Synthesis of l-dopa by escherichia intermedia cells immobilized in a polyacrylamide gel

Summary Escherichia intermedia cells were immobilized by entrapment in a polyacrylamide gel and used for l-dopa synthesis from pyrocatechol, pyruvate and ammonia. An immobilized cell preparation containing 75 mg cells/g gel retained 45%–50% of the activity of free cells. The effect of temperature, pH and substrate concentration of the initial rate of l-dopa synthesis was very similar for free and immobilized cells. Substrate inhibition was observed for pyrocatechol, pyruvate and ammonia. In a batch reactor, 5.4 g·l^-1 l-dopa was obtained, with 100% conversion yield of pyrocatechol and l-dopa productivity of 0.18 g·l^-1·h^-1. The use of a pyrocatechol-borate complex decreased by-product formation and catalyst inactivation.     

Immobilized cells cultivated in semi-continuous mode in a fluidized bed reactor for xylitol production from sugarcane bagasse

Summary Xylitol production from sugarcane bagasse hemicellulosic hydrolyzate was evaluated in a fluidized bed reactor operated in semi-continuous mode, using cells immobilized on porous glass. The fermentative process was performed during five successive cycles of 72 h each one. The lowest xylitol production occurred in the first cycle, where a high cell concentration (12 g l⁻¹) was observed. In the subsequent cycles the xylitol concentration was ever increasing due to the cells adaptation to the medium. In the last one, 18 g xylitol l⁻¹ was obtained with a yield factor of 0.44 g g⁻¹ and volumetric productivity of 0.32 g l⁻¹ h⁻¹.     

High-level production of arachidonic acid by fed-batch culture of <Emphasis Type="Italic"> Mortierella alpina</Emphasis> using NH<Subscript>4</Subscript>OH as a nitrogen source and pH control

Mortierella alpina was grown in a fed-batch culture using a 12-l jar fermenter with an initial 8-l working volume containing 20 g glucose l⁻¹ and 10 g corn-steep powder l⁻¹. Glucose was intermittently fed to give 32 g l⁻¹ at each time. The pH of culture was maintained using 14% (v/v) NH₄OH, which also acted as a nitrogen source. A final cell density of 72.5 g l⁻¹ was reached after 12.5 days with a content of arachidonic acid (ARA) at 18.8 g l⁻¹. These values were 4 and 1.8 times higher than the respective values in batch culture. Our results suggest that the combined feeding of glucose and NH₄⁺ to the growth of M. alpina could be applied for the industrial scale production of ARA.     

Degradation kinetics of phenol by immobilized cells of Candida tropicalis in a fluidized bed reactor

Degradation kinetics of phenol by free and agar-entrapped cells of Candida tropicalis was studied in batch cultures. The initial phenol degradation rate achieved with free cells was higher than that obtained with immobilized cells, when phenol concentrations up to 1000 mg l^–1 were used. However, at higher phenol concentrations, the behaviour was quite different. The initial degradation rate of the immobilized yeast cells was about 10 times higher than that of the free cells, at a phenol concentration of 3500 mg l^–1. The semicontinuous and continuous degradation of phenol by immobilized yeast cells was also investigated in a multi-stage fluidized bed reactor. The highest phenol removal efficiencies and degradation rates as well as the lowest values of residual phenol and chemical oxygen demand were obtained in the semicontinuous culture when phenol concentrations up to 1560 mg l^–1 were used.     

Optimization of lactic acid production by immobilized <Emphasis Type="Italic">Lactococcus lactis</Emphasis> IO-1

Production of lactic acid from glucose by immobilized cells of Lactococcus lactis IO-1 was investigated using cells that had been immobilized by either entrapment in beads of alginate or encapsulation in microcapsules of alginate membrane. The fermentation process was optimized in shake flasks using the Taguchi method and then further assessed in a production bioreactor. The bioreactor consisted of a packed bed of immobilized cells and its operation involved recycling of the broth through the bed. Both batch and continuous modes of operation of the reactor were investigated. Microencapsulation proved to be the better method of immobilization. For microencapsulated cells at immobilized cell concentration of 5.3 g l⁻¹, the optimal production medium had the following initial concentrations of nutrients (g l⁻¹): glucose 45, yeast extract 10, beef extract 10, peptone 7.5 and calcium chloride 10 at an initial pH of 6.85. Under these conditions, at 37 °C, the volumetric productivity of lactic acid in shake flasks was 1.8 g l⁻¹ h⁻¹. Use of a packed bed of encapsulated cells with recycle of the broth through the bed, increased the volumetric productivity to 4.5 g l⁻¹ h⁻¹. The packed bed could be used in repeated batch runs to produce lactic acid.     

Synthesis of l-tyrosine by immobilized Escherichia intermedia cells

Summary Cells of Escherichia intermedia were immobilized by entrapment in a polyacrylamide gel and used for the enzymatic production of l-tyrosine from phenol, pyruvate, and ammonia. A preparation containing 50 mg of cells/g of gel retained 60% of its original activity. The effect of temperature, pH and substrate concentration on the activity of free cells was almost identical with the effect on immobilized cells. Phenol showed inhibition and inactivation of the catalyst at high concentration. Synthesis of l-tyrosine (up to 10 g/l) was demonstrated in batch reactors with high conversion yields (95–100%) and a maximal productivity of 2 g/l/h. In continuous reactor the catalyst showed a very high operational stability (more than 54 days without losses).     

Production of α-tocopherol by sequential heterotrophic–photoautotrophic cultivation of Euglena gracilis

Photoautotrophic cultivation of Euglena gracilis results in cells with high α-tocopherol content but the final cell concentration is usually very low due to the difficulty of supplying light efficiently to the photobioreactor. On the other hand, Euglena grows heterotrophically to high cell concentrations, using various organic carbon sources, but the α-tocopherol contents of heterotrophically grown cells are usually very low. Sequential heterotrophic/photoautotrophic cultivation, by which cells are grown heterotrophically to high cell concentrations and then transferred to photoautotrophic culture for accumulation of α-tocopherol was therefore investigated for efficient α-tocopherol production. In batch culture, using glucose as the organic carbon source, the cellular α-tocopherol content increased from 120 μg g⁻¹ at the end of heterotrophic phase to more than 400 μg g⁻¹ at the end of the photoautotrophic phase. By using ethanol as the organic carbon source during the heterotrophic phase, adding corn steep liquor as a nitrogen source and optimizing light supply during the photoautotrophic phase, the α-tocopherol content of the cells at the end of the photoautotrophic phase increased to 1700 μg g⁻¹. A system consisting of a mini-jar fermentor (for the heterotrophic phase) and an internally illuminated photobioreactor (for the photoautotrophic phase) was then constructed for continuous sequential heterotrophic/photoautotrophic cultivation. The cells were continuously cultivated heterotrophically in the mini-jar fermentor and the effluent was continuously passed through the photobioreactor for α-tocopherol accumulation. In this way, it was possible to produce 7 g l⁻¹ cells containing about 1100 μg α-tocopherol per g-cell continuously for more than 420 h. The continuous process resulted in α-tocopherol productivity of 100 μg l⁻¹ h⁻¹ which is about 9.5 and 4.6 times higher than those obtained in batch photoautotrophic culture and batch heterotrophic cultures, respectively.     

Biodegradation of pyridine by freely suspended and immobilized Pimelobacter sp.

Freely suspended and Ca-alginate-immobilized cells of Pimelobacter sp. were used for degradation of pyridine. When the pyridine concentration was up to 2 g l^–1, freely suspended cells completely degraded pyridine regardless of the initial cell concentrations used. However, when the pyridine concentration increased to 4 g l^–1, the initial cell concentration in freely suspended cell culture should be higher than 1.5 g dry cell weight l^–1 for complete degradation of pyridine. In addition, a freely suspended cell culture with a high initial cell concentration resulted in a high volumetric pyridine-degradation rate, suggesting the potential use of immobilized cells for pyridine-degradation. When the immobilized cells were used for pyridine-degradation, neither specific pyridine-degradation rate nor tolerance against pyridine was improved. However, a high volumetric pyridine-degradation rate in the range 0.082–0.129 g l^–1 hr^–1 could be achieved by the immobilized cells because of the high cell concentration. Furthermore, when the immobilized cells were reused in degrading pyridine at a concentration of 2–4 g l^–1 they did not lose their pyridine-degrading activity for 2 weeks. Taken together, the data obtained here showed the feasibility of using immobilized cells for pyridine-degradation.     

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.     

Fermentation of xylose and rice straw hydrolysate to ethanol byCandida shehatae NCL-3501

Candida shehatae NCL-3501 utilized glucose and xylose efficiently in batch cultures. The specific rate of ethanol production was higher with mixtures of glucose and xylose (0.64–0.83 g g^–1 cells d^–1) compared to that with individual sugars (0.38–0.58 g g^–1 cells d^–1). Although the optimum temperature for growth was 30°C, this strain grew and produced appreciable levels of ethanol at 45°C. A stable ethanol yield (0.40–0.43 g g^–1 substrate utilized) was obtained between 10 g L^–1 and 80 g L^–1 of initial xylose concentration. Conversion efficiency was further improved by immobilization of the cells in calcium alginate beads. Free or immobilized cells ofC. shehatae NCL-3501 efficiently utilized sugars present in rice straw hemicellulose hydrolysate, prepared by two different methods, within 48 h. Ethanol yields of 0.45 g g^–1 and 0.5 g g^–1 from autohydrolysate, and 0.37 g g^–1 from acid hydrolysate were produced by free and immobilized cells, respectively.     

β-Galactosidase from Talaromyces thermophilus immobilized on to Eupergit C for production of galacto-oligosaccharides during lactose hydrolysis in batch and packed-bed reactor

The β-galactosidase from Talaromyces thermophilus CBS 236.58 immobilized onto Eupergit C produced galacto-oligosaccharides (GalOS) in batchwise and continuous packed-bed mode of operation. A maximum yield of GalOS of 12, 39 and 80 g l⁻¹ was obtained for initial lactose concentrations of 50, 100 and 200 g l⁻¹, respectively, for batch conversion experiments. The immobilized enzyme could be re-used for several cycles for lactose hydrolysis and transformation. The maximum GalOS concentration of approximately 50 g l⁻¹ was obtained with the dilution rate of 0.375 h⁻¹ in a packed-bed reactor, when using an initial lactose concentration of 200 g l⁻¹. Continuous conversion of lactose in the packed-bed reactor resulted in the formation of relatively more trisaccharides than when employing the immobilized enzyme in discontinuous mode of operation.     

Enhancement of inosine production by <Emphasis Type="BoldItalic">Bacillus subtilis</Emphasis> through suppression of carbon overflow by sodium citrate

Sodium citrate, added to culture medium at 2 g l⁻¹, increased inosine production by B. subtilis by 18% to 16 g l⁻¹. The phosphoenolpyruvate (PEP) pool was increased by 2.3-fold, while the pyruvate and acetate pools were decreased by 78% and 57%, respectively. Pyruvate kinase might thus be a regulatory site for inosine synthesis.     

Degradation of caffeine by immobilized cells of Pseudomonas putida strain C 3024

Summary A caffeine-resistant strain of Pseudomonas putida was isolated from soil and was grown with caffeine as the sole source of carbon, energy and nitrogen. Cells were immobilized in agar gel particles which were continuously supplied with a caffeine solution (0.52 g · l^–1, D=1.0 h^–1) in a homogeneously mixed aerated reaction vessel. In the presence of the ATPase inhibitor arsenate the caffeine was removed by the immobilized cells at an average rate of 0.25 mg caffeine · h^–1 · (mg cell carbon)^–1 during 6 days. Thereafter a rapid decline of activity was observed. From a similar system without arsenate supplied with a growth medium containing a limiting amount of caffeine (0.13 g · l^–1) the caffeine was almost completely oxidized by the immobilized cells. The concentration of the remaining caffeine was 1.4 mg · l^–1, which is much lower than the substrate constant for caffeine (9.7 mg · l^–1) observed with freshly harvested suspended resting cells.     

Production of citric acid with immobilized Yarrowia lipolytica

Summary Citric acid was produced with immobilized Yarrowia lipolytica yeast in repeated batch-shake-flask and air-lift fermentations. In active and passive immobilization methods calcium alginate, -carrageenan, polyurethane gel, nylon web and polyurethane foams were tested as carriers in repeated-batch fermentations. The highest citric acid productivity of 155 mg l^–1 h^–1 was reached with alginate-bead-immobilized cells in the first batch. A decrease in bead diameter from 5–6 mm to 2–3 mm increased the volumetric citric acid productivity threefold. In an air-lift bioreactor the highest citric acid productivity of 120 mg l^–1 h^–1 with a product concentration of 16.4 g l^–1 was obtained with cells immobilized in -carrageenan beads. Offprint requests to: H. Kautola     

Transformation of arachidonic acid to 19-hydroxy- and 20-hydroxy-eicosatetraenoic acids using Candida bombicola

Candida bombicola (ATCC 22214) and C. apicola (ATCC 96134), grown on glucose (100 g l^–1) and arachidonic acid (5Z, 8Z, 11Z, 14Z-eicosatetraenoic acid; AA), 1.25 g l^–1, synthesized sophorolipid up to 0.93 g l^–1. Acid hydrolysis of sophorolipid yielded 19-hydroxy-5Z, 8Z, 11Z, 14Z-eicosatetraenoic acid (19-HETE) and 20-hydroxy-5Z, 8Z, 11Z, 14Z-eicosatetraenoic acid (20-HETE) which were identified by TLC and GC-MS; the ratio of synthesis was 73:27, respectively. Conversion of AA by immobilized Candida bombicola, suspended in beads of 2% (w/v) calcium alginate for 96 h, gave an 83% conversion of 1 g AA l^–1 to 19- and 20-HETE. There was no significant loss in the efficiency of the immobilized cells after ten uses.     

Asymmetric reduction of (<Emphasis Type="Italic">S</Emphasis>)-3-chloro-1-phenylpropanol from 3-chloropropiophenone by preheated immobilized <Emphasis Type="Italic">Candida</Emphasis> <Emphasis Type="Italic">utilis</Emphasis>

An efficient method for asymmetric reduction of (S)-3-chloro-1-phenylpropanol from 3-chloropropiophenone was developed using preheated Candida utilis cells immobilized in calcium alginate gel beads. Heating the immobilized cells (bead diameter 1.5 mm) at 45°C for 50 min allowed the reaction to proceed with 99.5% enantiomeric excess (ee) and an 85% yield with 1 g substrate l⁻¹ (batch addition in three aliquots) in 48 h. The immobilized cells retained approximately 50% of their original catalytic activity after being reused three times.     

Purification and properties of a novel raw starch degrading-cyclodextrin glycosyltransferase from Klebsiella pneumoniae AS- 22

A novel raw starch degrading α-cyclodextrin glycosyltransferase (CGTase; E.C. 2.4.1.19), produced by Klebsiella pneumoniae AS-22, was purified to homogeneity by ultrafiltration, affinity and gel filtration chromatography. The specific cyclization activity of the pure enzyme preparation was 523 U/mg of protein. No hydrolysis activity was detected when soluble starch was used as the substrate. The molecular weight of the pure protein was estimated to be 75 kDa with SDS-PAGE and gel filtration. The isoelectric point of the pure enzyme was 7.3. The enzyme was most active in the pH range 5.5–9.0 whereas it was most stable in the pH range 6–9. The CGTase was most active in the temperature range 35–50°C. This CGTase is inherently temperature labile and rapidly loses activity above 30°C. However, presence of soluble starch and calcium chloride improved the temperature stability of the enzyme up to 40°C. In presence of 30% (v/v) glycerol, this enzyme was almost 100% stable at 30°C for a month. The K_m and k_cat values for the pure enzyme were 1.35 mg ml⁻¹ and 249 μM mg⁻¹ min⁻¹, respectively, with soluble starch as the substrate. The enzyme predominantly produced α-cyclodextrin without addition of any complexing agents. The conditions employed for maximum α-cyclodextrin production were 100 g l⁻¹ gelatinized soluble starch or 125 g l⁻¹ raw wheat starch at an enzyme concentration of 10 U g⁻¹ of starch. The α:β:γ-cyclodextrins were produced in the ratios of 81:12:7 and 89:9:2 from gelatinized soluble starch and raw wheat starch, respectively.     

Multiple growth inhibition of <Emphasis Type="Italic">Klebsiella pneumoniae</Emphasis> in 1,3-propanediol fermentation

The inhibition of substrate and product on the growth of Klebsiella pneumoniae in anaerobic and aerobic batch fermentation for the production of 1,3-propanediol was studied. The cells under anaerobic conditions had a higher maximum specific growth rate of 0.19 h^–1 and lower tolerance to 110 g glycerol l^–1, compared to the maximum specific growth rate of 0.17 h^–1 and tolerance to 133 g glycerol l^–1 under aerobic conditions. Acetate was the main inhibitory metabolite during the fermentation under anaerobic conditions, with lactate and ethanol the next most inhibitory. The critical concentrations of acetate, lactate and ethanol were assessed to be 15, 19, 26 g l^–1, respectively. However, cells grown under aerobic conditions were more resistant to acetate and lactate but less resistant to ethanol. The critical concentrations of acetate, lactate and ethanol were assessed to be 24, 26, and 17 g l^–1, respectivelyRevisions requested 8 september; Revisions received 2 November 2004     

l-Malic acid formation by immobilized Saccharomyces cerevisiae amplified for fumarase

The yeast Saccharomyces cerevisiae was amplified for the enzyme fumarase by cloning the single nuclear gene downstream of a strong promoter. The overproducing strain converted fumaric acid to l-malic acid at a rate of 65 mM g⁻¹ h⁻¹ in free cell experiments, and approximately 87% of the fumaric acid was converted to l-malic acid within 45 min. Activity was dependent on the addition of surfactant to the medium, and minimal activity was seen with the wild-type yeast strain. The constructed strain was immobilized in agarose beads (2.4 mm mean diameter) and within agarose microspheres (193 and 871 μm mean diameter). The rate of bioconversion increased with decreasing bead diameter, with similar rates observed with the 193-μm diameter microspheres to that achieved with the free cells. The presence of surfactant was essential for initial activity of the immobilized cells; however, high activity was observed in subsequent experiments in the absence of surfactant. Stable activities over a 48-h period were maintained within the large-diameter agarose beads, while decreasing activities were observed within the agarose microspheres.     

Propionic acid production by immobilized cells of a propionate-tolerant strain of Propionibacterium acidipropionici

Cells of the propionate-tolerant strain Propionibacterium acidipropionici P200910, immobilized in calcium alginate beads, were tested for propionic and acetic acid production both in a semidefined laboratory medium and in corn steep liquor in batch, fed-batch, and continuous fermentation. Cell density was about 9.8 × 10⁹ cells/g (wet weight) of beads, and beads were added to the medium at 0.1 g (wet weight) beads/ml. Beads could be reused for several consecutive batch fermentations; propionic acid production in the tenth cycle was about 50%–70% of that in the first cycle. In batch culture complete substrate consumption (glucose in semidefined medium, lactate in corn steep liquor) and maximum acid production were seen within 36 h, and acid yields from the substrate were higher than in free-cell fermentations. Fed-batch fermentations were incubated up to 250 h. Maximum propionic acid concentrations obtained were 45.6 g/l in corn steep liquor and 57 g/l in semidefined medium; this is the highest concentration achieved to date in our laboratory. Maximum acetic acid concentrations were 17 g/l and 12 g/l, respectively. In continuous fermentation of semidefined medium, dilution rates up to 0.31 h^–1 could be used, which gave higher volumetric productivities (0.96 g l^–1 h^–1 for propionic acid and 0.26 g l^–1 h^–1 for acetic acid) than we have obtained with free cells. Corn steep liquor shows promise as an inexpensive medium for production of both acids by immobilized cells of propionibacteria.Journal paper no. J- 15614 of the Iowa Agriculture and Home Economics Experiment Station, Ames, Iowa. Project no. 3122