n-carbamoyl-d-p-hydroxyphenylglycine production using immobilized d-hydantoinase from recombinant E. coli

An immobilized d-hydantoinase was characterized and employed to produce n-carbamoyl-d-p-hydroxyphenylglycine (CpHPG) in a repeated batch process. The V_max and K_m of the immobilized d-hydantoinase at 50°C were 6.28 mm min⁻¹ g⁻¹ biocatalyst and 71.6 mm, respectively. The product CpHPG did not inhibit the activity of d-hydantoinase. Optimal reaction temperature was 60°C. A decrease in activity of immobilized d-hydantoinase due to thermal inactivation could be described as first-order decay; the deactivation energy was 23.97Kcal mol⁻¹. Under process conditions (50°C, 10% w/v substrate, and pH 8.5), the half-life of the immobilized d-hydantoinase was eight batches. The attrition of immobilized d-hydantoinase particles with a large amount of insoluble substrate particles during stirring resulted in fine biocatalyst particles. In addition to the thermal inactivation, the loss of fine biocatalyst particles during the recovery step contributed to the low operational stability.     

Design of a noncovalently linked bifunctional enzyme for whole-cell biotransformation

Optical pure d-p-hydroxyphenylglycine (d-HPG) is a precursor for semi-synthetic antibiotics. It can be synthesized from d,l-hydroxyphenyl hydantoin (HPH) by a two-step reaction mediated by d-hydantoinase (HDT) and amidohydrolase (AHL). In this study, a bifunctional enzyme was originally created by in-frame fusion of AHL with HDT genes (AHL-HDT). However, the AHL-HDT fusion protein expressed in Escherichia coli was prone to aggregates, recognized as a frequently encountered problem for this conventional method. To address this issue, small interacting motifs, cohesin (Coh) and dockerin (Doc) domains of cellulosomes, were explored and illustrated to interact in vivo. Accordingly, Coh and Doc were fused with AHL and HDT, respectively. After co-expression in E. coli, Coh-tagged AHL and Doc-tagged HDT assembled into a soluble protein complex via the high-affinity interaction of Coh and Doc. Consequently, the protein assembly exhibited both AHL and HDT activities and a higher reaction rate than free counterparts. Whole cells expressing the protein assembly were more stable than ones with free proteins for d-HPG production, and they could be recycled six times with a conversion yield of d-HPG exceeding 90%.     

Biooxidation of ferrous iron by immobilized Acidithiobacillus ferrooxidans in poly(vinyl alcohol) cryogel carriers

PVA-cryogels entrapping about 10⁹ cells of Acidithiobacillus ferrooxidans per ml of gel were prepared by freezing-thawing procedure, and the biooxidation of Fe²⁺ by immobilized cells was investigated in a 0.365 l packed-bed bioreactor. Fe²⁺ oxidation fits a plug-flow reaction model well. A maximum oxidation rate of 3.1 g Fe²⁺ l^–1 h^–1 was achieved at the dilution rate of 0.4 h^–1 or higher, while no obvious precipitate was determined at this time. In addition, cell-immobilized PVA-cryogels packed in bioreactor maintained their oxidative ability for more than two months under non-sterile conditions. Nomenclature: C _A0 – Concentration of Fe²⁺ in feed stream (g l^–1) C _A – Concentration of Fe^{2 +} in outlet stream (g l^{– 1}) D – Dilution rate of the packed-bed bioreactor (h^–1) F – Volumetric flow rate of iron solution (l h^–1) F _A0 – Mass flow rate of Fe²⁺ in the feed stream (g h^–1) K – Kinetic constant (l l^–1 h^–1) r _A – Oxidation rate of Fe²⁺ (g l^–1 h^–1) V – Volume of packed-bed bioreactor (l) X _A – Conversion ratio of Fe²⁺ (%)     

Biofiltration of waste gases with the fungi Exophiala oligosperma and Paecilomyces variotii

Two biofilters fed toluene-polluted air were inoculated with new fungal isolates of either Exophiala oligosperma or Paecilomyces variotii, while a third bioreactor was inoculated with a defined consortium composed of both fungi and a co-culture of a Pseudomonas strain and a Bacillus strain. Elimination capacities of 77 g m^–3 h^–1 and 55 g m^–3 h^–1 were reached in the fungal biofilters (with removal efficiencies exceeding 99%) in the case of, respectively, E. oligosperma and Paecilomyces variotii when feeding air with a relative humidity (RH) of 85%. The inoculated fungal strains remained the single dominant populations throughout the experiment. Conversely, in the biofilter inoculated with the bacterial–fungal consortium, the bacteria were gradually overgrown by the fungi, reaching a maximum elimination capacity around 77 g m^–3 h^–1. Determination of carbon dioxide concentrations both in batch assays and in biofiltration studies suggested the near complete mineralization of toluene. The non-linear toluene removal along the height of the biofilters resulted in local elimination capacities of up to 170 g m^–3 h^–1 and 94 g m^–3 h^–1 in the reactors inoculated, respectively, with E. oligosperma and P. variotii. Further studies with the most efficient strain, E. oligosperma, showed that the performance was highly dependent on the RH of the air and the pH of the nutrient solution. At a constant 85% RH, the maximum elimination capacity either dropped to 48.7 g m^–3 h^–1 or increased to 95.6 g m^–3 h^–1, respectively, when modifying the pH of the nutrient solution from 5.9 to either 4.5 or 7.5. The optimal conditions were 100% RH and pH 7.5, which allowed a maximum elimination capacity of 164.4 g m^–3 h^–1 under steady-state conditions, with near-complete toluene degradation.     

Simultaneous removal of benzene, toluene and xylenes mixture by a constructed microbial consortium during biofiltration

A bacterial consortium with complementary metabolic capabilities was formulated and specific removal rates were 0.14, 0.35, 0.04, and 0.39 h^–1 for benzene, toluene, o-xylene, and m,p-xylene, respectively. When immobilized on a porous peat moss biofilter, removal of all five (= BTX) components was observed with rates of 1.8–15.4 g m^–3 filter bed h^–1. Elimination capacities with respect to the inlet gas concentrations of BTX and airflow rates showed diffusive regimes in the tested concentration range of (0.1–5.3 g m^–3) and airflow (0.55–1.82 m³ m^–2 h^–1) except for o-xylene which reached its critical gas concentration at 0.3 g m^–3.     

Continuous ethanol production byZymomonas mobilis andSaccharomyces cerevisiae in biofilm reactors

Continuous ethanol fermentations were performed in duplicate for 60 days withZymomonas mobilis ATCC 331821 orSaccharomyces cerevisiae ATCC 24859 in packed-bed reactors with polypropylene or plastic composite-supports. The plastic composite-supports used contained polypropylene (75%) with ground soybean-hulls (20%) and zein (5%) forZ. mobilis, or with ground soybean-hulls (20%) and soybean flour (5%) forS. cerevisiae. Maximum ethanol productivities of 536 gL^–1 h^–1 (39% yield) and 499 gL^–1 h^–1 (37% yield) were obtained withZ. mobilis on polypropylene and plastic composite-supports of soybean hull-zein, respectively. ForZ. mobilis, and optimal yield of 50% was observed at a 1.92h^–1 dilution rate for soybean hull-zein plastic composite-supports with a productivity of 96gL^–1h^–1, whereas with polypropylene-supports the yield was 32% and the productivity was 60gL^–1h^–1. With aS. cerevisiae fermentation, the ethanol production was less, with a maximum productivity of 76gL^–1h^–1 on the plastic composite-support at a 2.88h^–1 dilution rate with a 45% yield. Polypropylene-support bioreactors were discontinued due to reactor plugging by the cell mass accumulation. Support shape (3-mm chips) was responsible for bioreactor plugging due to extensive biofilm development on the plastic composite-supports. With suspensionculture continuous fermentations in continuously-stirred benchtop fermentors, maximum productivities of 5gL^–1h^–1 were obtained with a yield of 24 and 26% withS. cerevisiae andZ. mobilis, respectively. Cell washout in suspensionculture continuous fermentations was observed at a 1.0h^–1 dilution rate. Therefore, for continuous ethanol fermentations, biofilm reactors out-performed suspension-culture reactors, with 15 to 100-fold higher productivities (gL^–1h^–1) and with higher percentage yields forS. cerevisiae andZ. mobilis, respectively. Further research is needed with these novel supports to evaluate different support shapes and medium compositions that will permit medium flow, stimulate biofilm formation, reduce fermentation costs, and produce maximum yields and productivities.This is Journal Paper No. J-16357 of the Iowa Agriculture and Home Economics Experiment Station, Ames, Iowa. Project No. 3253     

Inhibitory effect of garlic on bacterial pathogens from spices

An unconventional technique for primary screening of bacterial susceptibility to garlic (Allium sativum Linn.), using a slice from its clove, was described. Aqueous extracts of garlic were found to possess a potent bacteriostatic principle against Gram-positive as well as Gram-negative foodborne bacterial pathogens. In agar medium, the minimum inhibitory concentrations (MICs) of garlic were 6–10 mg ml^–1 for Bacillus cereus, 30–40 mg ml^–1 for Staphylococcus aureus (excepting the isolate from garlic, where the MIC was 100 mg ml^–1), 20–30 mg ml^–1 for Clostridium perfringens, 10 mg ml^–1 for Escherichia coli (30 mg ml^–1 for the garlic isolate), 40–100 mg ml^–1 for Salmonella, and 10–40 mg ml^–1 for Shigella. It inhibited the growth of all these strains, which were resistant to some commonly used antibiotics. Most of the tested strains were resistant to penicillins, although sensitive to garlic. While the growth of B. cereus and Cl. perfringens was completely inhibited at 10 and 70 mg garlic, respectively, ml^–1 test broth, their respective enterotoxin production ceased at 10 and 50 mg garlic ml^–1.     

Xylitol production from barley bran hydrolysates by continuous fermentation with Debaryomyces hansenii

The continuous bioconversion of xylose-containing solutions (obtained by acid hydrolysis of barley bran) into xylitol was carried out using the yeast Debaryomyces hansenii under microaerophilic conditions with or without cell recycle. In fermentations without cell recycle, the volumetric productivities ranged from 0.11–0.6 g l^–1 h^–1 were obtained for dilution rates of 0.008–0.088 h^–1. In experiments performed with cell recycle after membrane separation, the optimum xylitol productivity (2.53 g l^–1 h^–1) was reached at a dilution rate of 0.284 h^–1.     

Continuous production of poly(3-hydroxybutyrate-co-3-hyhroxyvalerate) byAlcaligenes eutrophus

Summary Copolymers of 3-hydroxybutyrate (3HB) and 3-hydroxyvalerate (3HV) were produced in a continuous culture ofAlcaligenes eutrophus with 17.5 gl ^–1 of fructose and 2.5gl ^–1 of pentanoic acid in the feed. The P(3HB-co-3HV) productivity was maximal at a dilution rate of 0.17h^–1 and yielded 0.31gl ^–1h^–1 under an ammonium-limited condition. The 3HV content in copolymers increased from 11 to 79 mol% as the dilution rate of cells was increased from 0.06 to 0.32h^–1.     

Sequential kinetic parameter estimation of anaerobic fluidized bed bioreactor using an optimization technique

Mathematical model parameters for the methanogenic degradation of propylene glycol were estimated in a sequential manner by means of an optimization technique. Model parameters determined from an initial experimental data set using one bioreactor were then verified with the results from a second bioreactor. The proposed methodology is a useful tool to obtain model parameters for continuous flow reactors with completely mixed regime. Abbrevations: S – substrate concentration (mg COD l^–1); S _in – influent substrate concentration (mg COD l^–1); D _L – dilution rate (day^–1); – stoichiometric coefficients (ND); nx – number of microbial species (ND); X _S – fixed biomass concentration (mg biomass l^–1); X _L – suspended biomass concentration of (mg biomass l^–1); k _d – decay rate of biomass (day^–1); b _S – specific detachment rate of biofilm (day^–1); – specific growth rate of biomass (day^–1); _m – maximum specific growth rate of biomass (day^–1); K _S – half saturation constant (mg COD l^–1); K _I – inhibition constant (mg COD l^–1).     

Biomass relationship to growth and phosphate uptake ofPseudomonas fluorescens,Escherichia coli andAcinetobacter radioresistens in mixed liquor medium

The ability ofPseudomonas fluorescens, Escherichia coli andAcinetobacter radioresistenns to remove phosphate during growth was related to the initial biomass as well as to growth stages and bacterial species. Phosphate was removed by these bacteria under favourable conditions as well as under unfavourable conditions of growth. Experiments showed a relationship between a high initial cell density and phosphate uptake. More phosphate was released than removed when low initial cell densities (10²–10⁵ cells ml^–1) were used. At a high initial biomass concentration (10⁸ cells ml^–1), phosphate was removed during the lag phase and during logarthmic growth byP. fluorescens. Escherichia coli. at high initial biomass concentrations (10⁷ cells ml^–1), accumulated most of the phosphate during the first hour of the lag phase and/or during logarithmic growth and in some cases removed a small quantily of phosphate during the stationary growth phase.Acinetobacter radioresistens, at high initial cell densities (10⁶, 10⁷ cells ml^–1) removed most of phosphate during the first hour of the lag phase and some phosphate during the stationary growth phase.Pseudomonas fluorescens removed phosphate more thanA. radioresistens andE. coli with specific average ranges from 3.00–28.50 mg L^–1 compared to average ranges of 4.92–17.14 mg L^–1 forA. radioresistens and to average ranges of 0.50–8.50 mg L^–1 forE. coli.     

Direct alcoholic fermentation of starchy biomass using amylolytic yeast strains in batch and immobilized cell systems

Summary Direct alcoholic fermentation of dextrin or soluble starch with selected amylolytic yeasts was studied in both batch and immobilized cell systems. In batch fermentations, Saccharomyces diastaticus was capable of fermenting high dextrin concentrations much more efficiently than Schwanniomyces castellii. From 200 g·l^–1 of dextrin S. diastaticus produced 77 g·l^–1 of ethanol (75% conversion efficiency). The conversion efficiency decreased to 59% but a higher final ethanol concentration of 120 g·l^–1 was obtained with a medium containing 400 g·l^–1 of dextrin. With a mixed culture of S. diastaticus and Schw. castellii 136 g·l^–1 of ethanol was produced from 400 g·l^–1 of dextrin (67% conversion efficiency). S. diastaticus cells attached well to polyurethane foam cubes and a S. diastaticus immobilized cell reactor produced 69 g·l^–1 of ethanol from 200 g·l^–1 of dextrin, corresponding to an ethanol productivity of 7.6g·l^–1·h^–1. The effluent from a two-stage immobilized cell reactor with S. diastaticus and Endomycopsis fibuligera contained 70 g·l^–1 and 80 g·l^–1 of ethanol using initial dextrin concentrations of 200 and 250 g·l^–1 respectively. The corresponding values for ethanol productivity were 12.7 and 9.6 g·l^–1·h^–1. The productivity of the immobilized cell systems was higher than for the batch systems, but much lower than for glucose fermentation.     

L-Sorbose production in a continuous fermenter with and without cell recycle

The kinetics of continuous l-sorbose fermentation using Acetobacter suboxydans with and without cell recycle (100%) were investigated at dilution rates (D) of 0.05, 0.10, 0.15 and 0.3 h^–1. The biomass and sorbose concentrations for continuous fermentation without recycle increased as the dilution rate was increased from 0.05 to 0.10 h^–1. A maximum biomass concentration of 8.44 g l^–1 and sorbose concentration of 176.90 g l^–1 were obtained at D=0.10 h^–1. The specific rate of sorbose production and volumetric sorbose productivity at this dilution rate were 2.09 g g^–1 h^–1 and 17.69 g l^–1 h^–1. However, on further increasing the dilution rate to 0.3 h^–1, both biomass and sorbose concentrations decreased to 2.93 and 73.20 g l^–1 respectively, mainly due to washout of the reactor contents. However, the specific rate of sorbose formation and volumetric sorbose productivity at this dilution rate increased to 7.49 g g^–1 h^–1 and 21.96 g l^–1 h^–1 respectively. Continuous fermentation with 100% cell recycle served to further enhance the concentration of biomass and sorbose to 28.27 and 184.32 g l^–1 respectively (in the reactor at a dilution rate of 0.05 h^–1). Even though, there was a decline in the biomass and sorbose concentrations to 6.8 and 83.40 g l^–1 at a dilution rate of 0.3 h^–1, the specific rates of sorbose formation and volumetric sorbose productivity increased to 3.67 g g^–1h^–1 and 25.02 g l^–1 h^–1.     

Influence of operational parameters in the flocculation and production ofLactobacillus plantarum

Summary The influence of different operational parameters, such as the dilution rate (D) and the bleeding rate (B), in the production of a flocculent strain ofLactobacillus plantarum was studied. The effect of the dilution rate was demonstrated to be related to the lactic acid concentration inside the reactor. The effect of the bleeding rate was shown to be critical in the stabilization of the operation (due to a better pH control). It also allowed a continuous recovery of cells outside the reactor. Viability testing of the lactic starter cultures showed that operation with cell purge increased the viability of the starter cultures obtained.Nomenclature B Bleeding rate, h^–1 - D Dilution rate, h^–1 - F Feed flow rate, L h^–1 - I Feed velocity, m h^–1 - Specific growth rate, h^–1 - v Lactic acid specific productivity, g g^–1 h^–1 - P Product concentration (lactic acid), g L^–1 - P _out Product concentration leaving the system, g L^–1 - Q _b Bleeding flow rate, L h^–1 - R Recirculation velocity, m h^–1 - S Substract concentration, g L^–1 - t Time, h - T _p Time of ascensional flow (length of the column/total ascensional velocity), h - T _r Residence time (1/D), h - V Volume of the reactor, L - X Cell concentration, g L^–1 - X _out Cell concentration leaving the system, g L^–1     

Nutrient (N,P, Si) fluxes between marine sediments and water column in coastal and open Adriatic

Nutrient benthic fluxes, as well as sediment phosphorus concentration at the open sea and coastal water stations of the Central and South Adriatic were studied during 1997–98. The fluxes were in the ranges: 0.16–2.67 mmol m^–2 d^–1 (silicate); –0.031–0.164 mmol m^–2 d^–1 (phosphate); –0.51–2.03 mmol m^–2 d^–1 (ammonia); and –1.32–1.62 mmol m^–2 d^–1 (nitrate + nitrite). Silicate flux showed a gradient from the coastal area to the open sea. Ammonia was the main nitrogen species in the flux at the estuary and bay stations, while the sum of nitrate and nitrite was predominant at the open sea stations. Relationships between phosphate and ammonia fluxes (r = 0.699, p<0.01) as well as phosphate and silicate (r = 0.529, p<0.01) were established.     

Phytoplankton and zooplankton (Cladocera,Copepoda) relationship in the eutrophicated River Danube (Danubialia Hungarica,CXI)

The seasonal variation in primary production, individual numbers, and biomass of phyto- and zooplankton was studied in the River Danube in 1981. The secondary production of two dominant zooplankton species (Bosmina longirostris and Acanthocyclops robustus) was also estimated. In the growing season (April–Sept.) individual numbers dry weights and chlorophyll a contents of phytoplankton ranged between 30–90 × 10⁶ individuals, l^–1, 3–12 mg l^–1, and 50–170 µg l^–1, respectively. Species of Thalassiosiraceae (Bacillariophyta) dominated in the phytoplankton with a subdominance of Chlorococcales in summer. Individual numbers and dry weights of crustacean zooplankton ranged between 1400–6500 individuals m^–3, and 1.2–12 mg m^–3, respectively. The daily mean gross primary production was 970 mg C m^–3 d^–1, and the net production was 660 mg C m^–3 d^–1. Acanthocyclops robustus populations produced 0.2 mg C m^–3 d^–1 as an average, and Bosmina longirostris populations 0.07 mg C m^–3 d^–1. The ecological efficiency between phytoplankton and crustacean zooplankton was 0.03%.     

Brachionus calyciflorus Pallas as agent for the removal of E. coli in sewage ponds

Brachionus calyciflorus (Pallas) is a common brachionid in sewage oxidation ponds. The uptake and assimilation of E. coli was optimal at concentrations of 2.7–6.9 × 10⁸ cells ml^–1 while assimilation coefficient per body weight of B. calyciflorus was found to be 10% · Ind.^–1 d^–1. More than two eggs per individual were produced during 24 hours when brachionids were fed with a mixutre of E. coli (10⁹ cells · ml^–1) and Chlorella spp. (10⁶ cells · ml^–1). The nutritional value of the mixture of E. coli and Chlorella spp. was found to be higher than that of bacteria alone.     

Kinetic analysis of ethanol production by an acetate-resistant strain of recombinant Zymomonas mobilis

Zymomonas mobilis ZM4/Ac^R (pZB5), a mutant recombinant strain with increased acetate resistance, has been isolated following electroporation of Z. mobilis ZM4/Ac^R. This mutant strain showed enhanced kinetic characteristics in the presence of 12 g sodium acetate l^–1 at pH 5 in batch culture on 40 g glucose, 40 g xylose l^–1 medium when compared to ZM4 (pZB5). In continuous culture, there was evidence of increased maintenance energy requirements/uncoupling of metabolism for ZM4/Ac^R (pZB5) in the presence of sodium acetate; a result confirmed by analysis of the effect of acetate on other strains of Z. mobilis. Nomenclature m Cell maintenance energy coefficient (g g^–1 h^–1)Maximum overall specific growth rate (1 h^–1)Maximum specific ethanol production rate (g g^–1 h^–1)Maximum specific total sugar utilization rate (g g^–1 h^–1)Biomass yield per mole of ATP (g mole^–1 Ethanol yield on total sugars (g g^–1)Biomass yield on total sugars (g g^–1)True biomass yield on total sugars (g g^–1)     

Evaluation of the potential of Aspergillus niger species for the bioconversion of L-phenylalanine into 2-phenylethanol

Aspergillus niger was explored, for the first time, for the production of 2-phenylethanol (a rose-like aroma) using L-phenylalanine as precursor. Among the strains screened, A. niger CMICC 298302 was shown to produce, in a culture medium containing 6 g L-phenylalanine l^–1 and 60 g glucose l^–1, 1375 mg 2-phenylethanol l^–1 with a productivity of 153 mg l^–1 day^–1 and a molar yield of 74%. 2-Phenylethanol concentrations of 1 to 2 g l^–1 led to a two-fold and ten-fold decrease, respectively, in the mycelial radial growth rate. However, 2-phenylethanol was synthesized as the sole aromatic product and accumulated in the culture broth.     

In vitro multiplication and microrhizome induction in Curcuma aromatica Salisb.

Shoot multiplication and plant regeneration was achieved from freshly sprouted shoots of Curcuma aromatica on Murashige and Skoog's medium supplemented with BA alone (1–7 mgL^–1) or a combination of BA(1–5 mgL^–1) and Kn (0.5–1 mgL^–1). A concentration of 5 mgL^–1 BA was optimum for shoot multiplication and rooting of shoots. The regenerated plants grew profusely on transfer to liquid medium.In vitro raised plants were successfully established in the field. Microrhizomes were induced at the base of the in vitro derived shoots upon transfer to medium containingvarious combinations and concentrations of sucrose and BA and grown under varying photoperiods. MS basal medium with 5 mgL^–1 BA, 60 gL^–1 sucrose and an8 h photoperiod was optimum for induction ofmicrorhizomes within 30 days of culture. Harvestedmicrorhizomes stored in moist sand in poly-bagssprouted after 2 months of storage at roomtemperature. For in vitro storage, microrhizomeswere grown in medium containing 0.1 mgL^–1 BA.Microrhizome formation was found to be controlled bythe concentrations of BA and sucrose as well asphotoperiod during culture.