Development of medium for enhanced production of glutaminase-free <Emphasis Type="SmallCaps">l</Emphasis>-asparaginase from <Emphasis Type="Italic">Pectobacterium carotovorum</Emphasis> MTCC 1428

Glutaminase-free l-asparaginase is known to be an excellent anticancer agent. In the present study, statistically based experimental designs were applied to maximize the production of glutaminase-free l-asparaginase from Pectobacterium carotovorum MTCC 1428. Nine components of the medium were examined for their significance on the production of l-asparaginase using the Plackett–Burman experimental design. The medium components, viz., glucose, l-asparagine, KH₂PO₄, and MgSO₄·7H₂O, were screened based on their high confidence levels (P < 0.04). The optimum levels of glucose, l-asparagine, KH₂PO₄, and MgSO₄·7H₂O were found to be 2.076, 5.202, 1.773, and 0.373 g L⁻¹, respectively, using the central composite experimental design. The maximum specific activity of l-asparaginase in the optimized medium was 27.88 U mg⁻¹ of protein, resulting in an overall 8.3-fold increase in the production compared to the unoptimized medium.     

d-Glucose does not catabolite repress a transketolase-deficientd-ribose-producingBacillus subtilis mutant strain

WhenBacillus subtilis strain ATCC 21951, a transketolase-deficientd-ribose-producing mutant, was grown ond-glucose plus a second substrate which is metabolized via the oxidative pentose phosphate cycle (d-gluconic acid,d-xylose,l-arabinose ord-xylitol),d-glucose did not catabolite repress metabolism of the second carbon source. Thed-ribose yield obtained with the simultaneously converted carbon substrates, significantly exceeded that when onlyd-glucose was used. In addition, the concentration of glycolytic by-products and the fermentation time significantly decreased. Based on these findings, a fermentation process was developed withB. subtilis strain ATCC 21951 in whichd-glucose (100 g L^–1) andd-gluconic acid (50 g L^–1) were converted into 45 g L^–1 ofd-ribose and 7.5 g L^–1 of acetoin. A second process, based ond-glucose andd-xylose (100 g L^–1 each), yielded 60 g L^–1 ofd-ribose and 4 g L^–1 of acetoin plus 2,3-butanediol. Both mixed carbon source fermentations provide excellent alternatives to the less efficientd-glucose-based processes used so far.     

Sequential liquid-liquid extraction of d-amino acid oxidase from Trigonopsis variabilis

A method for isolation of d-amino acid oxidase (DAAO) from disrupted Trigonopsis variabilis cells has been developed. In an aqueous two-phase system consisting of PEG6000 (220 g l^–1), potassium phosphate (110 g l^–1, K₂HPO₄ + KH₂PO₄ = 10.1:1, mol mol^–1) and dl-methionine (11 g l^–1), the major portion of cellular proteins (87%) was partitioned into the salt phase. By sequential extraction, 48% of DAAO was recovered in PEG phase, giving a yield of 211 U mg protein^–1.     

Biological acidification during grape must fermentation using mixed cultures of <Emphasis Type="Italic">Kluyveromyces thermotolerans</Emphasis> and <Emphasis Type="Italic">Saccharomyces cerevisiae</Emphasis>

Four mixed culture fermentations of grape must were carried out with Kluyveromyces thermotolerans strain TH941 and Saccharomyces cerevisiae strain SCM952. In the first culture, both yeasts were added together, whereas in the remaining three cultures S. cerevisiae was added 1, 2, and 3 days after the inoculation of K. thermotolerans. The growth and survival of the K. thermotolerans strain and the amount of the produced l-lactic acid depend on the time of inoculation of the S. cerevisiae strain and provided an effective acidification during alcoholic fermentation. The four cultures contained, respectively, at the end of fermentation 0.18, 1.80, 4.28, and 5.13 g l-lactic acid l⁻¹. The grape must with an initial pH of 3.50 was effectively acidified (70% increase in titratable acidity, 0.30 pH unit decrease) by the production of 5.13 g l-lactic acid l⁻¹.     

Evaluation ofl-lactic acid production in batch, fed-batch, and continuous cultures ofRhizopus sp. MK-96-1196 using an airlift bioreactor

Various processes which producel-lactic acid using ammonia-tolerant mutant strain,Rhizopus sp. MK-96-1196, in a 3 L airlift bioreactor were evaluated. When the fed-batch culture was carried out by keeping the glucose concentration at 30 g/l, more than 140 g/l ofl-lactic acid was produced with a product yield of 83%. In the case of the batch culture with 200 g/l of initial glucose concentration, 121 g/L ofl-lactic acid was obtained but the low product yield based on the amount of glucose consumed. In the case of a continuous culture, 1.5 g/l/h of the volumetric productivity with a product yield of 71% was achieved at dilution rate of 0.024 h⁻¹. Basis on these results three processes were evaluated by simple variable cost estimation including carbon source, steam, and waste treatment costs. The total variable costs of the fed-batch and continuous cultures were 88% and 140%, respectively, compared to that of batch culture. The fed-batch culture with highl-lactic acid concentration and high product yield decreased variable costs, and was the best-suited for the industrial production ofl-lactic acid.     

Production of <Emphasis Type="SmallCaps">d</Emphasis>-lactic acid from sugarcane molasses,sugarcane juice and sugar beet juice by <Emphasis Type="Italic">Lactobacillus delbrueckii</Emphasis>

Lactobacillus delbrueckii was grown on sugarcane molasses, sugarcane juice and sugar beet juice in batch fermentation at pH 6 and at 40°C. After 72 h, the lactic acid from 13% (w/v) sugarcane molasses (119 g total sugar l⁻¹) and sugarcane juice (133 g total sugar l⁻¹) was 107 g l⁻¹ and 120 g l⁻¹, respectively. With 10% (w/v) sugar beet juice (105 g total sugar l⁻¹), 84 g lactic acid l⁻¹ was produced. The optical purities of d-lactic acid from the feedstocks ranged from 97.2 to 98.3%.     

Production of <Emphasis Type="SmallCaps">l</Emphasis>-lactic acid by <Emphasis Type="Italic">Rhizopus oryzae</Emphasis> using semicontinuous fermentation in bioreactor

Semicontinuous fermentation using pellets of Rhizopus oryzae has been recognized as a promising technology for l-lactic acid production. In this work, semicontinuous fermentation of R. oryzae AS 3.819 for l-lactic acid production has been developed with high l-lactic acid yield and volumetric productivity. The effects of factors such as inoculations, CaCO₃ addition time, and temperature on l-lactic acid yield and R. oryzae morphology were researched in detail. The results showed that optimal fermentation conditions for the first cycle were: inoculation with 4% spore suspension, CaCO₃ added to the culture medium at the beginning of culture, and culture temperature of 32–34°C. In orthogonal experiments, high l-lactic acid yield was achieved when the feeding medium was (g/l): glucose, 100; (NH₄)₂SO₄, 2; KH₂PO₄, 0.1; ZnSO₄·7H₂O, 0.33; MgSO₄·7H₂O, 0.15; CaCO₃, 50. Twenty cycles of semicontinuous fermentation were carried out in flask culture. l-lactic acid yield was 78.75% for the first cycle and 80–90% for the repeated cycles; the activities of lactate dehydrogenases (LDH) were 7.2–9.2 U/mg; fermentation was completed in 24 h for each repeated cycle. In a 7-l magnetically stirred fermentor, semicontinuous fermentation lasted for 25 cycles using pellets of R. oryzae AS 3.819 under the optimal conditions determined from flask cultures. The final l-lactic acid concentration (LLAC) reached 103.7 g/l, and the volumetric productivity was 2.16 g/(l·h) for the first cycle; in the following 19 repeated cycles, the final LLAC reached 81–95 g/l, and the volumetric productivities were 3.40–3.85 g/(l·h).     

Production of D(-)-lactic acid from cellulose by simultaneous saccharification and fermentation using Lactobacillus coryniformis subsp. torquens

D(–)-Lactic acid was produced from cellulose by simultaneous saccharification and fermentation (SSF) in media containing cellulolytic enzymes and Lactobacillus coryniformis subsp. torquens ATCC 25600 at 39 °C and pH 5.4, yielding 0.89 g D(–)-lactic acid g^–1 cellulose at a mean volumetric productivity of 0.5 g l^–1 h^–1. No L(+)-lactic acid was found in the medium.     

Selective production of bikaverin in a fluidized bioreactor with immobilized Gibberella fujikuroi

The best culture medium composition for the production of bikaverin by Gibberella fujikuroi in shake-flasks, i.e. 100 g glucose l^–1; 1 g NH₄Cl l^–1; 2 g rice flour l^–1; 5 g KH₂PO₄ l^–1 and 2.5 g MgSO₄ l^–1, was obtained through a fractional factorial design and then scaled-up to a fluidized bioreactor. The effects of carbon and nitrogen concentrations, inoculum size, aeration, flow rate and bead sizes on batch bikaverin production using immobilized G. fujikuroi in a fluidized bioreactor were determined by an orthogonal experimental design. Concentrations of up to 6.83 g bikaverin l^–1 were obtained when the medium contained 100 g glucose l^–1 and 1 g NH₄Cl l^–1 with an inoculum ratio of 10% v/v, an aeration rate of 3 volumes of air per volume of medium min^–1, and a bead size of 3 mm. Based on dry weight, the bikaverin production was 30–100 times larger than found in submerged culture and approximately three times larger than reported for solid substrate fermentation.     

Production of <Emphasis Type="SmallCaps">d</Emphasis>-lactic acid by <Emphasis Type="Italic">Corynebacterium glutamicum</Emphasis> under oxygen deprivation

In mineral salts medium under oxygen deprivation, Corynebacterium glutamicum exhibits high productivity of l-lactic acid accompanied with succinic and acetic acids. In taking advantage of this elevated productivity, C. glutamicum was genetically modified to produce d-lactic acid. The modification involved expression of fermentative d-lactate dehydrogenase (d-LDH)-encoding genes from Escherichia coli and Lactobacillus delbrueckii in l-lactate dehydrogenase (l-LDH)-encoding ldhA-null C. glutamicum mutants to yield strains C. glutamicum ΔldhA/pCRB201 and C. glutamicum ΔldhA/pCRB204, respectively. The productivity of C. glutamicum ΔldhA/pCRB204 was fivefold higher than that of C. glutamicum ΔldhA/pCRB201. By using C. glutamicum ΔldhA/pCRB204 cells packed to a high density in mineral salts medium, up to 1,336 mM (120 g l⁻¹) of d-lactic acid of greater than 99.9% optical purity was produced within 30 h.     

Biosynthesis of indole-3-acetic acid in tomato shoots: Measurement,mass-spectral identification and incorporation of −2H from −2H2O into indole-3-acetic acid,d- and l-tryptophan,indole-3-pyruvate and tryptamine

Indole-3-acetic acid (IAA) and its putative precursors, l- and d-tryptophan, indole-3-pyruvate, and tryptamine were isolated from tomato (Lycopersicon esculentum (L.) Mill.) shoots, identified by mass spectrometry, and measured using capillary gas chromatography with an electron capture detector and radioactive internal standards. Average amounts present were 7.9ng · (g FW)^–-1 IAA, 5.7ng · (g FW)^–-1 indole-3-pyruvate, 132 ng · (g FW)^–-1 tryptamine, 103 ng · (g FW)^–-1 d-tryptophan, and 2250 ng · (g FW)^–-1 l-tryptophan. Indole-3-acetaldoxime was not found; detection limits were less than 1ng · (g FW)^–-1. When tomato shoots were incubated for 6, 10 and 21 h in 30% ^–2H₂O, up to four positions in IAA, l- and d-tryptophan, tryptamine and indole-3-pyruvate became labelled with ^–2H. Compounds became labelled rapidly with 10% of IAA molecules containing ^–2H after 6 h. The percentage of labelled molecules of IAA and l-tryptophan increased up to 10 h but then decreased again, correlating with an increase in the total shoot tryptophan and presumably a result of protein hydrolysis in the excised, slowly senescing tissue. The amount of ^–2H in d-tryptophan also showed an increase followed by a decrease, but the proportion of labelled molecules was much less than in l-tryptophan and IAA. Tryptamine became labelled initially at a similar rate to IAA but continued to accumulate ^–2H up to 21 h. We conclude that tryptamine is synthesized from a different pool of tryptophan from that used in IAA synthesis, and is not a major endogenous precursor of IAA in tomato shoots. Indole-3-pyruvate was the most heavily labelled compound after 6 and 10 h incubation (21-h data not available). Furthermore, the proportion of ^–2H-labelled indole-3-pyruvate molecules was quantitatively consistent with the amount of label in IAA. On the other hand, a quantitative comparison of the IAA turnover rate and the rate of ^–2H incorporation into both l- and d-tryptophan indicates that IAA is not made from the total shoot pool of either l- or d-tryptophan. Instead IAA appears to be synthesized from a restricted pool which is turning over rapidly and which has access to both newly synthesized tryptophan and that from protein hydrolysis.Abbreviations GC-ecd gas chromatography with electroncapture detector - GC-MS combined gas chromatography-mass spectrometry - HPLC high-performance liquid chromatography - IAA indole-3-acetic acid - IAOX indole-3-acetaldoxime - IPyA indole-3-pyruvate - PFB pentafluorobenzyl - R_T retention time - TNH₂ tryptamine - Trp tryptophan - SIM selected ion monitoring We wish to thank Ms. Sue Alford for running the mass spectra and Dr Harry Young for advice with the mass spectrometry. The work was supported by grants from the University of Auckland Research Committee and the C. Alma Baker Trust fund. The mass spectrometer was supported jointly by the University Grants Commitee (NZ) and the DSIR Division of Horticulture and Processing.     

Biotransformation of oleic acid into 10-hydroxy-8E-octadecenoic acid by Pseudomonas sp. 42A2

Pseudomonas sp. 42A2 when incubated for 36 h with oleic acid (20 g l^–1) in a stirred bioreactor, accumulated 10-hydroxy-8E-octadecenoic acid. Production in a 2 l bioreactor with 1.4 l of working volume, was increased from 0.65 g l^–1 to 7.4 g l^–1 with K _L a values ranging between 15 and 200 h^–1. A linear relationship was found between volumetric productivity and oxygen transfer rates and an exponential relation between the specific rate of product formation and specific growth rate.     

Production of l-lactic acid by Rhizopus species

Of 19 Rhizopus spp. only four produced l-lactic acid in shake-flask culture. Aerobically and in the presence of a neutralizing agent, Rhizopus oryzae NRRL 395 produced the highest concentration of l-lactic acid (65 g/l) but with O₂-limited growth ethanol was produced instead.C.R. Soccol and V.I. Stonoga are with the Laboratório de Processos Biotecnológicos, Departmento de Engenharia Química da Universidade Federal do Paraná, 81531-970 Curitiba, PR, Brazil; M. Raimbault is with the Centre ORSTOM, Laboratoire de Biotecnologie, Physiologie et Métabolisme Cellulaires, 911, Avenue Agropolis, 34032 Montpellier, Cedex 1, France.     

Therlt11 andraec1 mutants ofArabidopsis thaliana lack the activity of a basic-amino-acid transporter

The concentration dependence of the influx ofl-lysine in excised roots ofArabidopsis thaliana seedlings was analyzed for the wild-type (WT) and two mutants,rlt11 andraec1, which had been selected as resistant to lysine plus threonine, and to S-2-aminoethyl-l-cysteine, respectively. In the WT three components were resolved: (i) a high-affinity, low-capacity component [K _m = 2.2 M;V _max = 23 nmol·(g FW)^–1·h^–1]; (ii) a low-affinity, high-capacity component [K _m = 159 M;V _max = 742 nmol·(g FW)^–1·h^–1]; (iii) a component which is proportional to the external concentration, with a constant of proportionalityk = 104 nmol·(g FW)^–1 h^–1];·mM^–1. The influx ofl-lysine in the mutants was lower than in the WT, notably in the concentration range 0.1–0.4 mM, where it was only 7% of that in the WT. In both mutants the reduced influx could be fully attributed to the absence of the low-affinity (high-K _m ) component. This component most likely represents the activity of a specific basic-amino-acid transporter, since it was inhibited by several other basic amino acids (arginine, ornithine, hydroxylysine, aminoethylcysteine) but not byl-valine. The high-affinity uptake ofl-lysine may be due to the activity of at least two general amino acid transporters, as it was inhibitable byl-valine, and could be further dissected into two components with a high affinity (K _i = 1–5 M; and a low affinity (K _i = 0.5–1mM) forl-valine, respectively. Therlt11 andraecl mutant have the same phenotype and the corresponding loci were mapped on chromosome 1, but it is not yet clear whether they are allelic.Abbreviations AEC S-2-aminoethyl-l-cysteine - K _i equilibrium constant - WT wild-type     

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

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

Introduction of a stress-responsive gene, yggG, enhances the yield of l-phenylalanine with decreased acetic acid production in a recombinant Escherichia coli

A stress-responsive gene, yggG, was introduced into an l-phenylalanine producer, Escherichia coli AJ12741. In shake-flask culture, the yggG-containing recombinant strain (named AJ12741/pHYGG) produced 6.4 g l-phenylalanine l⁻¹ at the end of culture and its yield on glucose was 0.16 g l-phenylalanine g glucose⁻¹. These values are much higher than those of the original AJ12741 strain (3.7 g l-phenylalanine l⁻¹ and 0.09 g l-phenylalanine g glucose⁻¹, respectively). On the other hand, AJ12741/pHYGG strain produced only 4.5 g acetic acid l⁻¹ and its yield on glucose was about a half of that of the AJ12741 culture. Analysis of gene expression revealed that in late growth phase, the expression levels of genes involved in acetic acid production (pta, ackA, and poxB) were relatively low in AJ12741/pHYGG cells. In particular, the level of poxB expression in AJ12741/pHYGG strains was one-seventh of that of the original strain. These results suggest that the formation of a bottleneck for acetic acid production brings about a metabolic flow favorable to l-phenylalanine synthesis in the recombinant strain over-expressing the yggG gene. Electronic supplementary material  The online version of this article (doi:) contains supplementary material, which is available to authorized users.     

Application of statistically-based experimental designs for the optimization of nisin production from whey

Statistically-based experimental designs were applied for the optimization of nisin production by Lactococcus lactis in a whey-based medium. Yeast extract, KH₂PO₄, and MgSO₄ were identified to have significant effects on nisin biosynthesis by a Plackett–Burman design. These three significant factors were subsequently optimized using central composite design, and the optimal conditions were determined to be 12.067 g l^–1 for yeast extract, 0.569 g l^–1 for KH₂PO₄, and 0.572 g l^–1 for MgSO₄. The validity of the optimal conditions was verified by a separate experiment.     

Living cell reaction process forl-isoleucine andl-valine production

Summary A new process (Living Cell Reaction Process) forl-isoleucine production using viable, non-growing cells ofBrevibacterium flavum AB-07 was optimised using ethanol as the energy source and -ketobutyric acid (-KB) as precursor.l-valine also could be produced from glucose at high yield by this process. This process differs from the usual fermentation method in that non-growing cells are used, and the production ofl-isoleucine andl-valine were carried out under conditions of repressed cell division and growth. Minimal medium missing the essential growth factor, biotin was employed as the reaction mixture for the production ofl-isoleucine andl-valine. The productivity ofl-isoleucine andl-valine were 200 mmol·l^–1 · day^–1 (molecular yield to -KB: 95%) and 300 mmol · l^–1 · day^–1 (molecular yield to glucose: 80%) respectively. The content ofl-isoleucine andl-valine in total amino acids produced in the each mixture were 97% and 96% respectively.     

Improvement of glycerol production by Candida krusei in batch and continuous cultures using corn steep liquor

No fermentation parameter was affected at phosphate concentration above 0.4 g l^–1 when KH₂PO₄ was used as phosphate source and the glucose consumption rate was difficult to control when corn steep liquor (CSL) was adopted as the phosphate source. However, if CSL was supplemented as a source of growth factors instead of as the phosphate source, not only glucose uptake and glycerol was improved, but also fermentation became easy to control and a steady state of continuous culture was easily obtained.     

Application of response surface methodology in medium optimization for spore production of <Emphasis Type="Italic">Coniothyrium minitans</Emphasis> in solid-state fermentation

Summary Spore production of Coniothyrium minitans was optimized by using response surface methodology (RSM), which is a powerful mathematical approach widely applied in the optimization of fermentation process. In the first step of optimization, with Plackett–Burman design, soluble starch, urea and KH²PO⁴ were found to be the important factors affecting C. minitans spore production significantly. In the second step, a 2³ full factorial central composite design and RSM were applied to determine the optimal concentration of each significant variable. A second-order polynomial was determined by the multiple regression analysis of the experimental data. The optimum values for the critical components for the maximum were obtained as follows: soluble starch 0.643 (36.43 g. l⁻¹), urea −0.544 (3.91 g l⁻¹) and KH²PO⁴ 0.049 (1.02 g l⁻¹) with a predicted value of maximum spore production of 9.94 × 10⁹ spores/g IDM. Under the optimal conditions, the practical spore production was 1.04 × 10¹⁰ spores/g IDM. The determination coefficient (R²) was 0.923, which ensure an adequate credibility of the model.