Microbial production of 2,3-butanediol by a newly-isolated strain of Serratia marcescens

A newly-isolated strain of Serratia marcescens, G12, was characterized for 2,3-butanediol (2,3-BD) production. In shake-flask and batch fermentations, 2,3-BD reached 48.5 and 51 g l^?1, respectively. Low amounts of (~8 g l^?1) of acetoin were also formed. In fed-batch fermentations, strain G12 produced 72.8 g 2,3-BD l^?1 with glucose initially at 130 g l^?1. When aeration rate was increased to 2.5 vvm for the fermentation process, 2,3-BD reached 87.8 g l^?1 and the highest productivity was 1.6 g l^?1 h^?1. Acetoin was at 6.2 g l^?1. G12 therefore may be a suitable candidate strain for large-scale production of 2,3-BD.     

Increased production of γ-lactones from hydroxy fatty acids by whole Waltomyces lipofer cells induced with oleic acid

Among several fatty acids tested, oleic acid was selected as the most efficient inducer for the production of 4-hydroxydodecanoic acid, a metabolite of β-oxidation, by Waltomyces lipofer. Cells were induced by incubation for 12 h in a medium containing 10 g l^?1 yeast extract, 10 g l^?1 peptone, 5 g l^?1 oleic acid, 1 g l^?1 glucose, and 0.05 % (w/v) Tween 80. The optimal reaction conditions for the production of γ-lactones by induced cells were pH 6.5, 35 °C, 200 rpm, 0.71 M Tris, 60 g l^?1 hydroxy fatty acid, and 20 g l^?1 cells. Non-induced cells produced 38 g l^?1 γ-dodecalactone from 60 g l^?1 10-hydroxystearic acid after 30 h, with a conversion yield of 63 % (w/w) and a productivity of 1.3 g l^?1 h^?1 under the optimized conditions, whereas induced cells produced 51 g l^?1 γ-dodecalactone from 60 g l^?1 10-hydroxystearic acid after 30 h, with a conversion yield of 85 % (w/w) and a productivity of 1.7 g l^?1 h^?1. The conversion yield and productivity of induced cells were 22 % and 1.3-fold higher, respectively, than those of non-induced cells. Induced cells also produced 28 g l^?1 γ-decalactone and 12 g l^?1 γ-butyrolactone from 60 g l^?1 12-hydroxystearic acid and 60 g l^?1 10-hydroxydecanoic acid, respectively, after 30 h. The concentration, conversion yield, and productivity of γ-dodecalactone and γ-decalactone are the highest reported thus far. This is the first study on the biotechnological production of γ-butyrolactone.     

Uncoupling glucose sensing from GAL metabolism for heterologous lactose fermentation in Saccharomyces cerevisiae

Objectives

Development of a system for direct lactose to ethanol fermentation provides a market for the massive amounts of underutilized whey permeate made by the dairy industry. For this system, glucose and galactose metabolism were uncoupled in Saccharomyces cerevisiae by deleting two negative regulatory genes, GAL80 and MIG1, and introducing the essential lactose hydrolase LAC4 and lactose transporter LAC12, from the native but inefficient lactose fermenting yeast Kluyveromyces marxianus.

Results

Previously, integration of the LAC4 and LAC12 genes into the MIG1 and NTH1 loci was achieved to construct strain AY-51024M. Low rates of lactose conversion led us to generate the Δmig1Δgal80 diploid mutant strain AY-GM from AY-5, which exhibited loss of diauxic growth and glucose repression, subsequently taking up galactose for consumption at a significantly higher rate and yielding higher ethanol concentrations than strain AY-51024M. Similarly, in cheese whey permeate powder solution (CWPS) during three, repeated, batch processes in a 5L bioreactor containing either 100 g/L or 150 g/L lactose, the lactose uptake and ethanol productivity rates were both significantly greater than that of AY-51024M, while the overall fermentation times were considerably lower.

Conclusions

Using the Cre-loxp system for deletion of the MIG1 and GAL80 genes to relieve glucose repression, and LAC4 and LAC12 overexpression to increase lactose uptake and conversion provides an efficient basis for yeast fermentation of whey permeate by-product into ethanol.

     

Two-stage fermentation process for enhanced mannitol production using Candida magnoliae mutant R9

Mutants of Candida magnoliae NCIM 3470 were generated by treatment of ultra-violet radiations, ethyl methyl sulphonate and N-methyl-N′-nitro-N-nitrosoguanidine. Mutants with higher reductase activity were screened by means of 2,3,5-triphenyl tetrazolium chloride agar plate assay. Among the screened mutants, the mutant R9 produced maximum mannitol (i.e. 46 g l^?1) in liquid fermentation medium containing 250 g l^?1 glucose and hence was selected for further experiments. Preliminary optimization studies were carried out on shake-flask level which increased the mannitol production to 60 g l^?1 in liquid fermentation medium containing 300 g l^?1 glucose. A two-stage fermentation process comprising of growth phase and production phase was employed. During the growth phase, glucose was supplemented and aerobic conditions were maintained. Thereafter, the production phase was initiated by supplementing fructose and switching to anaerobic conditions by discontinuing aeration and decreasing the speed of agitation. The strategy of two-stage fermentation significantly enhanced the production of mannitol up to 240 g l^?1, which is the highest among all fermentative production processes and corresponds to 81 % yield and 4 g l^?1 h^?1 productivity without formation of any by-product.     

The effect of hexose ratios on metabolite production in Saccharomyces cerevisiae strains obtained from the spontaneous fermentation of mezcal

Mezcal from Tamaulipas (México) is produced by spontaneous alcoholic fermentation using Agave spp. musts, which are rich in fructose. In this study eight Saccharomyces cerevisiae isolates obtained at the final stage of fermentation from a traditional mezcal winery were analysed in three semi-synthetic media. Medium M1 had a sugar content of 100 g l^?1 and a glucose/fructose (G/F) of 9:1. Medium M2 had a sugar content of 100 g l^?1 and a G/F of 1:9. Medium M3 had a sugar content of 200 g l^?1 and a G/F of 1:1. In the three types of media tested, the highest ethanol yield was obtained from the glucophilic strain LCBG-3Y5, while strain LCBG-3Y8 was highly resistant to ethanol and the most fructophilic of the mezcal strains. Strain LCBG-3Y5 produced more glycerol (4.4 g l^?1) and acetic acid (1 g l^?1) in M2 than in M1 (1.7 and 0.5 g l^?1, respectively), and the ethanol yields were higher for all strains in M1 except for LCBG-3Y5, -3Y8 and the Fermichamp strain. In medium M3, only the Fermichamp strain was able to fully consume the 100 g of fructose l^?1 but left a residual 32 g of glucose l^?1. Regarding the hexose transporters, a high number of amino acid polymorphisms were found in the Hxt1p sequences. Strain LCBG-3Y8 exhibited eight unique amino acid changes, followed by the Fermichamp strain with three changes. In Hxt3p, we observed nine amino acid polymorphisms unique for the Fermichamp strain and five unique changes for the mezcal strains.     

Highly selective hydrolysis for the outer glucose at the C-20 position in ginsenosides by β-glucosidase from Thermus thermophilus and its application to the production of ginsenoside F2 from gypenoside XVII

β-Glucosidase from Thermus thermophilus has specific hydrolytic activity for the outer glucose at the C-20 position in protopanaxadiol-type ginsenosides without hydrolysis of the inner glucose. The hydrolytic activity of the enzyme for gypenoside XVII was optimal at pH 6.5 and 90 °C, with a half-life of 1 h with 3 g enzyme l^?1 and 4 g gypenoside XVII l^?1. Under the optimized conditions, the enzyme converted the substrate gypenoside XVII to ginsenoside F₂ with a molar yield of 100 % and a productivity of 4 g l^?1 h^?1. The conversion yield and productivity of ginsenoside F₂ are the highest reported thus far among enzymatic transformations.     

Kinetics of growth and caffeine demethylase production of Pseudomonas sp. in bioreactor

The effect of various initial caffeine concentrations on growth and caffeine demethylase production by Pseudomonas sp. was studied in bioreactor. At initial concentration of 6.5 g l^?1 caffeine, Pseudomonas sp. showed a maximum specific growth rate of 0.2 h^?1, maximum degradation rate of 1.1 g h^?1, and caffeine demethylase activity of 18,762 U g CDW^?1 (CDW: cell dry weight). Caffeine degradation rate was 25 times higher in bioreactor than in shake flask. For the first time, we show highest degradation of 75 g caffeine (initial concentration 20 g l^?1) in 120 h, suggesting that the tested strain has potential for successful bioprocess for caffeine degradation. Growth kinetics showed substrate inhibition phenomenon. Various substrate inhibition models were fitted to the kinetic data, amongst which the double-exponential (R ² = 0.94), Luong (R ² = 0.92), and Yano and Koga 2 (R ² = 0.94) models were found to be the best. The Luedeking–Piret model showed that caffeine demethylase production kinetics was growth related. This is the first report on production of high levels of caffeine demethylase in batch bioreactor with faster degradation rate and high tolerance to caffeine, hence clearly suggesting that Pseudomonas sp. used in this study is a potential biocatalyst for industrial decaffeination.     

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.     

Effects of galactose and glucose on the hydrolysis reaction of a thermostable β-galactosidase from Caldicellulosiruptor saccharolyticus

A recombinant β-galactosidase from Caldicellulosiruptor saccharolyticus was purified with a specific activity of 211 U mg^?1 by using heat treatment and His-trap affinity chromatography. The native enzyme was an 80-kDa trimer with a molecular mass of 240 kDa. Maximum activity was observed at pH 6.0 and 80ºC, and the half-life at 70ºC was 48 h. The enzyme exhibited hydrolytic activity for p-nitrophenyl-β-d-galactopyranoside (pNPGal), oNPGal, or lactose, whereas no activity for p-nitrophenyl-β-d-glucopyranoside (pNPGlu), oNPGlu, or cellobiose. The catalytic residues E150 and E311 of β-galactosidase from C. saccharolyticus were completely conserved in all aligned glycoside hydrolase family 42 β-galactosidases. The results indicated that the enzyme was a β-galactosidase. Galactose uncompetitively inhibited the enzyme. Glucose inhibition of the enzyme was the lowest among β-galactosidases. When 50 g l^?1 galactose was added, the enzyme activity for pNPGal was reduced to 26%. When 400 g l^?1 glucose instead of galactose was added, the activity was reduced to 82%. When adding galactose (200 g l^?1), only 14% of the lactose was hydrolyzed after 180 min. In contrast, the addition of glucose (400 g l^?1) did not affect lactose hydrolysis, and more than 99% of the lactose was hydrolyzed after 120 min.     

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.     

Butanol production from concentrated lactose/whey permeate: Use of pervaporation membrane to recover and concentrate product

In these studies, butanol (acetone butanol ethanol or ABE) was produced from concentrated lactose/whey permeate containing 211 g L^?1 lactose. Fermentation of such a highly concentrated lactose solution was possible due to simultaneous product removal using a pervaporation membrane. In this system, a productivity of 0.43 g L^?1 h^?1 was obtained which is 307 % of that achieved in a non-product removal batch reactor (0.14 g L^?1 h^?1) where approximately 60 g L^?1 whey permeate lactose was fermented. The productivity obtained in this system is much higher than that achieved in other product removal systems (perstraction 0.21 g L^?1 h^?1 and gas stripping 0.32 g L^?1 h^?1). This membrane was also used to concentrate butanol from approximately 2.50 g L^?1 in the reactor to 755 g L^?1. Using this membrane, ABE selectivities and fluxes of 24.4–44.3 and 0.57–4.05 g m^?2 h^?1 were obtained, respectively. Pervaporation restricts removal of water from the reaction mixture thus requiring significantly less energy for product recovery when compared to gas stripping.     

Effect of photoperiod,light intensity and carbon sources on biomass and lipid productivities of Isochrysis galbana

Biomass and lipid productivities of Isochrysis galbana were optimized using nutrients of molasses (4, 8, 12 g l^?1), glucose (4, 8, 12 g l^?1), glycerol (4, 8, 12 g l^?1) and yeast extract (2 g l^?1). Combinations of carbon sources at different ratios were evaluated in which the alga was grown at three different light intensities (50, 100 and 150 μmol m^?2 s^?1) under the influence of three different photoperiod cycles (12/12, 18/6 and 24/0 h light/dark). A maximum cell density of 8.35 g l^?1 with 32 % (w/w) lipid was achieved for mixotrophic growth at 100 μmol m^?2 s^?1 and 18/6 h light/dark with molasses/glucose (20:80 w/w). Mixotrophic cultivation using molasses, glucose and glycerol was thus effective for the cultivation of I. galbana.     

Evaluation of ethanol production by a new isolate of yeast during fermentation in synthetic medium and sugarcane bagasse hemicellulosic hydrolysate

A new xylose fermenting yeast was isolated from over-ripe banana by enrichment in xylose-containing medium. The phylogenetic analysis of ITS1-5.8S-ITS2 region sequences of ribosomal RNA of isolate BY2 revealed that it shows affiliation to genus Pichia and clades with Pichia caribbica. In batch fermentation, Pichia strain BY2 fermented xylose, producing 15 g l^?1 ethanol from 30 g l^?1 xylose under shaking conditions at 28°C, with ethanol yield of 0.5 g g^?1 and volumetric productivity of 0.31 g l^?1 h^?1. The optimum pH range for ethanol production from xylose by Pichia strain BY2 was 5–7. Pichia strain BY2 also produced 6.08 g l^?1 ethanol from 30 g l^?1 arabinose. Pichia strain BY2 can utilize sugarcane bagasse hemicellulose acid hydrolysate for alcohol production, efficiency of fermentation was improved by neutralization, and sequential use of activated charcoal adsorption method. Percent total sugar utilized and ethanol yield for the untreated hydrolysate was 17.14% w/v and 0.33 g g^?1, respectively, compared with 66.79% w/v and 0.45 g g^?1, respectively, for treated hemicellulose acid hydrolysate. This new yeast isolate showed ethanol yield of 0.45 g g^?1 and volumetric productivity of 0.33 g l^?1 h^?1 from sugarcane bagasse hemicellulose hydrolysate detoxified by neutralization and activated charcoal treatment, and has potential application in practical process of ethanol production from lignocellulosic hydrolysate.     

Expression of exoinulinase genes in Saccharomyces cerevisiae to improve ethanol production from inulin sources

To improve inulin utilization and ethanol fermentation, exoinulinase genes from the yeast Kluyveromyces marxianus and the recently identified yeast, Candida kutaonensis, were expressed in Saccharomyces cerevisiae. S. cerevisiae harboring the exoinulinase gene from C. kutaonensis gave higher ethanol yield and productivity from both inulin (0.38 vs. 0.34 g/g and 1.35 vs. 1.22 g l^?1 h^?1) and Jerusalem artichoke tuber flour (0.47 vs. 0.46 g/g and 1.62 vs. 1.54 g l^?1 h^?1) compared with the strain expressing the exoinulinase gene from K. marxianus. Thus, the exoinulinase gene from C. kutaonensis is advantageous for engineering S. cerevisiae to improve ethanol fermentation from inulin sources.     

Production of 10-hydroxy-12,15(Z,Z)-octadecadienoic acid from α-linolenic acid by permeabilized cells of recombinant Escherichia coli expressing the oleate hydratase gene of Stenotrophomonas maltophilia

Recombinant Escherichia coli, expressing the oleate hydratase gene of Stenotrophomonas maltophilia, was permeabilized by sequential treatments with 0.125 M NaCl and 2 mM EDTA. The optimal conditions for the production of 10-hydroxy-12,15(Z,Z)-octadecadienoic acid from α-linolenic acid by permeabilized cells were 35 °C and pH 7.0 with 0.1 % (v/v) Tween 40, 50 g permeabilized cells l^?1, and 17.5 g α-linolenic acid l^?1. Under these conditions, permeabilized cells produced 14.3 g 10-hydroxy-12,15(Z,Z)-octadecadienoic acid l^?1 after 18 h, with a conversion yield of 82 % (g/g) and a volumetric productivity of 0.79 g l^?1 h^?1. These values were 17 and 168 % higher than those obtained by nonpermeabilized cells, respectively. The concentration, yield, and productivity of 10-hydroxy-12,15(Z,Z)-octadecadienoic acid obtained by permeabilized cells are the highest reported thus far.     

Microbial lipid production: screening with yeasts grown on Brazilian molasses

Rhodotorula glutinis CCT 2182, Rhodosporidium toruloides CCT 0783, Rhodotorula minuta CCT 1751 and Lipomyces starkeyi DSM 70296 were evaluated for the conversion of sugars from Brazilian molasses into single-cell oil (SCO) feedstock for biodiesel. Pulsed fed-batch fermentations were performed in 1.65 l working volume bioreactors. The maximum specific growth rate (µ_max), lipid productivity (Pr) and cellular lipid content were, respectively, 0.23 h^?1, 0.41 g l^?1 h^?1, and 41 % for Rsp. toruloides; 0.20 h^?1, 0.27 g l^?1 h^?1, and 36 % for Rta. glutinis; 0.115 h^?1, 0.135 g l^?1 h^?1, and 27 % for Rta. minuta; and 0.11 h^?1, 0.13 g l^?1 h^?1, and 32 % for L. starkeyi. Based on their microbial lipid productivity, content, and profile, Rsp. toruloides and Rta. glutinis are promising candidates for biodiesel production from Brazilian molasses. All the oils from the yeasts were similar to the composition of plant oils (rapeseed and soybean) and could be used as raw material for biofuels, as well as in food and nutraceutical products.     

Production of δ-decalactone from linoleic acid via 13-hydroxy-9(Z)-octadecenoic acid intermediate by one-pot reaction using linoleate 13-hydratase and whole <Emphasis Type="Italic">Yarrowia lipolytica</Emphasis> cells

Objective

To produce δ-decalactone from linoleic acid by one-pot reaction using linoleate 13-hydratase with supplementation with whole Yarrowia lipolytica cells.

Results

Whole Y. lipolytica cells at 25 g l^?1 produced1.9 g l^?1 δ-decalactone from 7.5 g 13-hydroxy-9(Z)-octadecenoic acid l^?1 at pH 7.5 and 30 °C for 21 h. Linoleate 13-hydratase from Lactobacillus acidophilus at 3.5 g l^?1 with supplementation with 25 g Y. lipolytica cells l^?1 in one pot at 3 h produced 1.9 g l^?1 δ-decalactone from 10 g linoleic acid l^?1 via 13-hydroxy-9(Z)-octadecenoic acid intermediate at pH 7.5 and 30°C after 18 h, with a molar conversion yield of 31 % and productivity of 106 mg l^?1 h^?1.

Conclusion

To the best of our knowledge, this is the first production of δ-decalactone using unsaturated fatty acid.

     

Improvement of 5-aminolevulinic acid production by Rubrivivax benzoatilyticus PS-5 with self-flocculation by co-fermentation of precursors and volatile fatty acids under pH-controlled conditions

Photosynthetic bacteria are known to utilize volatile fatty acids as a carbon source for growth and product formation. In this study, a new isolate, Rubrivivax benzoatilyticus PS-5, possessing self-flocculation properties, was cultivated in modified glutamate-malate (GM) medium containing glutamate and malate as carbon sources. The effect of acetic acid, propionic acid and butyric acid (at 1–4 g L^?1) as co-substrates and 7.5 mM glycine, 10 mM succinic acid as precursors for 5-aminolevulinic acid (ALA) production from R. benzoatilyticus PS-5 was investigated. Among the volatile fatty acids tested, acetic acid was preferred to butyric acid and propionic acid, with the optimum concentrations of 3 g L^?1, 1 g L^?1 and 3 g L^?1, respectively. The highest ALA production was 169.71 μM, 162.16 μM and 46.18 μM, respectively, while the highest productivity was 2.57 μM h^?1, 2.25 μM h^?1 and 0.96 μM h^?1, respectively. The precursor was consumed completely (100 %) while the assimilation of the acetic acid and butyric acid was 62.50 % and 48.65 %, respectively. Supplementation of propionic acid (at 1–4 g l^?1) had a negative effect on growth and ALA production. To increase production efficiency, the pH-control strategy (at pH 6.0–8.0) during fermentation was tested. The optimum pH was 7.0, giving the maximum ALA production of 286.18 μM and a productivity of 3.97 μM h^?1. These values were 1.68-fold and 1.54-fold higher, respectively, than those under uncontrolled pH conditions.     

Enhancing ethanol production from cellulosic sugars using <Emphasis Type="Italic">Scheffersomyces (Pichia) stipitis</Emphasis>

Studies were performed on the effect of CaCO₃ and CaCl₂ supplementation to fermentation medium for ethanol production from xylose, glucose, or their mixtures using Scheffersomyces (Pichia) stipitis. Both of these chemicals were found to improve maximum ethanol concentration and ethanol productivity. Use of xylose alone resulted in the production of 20.68 ± 0.44 g L^?1 ethanol with a productivity of 0.17 ± 0.00 g L^?1 h^?1, while xylose plus 3 g L^?1 CaCO₃ resulted in the production of 24.68 ± 0.75 g L^?1 ethanol with a productivity of 0.21 ± 0.01 g L^?1 h^?1. Use of xylose plus glucose in combination with 3 g L^?1 CaCO₃ resulted in the production of 47.37 ± 0.55 g L^?1 ethanol (aerobic culture), thus resulting in an ethanol productivity of 0.39 ± 0.00 g L^?1 h^?1. These values are 229 % of that achieved in xylose medium. Supplementation of xylose and glucose medium with 0.40 g L^?1 CaCl₂ resulted in the production of 44.84 ± 0.28 g L^?1 ethanol with a productivity of 0.37 ± 0.02 g L^?1 h^?1. Use of glucose plus 3 g L^?1 CaCO₃ resulted in the production of 57.39 ± 1.41 g L^?1 ethanol under micro-aerophilic conditions. These results indicate that supplementation of cellulosic sugars in the fermentation medium with CaCO₃ and CaCl₂ would improve economics of ethanol production from agricultural residues.     

Metabolic,physiological and kinetic aspects of the alcoholic fermentation of whey permeate by Kluyveromyces fragilis NRRL 665 and Kluyveromyces lactis NCYC 571

Optimum growth conditions for the fermentation of non-concentrated whey permeate by Kluyveromyces fragilis NRRL 665 have been defined. Use of 3.75 g yeast extract l^?1, a growth temperature of 38°C and a pH of 4.0 allowed a maximum productivity of 5.23 g ethanol l^?1 h^?1 in continuous culture with a yield 91% of theoretical. Complete batch fermentation of permeate with 100 g lactose l^?1 was possible with a maximum specific growth rate of 0.276 h^?1 without any change in ethanol yield. Fermentation of concentrated permeate resulted, however, in a general decrease of specific substrate consumption rate, demonstrated by the inability to completely convert an initial 90 or 150 g lactose l^?1 in continuous culture, even at dilution rates as low as 0.05 and 0.08 h^?1, respectively. The decrease could be related to substrate inhibition, to an increase in osmotic pressure caused by lactose and salts, and to ethanol inhibition of both alcohol and biomass yield. The decrease in specific productivity could be counterbalanced by use of high cell density cultures, obtained by cell recycle of K. fragilis. Fermentation of a non-concentrated permeáte at a dilution rate of 1 h^?1 resulted in a productivity of 22 g l^?1 h^?1 at 22 g ethanol l^?1. Cell recycle using flocculating Kluyveromyces lactis NCYC 571 was also tested. With this strain a productivity of 9.3 g l^?1 h^?1 at 45 g product l^?1 was attained at a dilution rate of 0.2 h^?1, with an initial lactose concentration of 95 g l^?1.