Ethanol production in simultaneous saccharification and fermentation of cellulose with temperature profiling

The effects of temperature on enzymatic saccharification of cellulose and simulataneous saccharification and fermentation (SSF) were investigated with 100 g·l⁻¹ Solka Floc, 5g·l⁻¹Trichoderma reesei cellulase, and Zymomonas mobilis ATCC 29191. The following results were obtained: 1) Ethanol fermentation under glucose dificient conditions can proceed for more than 100 h at 30°C but gradually ceases after 50 h of operation at 40°C. 2) Equivalent glucose yield based on cellulose for SSF operated at its optimum temperature (37°C) is higher than that for enzymatic saccharification of cellulose at the same temperature by 32%. However, the same equivalent glucose yields were obtained for both processes if they were operated at their respective optimum temperature. 3) SSF with temperature cycling increased the ethanol productivity but gave similar ethanol yield to SSF at 37°C. 4) SSF with temperature profiling gave an ethanol yield of 0.32 g·g⁻¹ and cellulose use of 0.86 g·g⁻¹ which were increased by 39% and 34% over SSF with temperature cycling and at 37°C.     

Continuous production of an antibiotic polypeptide (nisin) by Lactococcus lactis using a bioreactor coupled to a microfiltration module

The continuous production of nisin, an antibiotic polypeptide, by Lactococcus lactis in a bioreactor system coupled to a microfiltration module is described. Nisin productivity with respect to both cultivation time (ND) and the quantity of glucose consumed (ND/S_f) in continuous production was enhanced by maintaining a low concentration of lactic acid in the broth. A maximum ND of 7.80 × 10⁴ U·l⁻¹·h⁻¹ and ND/S_f of 5.20 × 10³ U·g⁻¹·h⁻¹ were obtained when the glucose concentration in the feed medium was 15 g/l. These values represent about 4.1- and 4.5-fold increases, respectively, over those obtained in batch culture.     

Influence of the concentrations of d-xylose and yeast extract on ethanol production by Pachysolen tannophilus

To determine the most favorable conditions for the production of ethanol by Pachysolen tannophilus, this yeast was grown in batch cultures with various initial concentrations of two of the constituents of the culture medium: d-xylose (s_o), ranging from 1 g·l⁻¹ to 200 g·l⁻¹, and yeast extract (l_o), ranging from 0 g·l⁻¹ to 8 g·l⁻¹. The most favorable conditions proved to be initial concentrations of S_o=25 g·l⁻¹ and l_o=4 g·l⁻¹, which gave a maximum specific growth rate of 0.26 h⁻¹, biomass productivity of 0.023 g·l⁻¹·h⁻¹, overall biomass yield of 0.094 g·g⁻¹, specific xylose-uptake rate (q_s) of 0.3 g·g⁻¹·h⁻¹ (for t=50 h), specific ethanol-production rate (q_E) of 0.065 g·g⁻¹·h⁻¹ and overall ethanol yield of 0.34 g·g⁻¹; q_s values decreased after the exponential growth phase while q_E remained practically constant.     

Improving mass transfer in an inclined tubular photobioreactor

The mass transfer and hydrodynamics of two outdoor tubular photobioreactor designs were compared, a Tredici-design near-horizontal tubular photobioreactor (NHTR) and an enhanced version of this reactor (ENHTR), for the purpose of improving algal growth via improved hydrodynamics. The enhancements included addition of vertical bubble columns at the sparger end and a larger degasser with a diffuser. Gas-liquid mass transfer and other performance measures were assessed for a range of gas sparging rates. The ENHTR modifications proved to be very successful, increasing oxygen stripping and carbon dioxide dissolution by 120–220 % and 0–50 %, respectively. There was an increase in axial mixing and a fourfold decrease in total mixing time. Experiments were conducted to determine that approximately 50 % of the mass transfer occurred in the vertical bubble columns, while 85–90 % of the mass transfer in the near-horizontal tubes occurred in the lower half of the tubes. These improvements can lead to increased algae productivity depending upon culture-specific parameters. The theoretical maximum productivity of a hypothetical algal culture would be 1.6 g m^?2 h^?1 in the NHTR, and we have previously achieved a maximum of 1.5 g m^?2 h^?1 growing Arthrospira at densities up to 7.5 g L^?1 in this reactor. Due to enhanced mass transfer in the ENHTR, the predicted maximum productivity should increase to 4.75 g m^?2 h^?1. The potential for further improvements in productivity due to various additional enhancements is described.     

Flow rate and bead size as critical parameters for immobilized-yeast reactors

The productivity of immobilized yeast cell reactors varies with a number of parameters, including flow, amount and growth rate of yeast, bead size and type of medium. Variation of these parameters has a pronounced effect on reaction rate. This paper presents typical ranges for these productivities and demonstrates the patterns of changes that take place when bead size, flow and reaction medium are varied. Saccharomyces cerevisiae cells were immobilized in calcium alginate beads for the production of ethanol. The productivity of immobilized yeast in a batch reactor (0.2 g ethanol/g yeast · h) was only two-thirds that of free cells suspended at an equivalent cell density (0.3 g ethanol/g yeast · h). Different flow rates and bead sizes were used to ‘optimize’ the productivity. The productivity of 3.34 mm beads at a flow rate of 8.8 litre h^?1(superficial velocity: 0.12 cm s^?1) was 95% higher than that at 1.0 l h^?1. Maximum productivities of 0.34, 0.27, 0.22 g/g yeast· h were obtained (at a flow rate of 8.8 l h^?1) for 9.2% yeast-immobilized beads of 3.34, 4.45 and 5.65 mm in diameter, respectively.     

Engineering high-gravity fermentations for ethanol production at elevated temperature with Saccharomyces cerevisiae

Thermal damage, high osmolarity, and ethanol toxicity in the yeast Saccharomyces cerevisiae limit titer and productivity in fermentation to produce ethanol. We show that long-term adaptive laboratory evolution at 39.5°C generates thermotolerant yeast strains, which increased ethanol yield and productivity by 10% and 70%, in 2% glucose fermentations. From these strains, which also tolerate elevated-osmolarity, we selected a stable one, namely a strain lacking chromosomal duplications. This strain (TTY23) showed reduced mitochondrial metabolism and high proton efflux, and therefore lower ethanol tolerance. This maladaptation was bolstered by reestablishing proton homeostasis through increasing fermentation pH from 5 to 6 and/or adding potassium to the media. This change allowed the TTY23 strain to produce 1.3–1.6 times more ethanol than the parental strain in fermentations at 40°C with glucose concentrations ~300 g/L. Furthermore, ethanol titers and productivities up to 93.1 and 3.87 g·L ⁻¹·hr ⁻¹ were obtained from fermentations with 200 g/L glucose in potassium-containing media at 40°C. Albeit the complexity of cellular responses to heat, ethanol, and high osmolarity, in this study we overcome such limitations by an inverse metabolic engineering approach.     

Continuous high-ethanol fermentation from cane molasses by a flocculating yeast

Repeated-batch fermentation by a flocculating fusant, Saccharomyces cerevisiae HA 2, was done in a molasses medium that contained 20% (w/v) total sugar, at 30°C in an automatically controlled fermentor, and the effects of ethanol concentration on the specific growth rate and the specific production rate of ethanol were studied. Both the specific growth rate and the specific production rate of ethanol fell with increase of ethanol concentration, and there was a linear correlation between each rate and the concentration of thanol. The maximum specific growth rate (μ_max) and the maximum specific production rate of ethanol (q_max) were 0.12 h⁻¹ and 0.1 g ethanol/10⁹ cells·h, respectively. The specific growth rate and the specific production rate of ethanol fell to zero at ethanol concentration of 89 g/l and 95 g/l, respectively. The number of viable cells, calculated from the linear inhibition equation, was 1.3 × 10⁹ cells/ml for production of 85 g/l ethanol at a dilution rate (D₁) of 0.2 h⁻¹. Based on this estimation, a laboratory-scale continuous fermentation, using two fermentors in series, was done. In the second fermentor, 85 g/l ethanol was produced at a dilution rate (D₁) of 0.2 h⁻¹ by the active feedig of the fermented mash from the first fermentor into the second fermentor by pumping (hereafter called active feeding). To maintain the number of viable cells above 10⁹ cells/ml in the second fermentor, a active feeding ratio of more than 23% was required. Under these conditions, 81 g/l ethanol was produced in the second fermentor at a dilution rate (D_t) of 0.25 h⁻¹, and the high ethanol productivity of 20.3 g/l·h could be achieved. A bench-scale continuous fermentation, using two fermentors in series, with a active feeding ratio of 25% was done. An ethanol concentration of 84 g/l in the second fermentor at a dilution rate (D_t) of 0.25 h⁻¹ was achieved, just as it was in the laboratory-scale fermentation test.     

Lipid and biomass production by the halotolerant microalga Nannochloropsis salina

The effect of environmental factors on cell-lipid content, on the growth rate and on the overall productivity of Nannochloropsis salina was tested in the laboratory and in outdoor cultures. Under optimum conditions in the laboratory, the maximum growth rate (μ_max) was 0·030 h⁻¹, which corresponds to a doubling time of 23 h. Cellular lipid content was affected by the phase of growth and the temperature, but not by nitrogen starvation, pH or the source of sea water. The most important factor affecting the output rate of biomass was the cell concentration. The maximum biomass productivity obtained in outdoor ponds was 24·5 g·m⁻²·day⁻¹, and the lipid production rate was 4·0 g m⁻²·day⁻¹.     

Effects of by-products of fermentation of banana pseudostem on ethanol separation by pervaporation

In this work, we performed recovery of ethanol from a fermentation broth of banana pseudostem by pervaporation (PV) as a lower-energy-cost alternative to traditional separation processes such as distillation. As real fermentation systems generally contain by-products, it was investigated the effects of different components from the fermentation broth of banana pseudostem on PV performance for ethanol recovery through commercial flat sheet polydimethylsiloxane (PDMS) membrane. The experiments were compared to a binary solution (ethanol/water) to determine differences in the results due to the presence of fermentation by-products. A real fermented broth of banana pseudostem was also used as feed for the PV experiments. Seven by-products from fermented broth were identified: propanol, isobutanol, methanol, isoamyl alcohol, 1-pentanol, acetic acid, and succinic acid. Moreover, the residual sugar content of 3.02 g/L¹ was obtained. The presence of methanol showed the best results for total permeate flux (0.1626 kg·m⁻²·h⁻¹) and ethanol permeate flux (0.0391 kg·m⁻²·h⁻¹) during PV at 25°C and 3 wt% ethanol, also demonstrated by the selectivity and enrichment factor. The lowest total fluxes of permeate were observed in the experiments containing the acids. Better permeance of 0.1171 from 0.0796 kg·m⁻²·h⁻¹ and membrane selectivity of 9.77 from 9.30 were obtained with real fermentation broth than with synthetic solutions, possibly due to the presence of by-products in the multicomponent mixtures, which contributed to ethanol permeation. The results of this work indicate that by-products influence pervaporation of ethanol with hydrophobic flat sheet membrane produced from the fermented broth of banana pseudostem.     

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.     

Bioprospecting of thermo- and osmo-tolerant fungi from mango pulp–peel compost for bioethanol production

The persistent edaphic stress on microbial succession due to dynamic changes during composting was explored for selection of multi-stress tolerant microbe(s) desirable for ethanol production. A total of 23 strains were isolated from mango compost using four successive enrichments in YP broth (g l^?1): glucose, 100; 150; 250 with ethanol (40) and cycloheximide (0.4) at 40 °C, pH 6.0. Based on multi-gene ribotyping, 14 yeasts (61 %) of Saccharomycetaceae, 2 filamentous fungi (8.6 %) and 7 bacteria (30.4 %) were obtained. Phenetic and phylogenetic analysis of the 14 yeasts revealed 64.3 % tolerant to 500 g l^?1 glucose, growth at 45 °C and resemblance to Candida sp. (14.3 %), Kluyveromyces marxianus (35.7 %), Pichia kudriavzevii (21.4 %) and Saccharomyces cerevisiae (28.6 %). Assessment of the 14 yeasts in glucose fermentation medium (pH 4.5 at 40 °C) showed ethanol productivity of ≥92 % by 12 yeasts with theoretical yields of 90–97 %. Fermentation of molasses (150 g l^?1 glucose equivalent) by P. kudriavzevii D1C at 40 °C resulted in 73.70 ± 0.02 g l^?1 ethanol and productivity of 4.91 ± 0.01 g l^?1 h^?1. Assessment of P. kudriavzevii D1C revealed multi-stress tolerance towards 5-hydroxymethyl furfural, ethanol (20 %, v/v), high gravity and H₂O₂ (0.3 M) indicating suitability for ethanol production using high gravity molasses and pre-treated lignocellulosic biomass fermentation.     

The study of renin–angiotensin–aldosterone in experimental diabetes mellitus

It is generally accepted that hypertension and other vascular pathologies increase in diabetes mellitus (DM) patients as a result of the renin–angiotensin–aldosterone (RAA) system. In this study, changes in the renin‐angiotensin‐aldosterone (RAA) system level was determined in Streptozotocin (STZ)‐injected rats. A total of 46 female Wistar albino rats (180–220 g body weight) was utilized in these experiments. STZ was given intraperitoneally to induce diabetes in rats. Streptozotocin (60 mg kg⁻¹ body weight) was dissolved in 0·1 m citrate–‐phosphate buffer (pH 4–5). The non‐diabetic rats were injected with sterilized buffer alone to act as a control group. Blood glucose levels were 398±8·2 mg dl⁻¹, 488±11·75 mg dl⁻¹ and 658±29·6 mg dl⁻¹ at days 3, 12 and 30 respectively. The level of plasma renin activity (PRA) was measured as 7·69±1·07 ng ml⁻¹ h⁻¹; 1·82±0·22 ng ml⁻¹ h⁻¹ and 0·67±0·12 ng ml⁻¹ h⁻¹ at days 3, 12 and 30, respectively. These values showed that the PRA levels are decreased with increased time period. Serum angiotensin converting enzyme (ACE, E.C. 3.4.15.1) levels were increased at days 12 and 30 (p<0·05 and p<0·005), whereas serum aldosterone levels were increased at days 3 and 12 (p<0·05). The level of urea and creatinine increased at days 12 and 30 (p<0·05 and p<0·005, respectively) when compared to the control group. The data from these experiments indicate that the PRA level decreased whereas ACE activity level increased in diabetic rats compared with the control. Aldosterone levels increased at the first stage of the experiment, but then decreased by the end of the experiment as a result of changes in renin and ACE levels. Copyright © 1999 John Wiley & Sons, Ltd.     

Disruption of glpF gene encoding the glycerol facilitator improves 1,3-propanediol production from glucose via glycerol in Escherichia coli

Engineered Escherichia coli has recently been applied to produce 1,3-propanediol (1,3-PDO) from glucose. A metabolic intermediate in the production pathway, glycerol, is partially secreted into the extracellular of E. coli through a glycerol facilitator encoded by glpF, and this secretion consequently decreases 1,3-PDO production. Therefore, we aimed to determine whether disrupting the glpF gene would improve 1,3-PDO production in E. coli. The intracellular glycerol concentration in a glpF-disruptant was 7·5 times higher than in a non-disruptant. The glpF-disrupted and non-disrupted E. coli strains produced 0·26 and 0·09 g l⁻¹ of 1,3-PDO, respectively, from 1% glucose after 72 h of cultivation. The specific growth rate (μ) and the 1,3-PDO yield from glucose (Y_P/S) in the disruptant were higher than those in the non-disruptant (ΔglpF, μ = 0·08 ± 0·00 h⁻¹, Y_P/S = 0·06 mol mol-glucose⁻¹; BW25113, μ = 0·06 ± 0·00 h⁻¹, Y_P/S = 0·02 mol mol-glucose⁻¹). Disruption of the glpF gene decreased the production of the by-product, acetic acid. These results indicated that disruption of glpF increased the intracellular concentration of glycerol and consequently increased 1,3-PDO production in E. coli.     

Heart rate as an indicator of metabolic rate and activity in adult Atlantic salmon, Salmo salar

Telemetered heart rate (f_H) was examined as an indicator of activity and oxygen consumption rate (VO₂) in adult, cultivated, Atlantic salmon, Salmo salar L. Heart rate was measured during sustained swimming in a flume for six fish at 10° C [mean weight, 1114 g; mean fork length (f. l.), 50·6 cm] and seven fish at 15° C (mean weight, 1119 g; mean f. l., 50·7 cm) at speeds of up to 2·2 body lengths/s. Semi–logarithmic relationships between heart rate and swimming speed were obtained at both temperatures. Spontaneously swimming fish in still water exhibited characteristic heart rate increases associated with activity. Heart rate and Vo₂ were monitored simultaneously in a 575–1 circular respirometer for six fish (three male, three female) at 4° C (mean weight, 1804 g; mean F. L., 62· cm) and six fish (three male, three female) at 10° C (mean weight, 2045 g; mean f. l., 63·2 cm) during spontaneous but unquantified activity. Linear regressions were obtained by transforming data for both f_H and Vo₂ to log values. At each temperature, slopes of the regressions between f_H and Vo₂ for individual fishes were not significantly different, but in some cases elevations were. All differences in elevation were between male and female fish. There were no significant differences in regression slope or elevation for fish of the same sex at the two temperatures and so regressions were calculated for the sexes, pooling data from 4 and 10° C. There was no significant difference in the mean ± S. D. Vo₂ between the sexes at 4° C (male, 66·0 ± 59·6 mgO₂ kg^?1 h^?1; female, 88·0 ± 60·1 mgO₂ kg^?1 h^?1) or 10° C (male, 166·2 ± 115·4 mgO₂ kg^?1 h^?1; female, 169·2 ± 111–1 mgO₂ kg^?1h^?1). Resting Vo₂ (x?± s. d.) at 4°C was 36·7 ± 8.4 mgO₂ kg^?1 h^?1, and 10° C was 72·8 ± 11·9 mgO₂ kg^?1 h^?1. Maximum Vo₂ (x?± S. D.) at 4° C was 250·6 ± 40·2 mgO₂ kg^?1 h^?1, and at 10° C was 423·6 ± 25·2 mgO₂ kg^?1 h^?1. Heart rate appears to be a useful indicator of metabolic rate over the temperature range examined, for the cultivated fish studied, but it is possible that the relationship for wild fish may differ.     

Algal biomass production,N uptake and N2 fixation in a synthetic medium

An experiment was conducted in the growth chamber to quantify the biomass production, N removal and N₂ fixation from a synthetic medium by Chlamydomonas reinhardtii and Anabaena flos-aquae. Nitrogen was supplied at a concentration of 100 mg liter⁻¹ of NO₃⁻−¹⁵N and NH₄⁺−¹⁵ (3·5 atom %), respectively. After 21 days Chlamydomonas reinhardtii removed an average of 83·8 and 78·7 mg N liter⁻¹ as NO₃⁻ and NH₄⁺, respectively. Averages of 0·89 and 0·71 g liter⁻¹ (first batch), 1·63 and 0·95 g liter⁻ (second batch) algal biomass were collected from NO₃⁻ and NH₄⁺ media, respectively. Uptake rates of 0·11 mg ¹⁵N g⁻¹ algae day⁻¹ from NO₃⁻ medium and 0·10 mg ¹⁵N g⁻¹ algae day⁻¹ from NH₄⁺ medium were calculated. Algal cells grown in NO₃⁻ and NH₄⁺ medium contained 71 and 65 g N kg⁻¹ (first batch), 39 and 58 g N kg⁻¹ (second batch), respectively. Anabaena flos-aquae produced averages of 0·58 and 0·46 g liter⁻¹ (first batch), 0·55 and 0·48 g liter⁻¹ (second batch) after 14 days of growth from NO₃⁻ and NH₄⁺ media, respectively. Blue-green algal biomass contained higher N (81–98 g kg⁻¹) than green algae. Isotope dilution method for determining N₂ fixation indicated that 55% and 77% of total N of blue-green algae grown in NO₃⁻ and NH₄⁺ media, respectively, was derived from the atmosphere.     

Effects of dehydration and low temperatures on the oxidation of high-potential cytochrome c by photosynthetic reaction centers in Ectothiorhodospira shaposhnikovii

Effects of temperature and dehydration on the efficiency of electron transfer from membrane-bound high-potential cytochromes c_h to the reaction-center bacteriochlorophyll (P-890) in Ectothiorhodospira shaposhnikovii have been studied. A kinetic analysis of the cytochrome oxidation suggests that there are at least two conformational states of the c_h-P-890 complex, of which only one allows photoinduced electron transfer from cytochrome to P-890⁺. Lowering the temperature of dehydration leads to a change in the proportion of the populations in the two conformations. The observed 2-fold deceleration of cytochrome oxidation can be related only to the diminution of the amount of photoactive cytochromes per reaction center. The rate constant for the transfer of an electron from cytochrome c_h to bacteriochlorophyll is 2.8 · 10⁵ s⁻¹ and is independent of temperature and dehydration (as estimated within the accuracy of the experiments). The effects produced by low temperature and dehydration are completely reversible. The thermodynamic parameters of the transition of the cytochrome from the nontransfer to electron-transfer conformation were estimated. For room temperature (+ 20°C) in chromatophore preparations, ΔG = −5.4 kJ · M⁻¹, ΔH = 60 kJ · M⁻¹, ΔS = 0.22 kJ · M⁻¹ · K⁻¹. For Triton X-100 subchromatophore preparations, the absolute values of the above parameters are significantly lower: ΔG = −2.8 kJ · M⁻¹, ΔH = 18 kJ · M⁻¹, and ΔS = 0.075 kJ · M⁻¹ · K⁻¹. To a larger extent, the above parameters are diminished for chromatophore preparations in an 80% glycerol solution: ΔG = −1.7 kJ · M⁻¹, ΔH = 6 kJ · M⁻¹, ΔS = 0.025 kJ · M⁻¹ · K⁻¹. The data suggest the hydrophobic character of the forces that maintain the P-890-c_h complex in the electron-transfer conformation. The results obtained suggest that electron tunneling within the complex cannot occur until a specific conformational configuration of the complex is formed. The efficiency of cytochrome c_h oxidation is determined by the temperature, the degree of dehydration and the environmental conditions, whereas the transfer of an electron itself in the electron-transfer configuration is essentially independent of temperature and hydration.     

Effect of controlled oxygen limitation on Candida shehatae physiology for ethanol production from xylose and glucose

Carbon distribution and kinetics of Candida shehatae were studied in fed-batch fermentation with xylose or glucose (separately) as the carbon source in mineral medium. The fermentations were carried out in two phases, an aerobic phase dedicated to growth followed by an oxygen limitation phase dedicated to ethanol production. Oxygen limitation was quantified with an average specific oxygen uptake rate (OUR) varying between 0.30 and 2.48 mmolO₂ g dry cell weight (DCW)^?1 h^?1, the maximum value before the aerobic shift. The relations among respiration, growth, ethanol production and polyol production were investigated. It appeared that ethanol was produced to provide energy, and polyols (arabitol, ribitol, glycerol and xylitol) were produced to reoxidize NADH from assimilatory reactions and from the co-factor imbalance of the two-first enzymatic steps of xylose uptake. Hence, to manage carbon flux to ethanol production, oxygen limitation was a major controlled parameter; an oxygen limitation corresponding to an average specific OUR of 1.19 mmolO₂ g DCW^?1 h^?1 allowed maximization of the ethanol yield over xylose (0.327 g g^?1), the average productivity (2.2 g l^?1 h^?1) and the ethanol final titer (48.81 g l^?1). For glucose fermentation, the ethanol yield over glucose was the highest (0.411 g g^?1) when the specific OUR was low, corresponding to an average specific OUR of 0.30 mmolO₂ g DCW^?1 h^?1, whereas the average ethanol productivity and ethanol final titer reached the maximum values of 1.81 g l^?1 h^?1 and 54.19 g l^?1 when the specific OUR was the highest.     

Studies on cephalosporin-C production in an air lift reactor using different growth modes of Cephalosporium acremonium

This paper deals with the studies on Cephalosporin-C production in a lab-scale airlift reactor using Cephalosporium acremonium. Various growth modes, viz. pellets and Siran supported bioparticles were used to improve the process over conventional free mycelial fermentation. Cephalosporin-C production was significantly improved by using bioparticles over the free mycelial culture, probably due to the enhanced mass transfer in the fermentation broth. However, the biofilm of the bioparticles became unstable as the fermentation proceeded, and increase in the free cells in the broth occurs. The maximum specific growth rate of free cells, pellets and Siran carrier were observed to be 0·037, 0·033 and 0·045 h⁻¹, respectively. The oxygen transfer coefficient also improved for the immobilised modes (100 h⁻¹, 70 h⁻¹ for Siran carrier and pellets) and thereby enhanced specific antibiotic productivity, 18–28% were observed.     

Continuous ethanol production from raw starch using a reversibly soluble-autoprecipitating amylase and flocculating yeast cells

Direct ethanol production from raw starch was performed continuously using a combination of a reversibly soluble-autoprecipitating amylase (D-AS) in which Dabiase K-27 was immobilized covalently on an enteric coating polymer (hydroxypropyl methylcellulose acetate succinate, AS) as a carrier, and a flocculating yeast. Continuous production was carried out using a reactor equipped with a mixing vessel and a separation vessel. D-AS and the yeast were separated continuously from the product solution by self-sedimentation in the separation vessel and they were utilized repeatedly. In the continuous saccharification of raw starch by D-AS alone, the glucose productivity was about 3.6 g/l/h at a dilution rate (D) of 0.1 h⁻¹. In the continuous ethanol production from raw starch by a combination of D-AS and flocculating yeast cells, high ethanol productivity up to 2.0 g/l/h was achieved at D=0.1 h⁻¹. Although the enzymatic activity of D-AS is inactivated due to insolubilization of the enzyme by the accumulation of NaCl produced in controlling the pH in the reactor, it is possible to recover the D-AS enzymatic activity by removing the NaCl. This continuous fermentation system suggests a potential for effective ethanol production from raw starch, and it may be widely applicable in heterogeneous culture systems using solid substrates other than raw starch.     

Mathematical modeling of the ethanol fermentation of cashew apple juice by a flocculent yeast: the effect of initial substrate concentration and temperature

In this work, the effect of initial sugar concentration and temperature on the production of ethanol by Saccharomyces cerevisiae CCA008, a flocculent yeast, using cashew apple juice in a 1L-bioreactor was studied. The experimental results were used to develop a kinetic model relating biomass, ethanol production and total reducing sugar consumption. Monod, Andrews, Levenspiel and Ghose and Tyagi models were investigated to represent the specific growth rate without inhibition, with inhibition by substrate and with inhibition by product, respectively. Model validation was performed using a new set of experimental data obtained at 34 °C and using 100 g L⁻¹ of initial substrate concentration. The model proposed by Ghose and Tyagi was able to accurately describe the dynamics of ethanol production by S. cerevisiae CCA008 growing on cashew apple juice, containing an initial reducing sugar concentration ranging from 70 to 170 g L⁻¹ and temperature, from 26 to 42 °C. The model optimization was also accomplished based on the following parameters: percentage volume of ethanol per volume of solution (%V _ethanol/V _solution), efficiency and reaction productivity. The optimal operational conditions were determined using response surface graphs constructed with simulated data, reaching an efficiency and a productivity of 93.5% and 5.45 g L⁻¹ h⁻¹, respectively.