxide with synthesis gas total pressures of 0.8–1.8 atm with an interval of 0.2 atm. The cell and product yields were 0.015 g cell/g CO and 0.41 g acetate/g CO, respectively. Formation of acetate was steady and the production trend was about the same for all of the gases initial pressure and at constant cell density. The ethanol concentration was enhanced by the initial presence of hydrogen and carbon dioxide in the liquid phase. There was no substrate inhibition while C. ljungdahlii was grown in the batch fermentation, even at high system pressure of 1.6 and 1.8 atm. A desired product molar ratio of ethanol:acetate (5:1) was achieved with total gas pressure of 1.6 and 1.8 atm.     

Production of 1,3-propanediol, 2,3-butanediol and ethanol by a newly isolated Klebsiella oxytoca strain growing on biodiesel-derived glycerol based media

The production of 1,3-propanediol, 2,3-butanediol and ethanol was studied, during cultivations of strain Klebsiella oxytoca FMCC-197 on biodiesel-derived glycerol based media. Different kinds of glycerol feedstocks and experimental conditions had an important impact upon the distribution of metabolic products; production of 1,3-propanediol was positively influenced by stable pH conditions and by the absence of N₂ gas infusions throughout the fermentation. Thus, during batch bioreactor fermentations conducted at increasing glycerol concentrations, 1,3-propanediol at 41.3 g/L and yield ～47% (w/w) was achieved at initial glycerol concentration ～120 g/L. At even higher initial glycerol media (150 and 170 g/L), growth was not ceased, but 1,3-propanediol production declined. During fed-batch fermentation under optimal experimental conditions, 126 g/L of glycerol were converted into 50.1 g/L of 1,3-propanediol. In this experiment, also 25.2 g/L of ethanol (conversion yield ～20%, w/w) were formed. A batch-bioreactor culture was performed under non-sterilized conditions and the 1,3-propanediol production was almost equivalent to the sterilized process. Concerning 2,3-butanediol formation, the most detrimental parameter was the absence of N₂ sparging and as a result, no 2,3-butanediol was produced. The presence of glucose as co-substrate seriously enhanced 2,3-butanediol production; when commercial glucose was employed as sole substrate, 32.1 g/L of 2,3-butanediol were formed.     

Enhancement of growth rate and β-galactosidase activity,and variation in organic acid profile of Bifidobacterium animalis subsp. lactis Bb 12

The behavior of Bifidobacterium animalis subsp. lactis Bb 12 under batch cultivation, after continuous culturing for up to 12 d, was monitored in skim milk-based media. Previous continuous culture for longer than 6 d affected the physiology of said microorganism. The minimum inhibitory concentrations of lactic and acetic acids increased from 18 to 26 g/l, whereas the molar ratio of acetic to lactic acid increased from 0.8 to 1.55, when the previous continuous culture increased its duration from 1 to 12 d. The specific lactose consumption rate decreased from 0.94 to 0.77 g_lactose/g_{cell dry mass}/h within the batch culture timeframe; this was concomitant with greater amounts of acetic and formic acids, and lower amounts of lactic acid produced. The β-galactosidase activity increased as continuous culturing time increased, and reached 446 units/ml by 12 d; however, the rate of enzyme synthesis decreased concomitantly. Succinic acid was produced during the exponential growth and stationary phases of the batch culture, but the former at exponential growth phase was higher as the continuous culturing time was longer. For comparison purposes, batch cultivation of samples taken from continuous cultures by 1 and 12 d was done using a semi-synthetic medium with glucose as carbon source; a pattern similar to that observed when using skim milk-based media was observed.     

The effect of prehydrolysis and improved mixing on high-solids batch simultaneous saccharification and fermentation of spruce to ethanol

In the production of ethanol from lignocellulosic material, it is necessary to reach a high ethanol concentration after fermentation. Simply increasing the substrate concentration leads to stirring problems and inhibition of the enzymes and yeast in the process.Batch simultaneous saccharification and fermentation (SSF) of steam-pretreated spruce with 13.7% water-insoluble solids (WIS) (25% total solids (TS)) was run in a stirred-tank reactor as well as in two reactors designed to handle solid or semi-solid material. In all reactors, the overall ethanol yields were only between 5 and 6%. Fermentation of the liquid fraction of the steam-pretreated spruce slurry resulted in an overall ethanol yield of 85%.22 h of prehydrolysis at 48 °C prior to SSF at 32 °C significantly increased the overall ethanol yield to 72% (final ethanol concentration of 47.8 g/L), using the whole slurry of steam-pretreated spruce at a dry matter content of 13.7% WIS (25% TS).     

Slow generation of hydrogen sulfide from sulfane sulfurs and NADH models

Here we report the model studies of the reactions between NADH models (using HEH and BNAH) and sulfane sulfurs (using polysulfides). Such reactions could lead to the oxidation of NADH models and the production of hydrogen sulfide (H₂S). Kinetics of the reaction between BNAH and elemental sulfur S₈ were determined in ethanol and the second-order rate constant was found to be 0.074 M^?1 min^?1 (at 37 °C) suggesting this is a slow process.     

Development and examination of a granular nitrogen-fixing wastewater treatment system

This work presents the first success at aerobic granulation in a nitrogen deficient system. Two sequencing batch reactors (SBRs) were used to treat nitrogen deficient (the N-fix system) or nitrogen-sufficient (containing NH₄Cl) synthetic wastewater (acetic acid as the sole carbon source). Granulation was observed in both systems, with particularly large granules (average diameter: 7 mm) grown in the N-fix system. We propose that the unique morphology of nitrogen-fixing granules is a consequence of the response of oxygen-sensitive diazotrophs to elevated oxygen concentrations.Both the nitrogen-fixing and nitrogen-supplemented systems were shown to be capable of removing all of the influent substrate carbon. Excellent biomass settleability characteristics were obtained, with the N-fix system having a final sludge volume index (SVI) of less than 100 mL g⁻¹ and its granules having settling velocities of over 1.4 cm s⁻¹. However, moderately high solids discharges were recorded for both systems, which revealed a potential limitation of granular sludge processes that is not widely discussed in the literature.     

Mixed culture of Saccharomyces cerevisiae and Acetobacter pasteurianus for acetic acid production

Mixed culture of Saccharomyces cerevisiae and Acetobacter pasteurianus was carried out for high yield of acetic acid. Acetic acid production process was divided into three stages. The first stage was the growth of S. cerevisiae and ethanol production, fermentation temperature and aeration rate were controlled at 32 °C and 0.2 vvm, respectively. The second stage was the co-culture of S. cerevisiae and A. pasteurianus, fermentation temperature and aeration rate were maintained at 34 °C and 0.4 vvm, respectively. The third stage was the growth of A. pasteurianus and production of acetic acid, fermentation temperature and aeration rate were controlled at 32 °C and 0.2 vvm, respectively. Inoculation volume of A. pasteurianus and S. cerevisiae was 16% and 0.06%, respectively. The average acetic acid concentration was 52.51 g/L under these optimum conditions. To enhance acetic acid production, a glucose feeding strategy was subsequently employed. When initial glucose concentration was 90 g/L and 120 g/L glucose was fed twice during fermentation, acetic acid concentration reached 66.0 g/L.     

High cell density co-culture for production of recombinant hydrolases

Sugarcane bagasse is a residue with great potential as a feedstock for second-generation ethanol production. One of the approaches studied for making use of this material is the utilization of enzymes to hydrolyze the cell wall carbohydrates and generate fermentable sugars. These enzymes can be produced by cultivation of filamentous fungi or bacteria; however, the high production cost still represents a bottleneck to second-generation ethanol production. Expression of recombinant hydrolases through a co-culture strategy could be an interesting alternative for producing a recombinant cocktail at high levels of productivity that is tailor-made for each material to be hydrolyzed. In this study we evaluate the production of hydrolases by co-culturing two recombinant Escherichia coli, each expressing a specific hydrolase, β-1,3-1,4-glucanase or β-1,4-xylanase, both isolated from Bacillus subtilis. The cultures were conducted in bioreactors in batch and fed-batch mode in order to reach high cell densities. Co-culture in batch cultivation reached a dry cell weight of 10.4 g/L and volumetric activities of 31.96 U/mL and 11.89 U/mL for xylanase and endoglucanase, respectively. Fed-batch cultivation reached a dry cell weight of 60 g/L and the volumetric activities of xylanase and endoglucanase were respectively up to 5 and 1.3 times higher than those in batch mode. A competition assay indicates that no clone predominates over the other during cultivation. These results suggest that co-culture is a potential technique for producing recombinant hydrolase cocktails at lower cost than those associated with the production of a single culture.     

Glycerol utilisation for the production of chemicals: Conversion to succinic acid,a combined experimental and computational study

An effective method for the valorisation of the main by-product of biodiesel production, i.e. glycerol is investigated in this work. It involves the biological conversion of glycerol to succinic acid, a top added-value material, which can be used as a building block for the production of various commodity and specialty chemicals. Our aim is to give new insights into this bioprocess, which has so far received little attention and is open for further investigation, through a combination of experimental and computational studies. The microorganism employed here was Actinobacillus succinogenes in batch bioreactors where glycerol was used as the sole carbon source.The highest obtained product yield, final succinate concentration and productivity were found to be equal to 1.23 g-succinate/g-glycerol, 29.3 g-succinate/L and 0.27 g-succinate/L/h, respectively. Furthermore, an unstructured model of the batch experiments was developed by considering both substrate and product inhibition. Kinetic parameters of the model were estimated by minimising the difference between experimental and predicted values. The corresponding optimisation problem was solved by using a combination of stochastic and deterministic methodologies, with the goal to probabilistically compute global minima and the resulting parameter values. The model developed can be utilised to successfully predict the concentration profiles of the five most important state variables (biomass, glycerol, succinic acid, formic acid, and acetic acid) with different initial glycerol concentrations. Scaled-up experiments in larger-scale bioreactors were used for further validation purposes. Our model can be further used to compute optimal operating/parametric conditions, which maximise yield, productivity and/or the final succinic acid concentration.     

Inhibition of CYP2E1 leads to decreased malondialdehyde–acetaldehyde adduct formation in VL-17A cells under chronic alcohol exposure

AimEthanol metabolism leads to the formation of acetaldehyde and malondialdehyde. Acetaldehyde and malondialdehyde can together form malondialdehyde–acetaldehyde (MAA) adducts. The role of alcohol dehydrogenase (ADH) and cytochrome P4502E1 (CYP2E1) in the formation of MAA-adducts in liver cells has been investigated.Main methodsChronic ethanol treated VL-17A cells over-expressing ADH and CYP2E1 were pretreated with the specific CYP2E1 inhibitor — diallyl sulfide or ADH inhibitor — pyrazole or ADH and CYP2E1 inhibitor — 4-methyl pyrazole. Malondialdehyde, acetaldehyde or MAA-adduct formation was measured along with assays for viability, oxidative stress and apoptosis.Key findingsInhibition of CYP2E1 with 10 μM diallyl sulfide or ADH with 2 mM pyrazole or ADH and CYP2E1 with 5 mM 4-methyl pyrazole led to decreased oxidative stress and toxicity in chronic ethanol (100 mM) treated VL-17A cells. In vitro incubation of VL-17A cell lysates with acetaldehyde and malondialdehyde generated through ethanol led to increased acetaldehyde (AA)-, malondialdehyde (MDA)-, and MAA-adduct formation. Specific inhibition of CYP2E1 or ADH and the combined inhibition of ADH and CYP2E1 greatly decreased the formation of the protein aldehyde adducts. Specific inhibition of CYP2E1 led to the greatest decrease in oxidative stress, toxicity and protein aldehyde adduct formation, implicating that CYP2E1 accelerates the formation of protein aldehyde adducts which can be an important mechanism for alcohol mediated liver injury.SignificanceCYP2E1-mediated metabolism of ethanol leads to increased AA-, MDA-, and MAA-adduct formation in liver cells which may aggravate liver injury.     

Inhibition of cellulases by phenols

Enzyme hydrolysis of pretreated cellulosic materials slows as the concentration of solid biomass material increases, even though the ratio of enzyme to cellulose is kept constant. This form of inhibition is distinct from substrate and product inhibition, and has been noted for lignocellulosic materials including wood, corn stover, switch grass, and corn wet cake at solids concentrations greater than 10 g/L. Identification of enzyme inhibitors and moderation of their effects is of considerable practical importance since favorable ethanol production economics require that at least 200 g/L of cellulosic substrates be used to enable monosaccharide concentrations of 100 g/L, which result in ethanol titers of 50 g/L. Below about 45 g/L ethanol, distillation becomes energy inefficient. This work confirms that the phenols: vanillin, syringaldehyde, trans-cinnamic acid, and hydroxybenzoic acid, inhibit cellulose hydrolysis in wet cake by endo- and exo-cellulases, and cellobiose hydrolysis by β-glucosidase. A ratio of 4 mg of vanillin to 1 mg protein (0.5 FPU) reduces the rate of cellulose hydrolysis by 50%. β-Glucosidases from Trichoderma reesei and Aspergillus niger are less susceptible to inhibition and require about 10× and 100× higher concentrations of phenols for the same levels of inhibition. Phenols introduced with pretreated cellulose must be removed to maximize enzyme activity.     

Genetic algorithm-based medium optimization for enhanced production of fluorescent pseudomonad R81 and siderophore

Fluorescent pseudomonad R81, a root-colonizing bacterium, is a potential bio-inoculant due to its plant growth promoting characteristics. It produces hydroxamate-type siderophore which is involved in disease suppression in plants. Genetic algorithm (GA) methodology was applied for the optimization of siderophore and cell mass production simultaneously in shake flask experiments. A total of 10 medium components were optimized within 80 experiments. A high siderophore concentration of 1.9 g/L and cell mass concentration of 2.8 g/L was achieved in the optimized medium. The application of GA was well suited for determination of optimum concentration levels of the medium constituents for a bi-objective function. GA was able to increase the siderophore concentration by 2.8-fold when compared to RSM-based optimization. Further, the batch fermentation of the GA-optimized medium in 14 L bioreactor without pH control produced 2.2 g/L siderophore in 36 h, the highest reported so far. GA was also successfully used to estimate the kinetic parameters of the mathematical models of the batch fermentation.     

Physiological and morphological study of encapsulated Saccharomyces cerevisiae

The impact of encapsulation on the anaerobic growth pattern of S. cerevisiae CBS 8066 in a defined synthetic medium over 20 consecutive batch cultivations was investigated. In this period, the ethanol yield increased from 0.43 to 0.46 g/g, while the biomass and glycerol yields decreased by 58 and 23%, respectively. The growth rate of the encapsulated cells in the first batch was 0.13 h⁻¹, but decreased gradually to 0.01 h⁻¹ within the 20 sequential batch cultivations. Total RNA content of these yeast cells decreased by 39% from 90.3 to 55 mg/g, while the total protein content decreased by 24% from 460 to 350 mg/g. On the other hand, the stored carbohydrates, that is, glycogen and trehalose content, increased by factors of 4.5 and 4 within 20 batch cultivations, respectively. Higher biomass concentrations inside capsules led to a lower glucose diffusion rate through the membrane, and volumetric mass transfer coefficient for glucose was drastically decreased from 6.28 to 1.24 (cm³/min) by continuing the experiments. Most of the encapsulated yeast existed in the form of single and non-budding cells after long-term application.     

Factors affecting the biotransformation of trimethylammonium compounds into l-carnitine by Escherichia coli

The biotransformation of d-carnitine and crotonobetaine into l-carnitine with wild and transformed E. coli strains under batch and continuous operation was optimised. In batch, the best conditions for the transformed strain were 30% oxygen saturation, a temperature of 41 °C and a minimal medium, whereas anaerobic cultures in either complex or minimal media at 37 °C and pH 7.5 were optimal for the wild strain. Studies on the expression of the enzymes involved in trimethylammonium metabolism showed that l-carnitine dehydratase activity was always higher than that of d-carnitine racemase. Experiments with the transformed strain in continuous cell-recycle reactors showed that, despite the higher productivity that could be achieved (0.65–1.2 g/L h), plasmid-bearing cells were segregated even when a selective medium was used. This fact was also confirmed by studying the evolution of the d-carnitine racemase level. Immobilization of the transformed strain in κ-carrageenan gels allowed continuous operation for l-carnitine production with no plasmid loss. In continuous processes with cell-retention systems, the wild strain showed higher productivity and stability than the transformed strain. Moreover, crotonobetaine was a better substrate for both strains used. Recycling with hollow-fiber cartridges provided the highest biomass level even though the l-carnitine dehydratase/biomass ratio was lower. However, membrane composition and cut-off had less influence on reactor performance as similar levels of productivity were attained. In spite of this, continuous processes attained a l-carnitine production as high as 11.5 g/L h as a result of the high enzyme induction and biomass levels.     

Batch and continuous fermentative production of hydrogen with anaerobic sludge entrapped in a composite polymeric matrix

Cell immobilization techniques were adopted to biohydrogen production using immobilized anaerobic sludge as the seed culture. Sucrose-based synthetic wastewater was converted to H₂ using batch and continuous cultures. A novel composite polymeric material comprising polymethyl methacrylate (PMMA), collagen, and activated carbon was used to entrap biomass for H₂ production. Using the PMMA immobilized cells, the favorable conditions for batch H₂ fermentation were 35 °C, pH 6.0, and an 20 g COD l⁻¹ of sucrose, giving a H₂ production rate of 238 ml h⁻¹ l⁻¹ and a H₂ yield of 2.25 mol H₂ mol sucrose⁻¹. Under these optimal conditions, continuous H₂ fermentation was conducted at a hydraulic retention time (HRT) of 4–8 h, giving the best H₂-producing rate of 1.8 l h⁻¹ l⁻¹ (over seven-fold of the best batch result) at a HRT of 6 h and a H₂ yield of 2.0 mol H₂ mol sucrose⁻¹. The sucrose conversion was essentially over 90% in all runs. The biogas consisted of only H₂ and CO₂. The major soluble metabolites were butyric acid, acetic acid, and 2,3-butandiol, while a small amount of ethanol also detected. The PMMA-immobilized-cell system developed in this work seems to be a promising H₂-producing process due to the high stability in continuous operations and the capability of achieving a competitively high H₂ production rate under a relatively low organic loading rate.     

Enhanced ethanol production by continuous fermentation in a two-tank system with cell recycling

An experimental method for producing ethanol continuously was designed and tested with a cell-recycling two-tank system, which was composed of two fermentors, each of which was individually equipped with a settler for recycling flocculent yeast. This system was effective for the continuous fermentation of ethanol from sucrose at high cell-recycling (r = 0.8–0.9) and dilution (up to 0.48 h^?1) rates. The system has several advantages; the high cell concentration in the fermentors and relief of substrate and product inhibition. Thus, the enhanced productivity using this continuous fermentation with the two-tank cell-recycling system was significantly higher compared with that of the batch fermentation. The results indicate that increased recycling ratios caused an increase in biomass concentration and subsequently, product concentration in the tank. The ethanol productivity increased with the dilution rate, but higher dilution rates could render increasing amounts of sugar unconverted. Continuous fermentation with the sugar feed concentration of 160 g/l at r = 0.9 and dilution rate of 0.2 h^?1 achieved the highest productivity with less than 2% of the unconverted sugar in the product steam. Under the same cell recycling ratios a productivity range of 6.9–7.5 g/l h^?1 could be achieved with feeding concentrations of 80–200 g/l, while batch fermentation at these sugar concentrations led to productivities of 3.85–4.48 g/l h^?1.     

Integrated continuous winemaking process involving sequential alcoholic and malolactic fermentations with immobilized cells

An integrated winemaking process – including sequential alcoholic and malolactic fermentations operated continuously – was developed. For the continuous alcoholic fermentation, yeast cells (Saccharomyces cerevisiae) were immobilized either on grape stems or on grape skins, while bacterial cells (Oenococcus oeni) used for conducting continuous malolactic fermentation were immobilized on grape skins only. The produced wines were subjected to chemical analysis by HPLC (ethanol, glycerol, sugars and organic acids) and by gas chromatography (major and minor volatile compounds). The final proposed integrated continuous process permitted the production of 960 mL/d of a dry white wine, with an alcoholic strength of about 13 vol%, by using two 1.5 L tower bed reactors packed with 260 g of grape skins. The produced wines revealed a good physicochemical quality. Moreover, 67% of the malic acid concentration could be reduced in the second reactor. Both fermentative processes proved to be much more efficient than those conducted traditionally with free cells or even with immobilized cells, but in the batch mode of operation.