High nisin Z production by Lactococcus lactis UL719 in whey permeate with aeration

The influence of controlled pH (5.0–6.5) and initial dissolved oxygen level (0–90% air saturation) on nisin Z production in a yeast extract/Tween 80-supplemented whey permeate (SWP) was examined during batch fermentations with citrate positive Lactococcus lactis subsp. lactis UL719. The total activity corresponding to the sum of soluble and cell-bound activities, as measured by a critical dilution method, was more than 50% lower at pH 5.0 than in the range 5.5–6.5, although the specific production decreased as pH increased. A maximum nisin Z activity of 8200 AU/ml (4100IU/ml) was observed in the supernatant after 8h of culture for pH ranging from 5.5 to 6.5. Prolonging the culture beyond 12h decreased this activity at pH 6.0 and 6.5 but not at pH 5.5 or 5.0. A corresponding increase in cell-bound activity was probably due to adsorption of soluble bacteriocin to the cell wall. Aeration increased cell-bound and total activity to maximum values of 32800 and 41000 AU/ml (16400 and 20500IU/ml), respectively, with an initial level of 60% air saturation after 24h of incubation at pH 6.0. The specific production at 60% or 90% initial air saturation was eight-fold higher than at 0%.     

Unstructured model for the decline phase of batch cultures of Lactobacillus helveticus growing on supplemented whey permeate

An unstructured model was previously developed to describe growth of Lactobacillus helveticus; this model accounted for the biomass kinetics until the stationary state was achieved. In the new model, the decline phase was modelled as an exponential decay, all the parameters having an obvious biological meaning. By means of both expressions, the whole growth history is described. This model has been tested for a wide range of yeast extract (YE) supplementations (5–30 g l⁻¹), i.e. for various autolysis kinetics (from 8 to 26% of autolysis after 8 h of death phase); in all cases, the new model fitted accurately the experimental data.     

Lactic acid production by batch fermentation of whey permeate: A mathematical model

Summary The batch fermentation of whey permeate to lactic acid was improved by supplementing the broth with enzyme-hydrolyzed whey protein. A mathematical model based on laboratory results predicts to a 99% confidence limit the kinetics of this fermentation. Cell growth, acid production and protein and sugar use rates are defined in quantifiable terms related to the state of cell metabolism. The model shows that the constants of the Leudeking-Piret model are not true constants, but must vary with the medium composition, and especially the peptide average molecular weight. The kinetic mechanism on which the model is based also is presented.Nomenclature K _i lactic acid inhibition constant (g/l) - K _pr protein saturation constant during cell growth (g/l) - K _pr protein saturation constant during maintenance (g/l) - K _s lactose saturation constant (g/l) - [LA] lactic acid concentration (g/l) - [PR] protein concentration (g/l) - [S] lactose concentration (g/l) - t time (h) - [X] cell mass concentration (g/l) - , fermentation constants of Leudeking and Piret - specific growth rate (l/h) - Y _{g, LA/S} acid yield during cell growth (g acid/g sugar) - Y _{m, LA/S} acid yield during maintenance (g acid/g sugar) - Y _x/pr yield (g cells/g protein) - specific sugar use rate during cell growth (g sugar/h·g cell) - specific sugar use rate during maintenance (g sugar/h·cell)     

Immunodot detection of nisin Z in milk and whey using enhanced chemiluminescence

A highly specific antisera was produced in New Zealand white rabbits against nisin Z, a 3400 Da bacteriocin produced by Lactococcus lactis ssp. lactis biovar. diacetylactis UL 719. A dot immunoblot assay was then developed to detect nisin Z in milk and whey. As few as 1·5 10⁻¹ international units per ml (IU ml⁻¹), corresponding to 0·003 μg ml⁻¹ of pure nisin Z, were detected in carbonate-bicarbonate buffer within 6 h using chemiluminescence. When milk and whey samples were tested, approximately 0·155 μg ml⁻¹ (7·9 IU ml⁻¹) of nisin Z was detected. The detection limit obtained was lower than that of traditional methods including microtitration and agar diffusion.     

Batch cultures of supplemented whey permeate using Lactobacillus helveticus: unstructured model for biomass formation, substrate consumption and lactic acid production

The Luedeking and Piret expression can not account for the cessation of production observed at the end of batch; so an empiric term has been previously added to this equation which accounted in a global way for possible substrate limitations. In the model developed in this work, a carbon substrate limitation appeared explicitly in the production expression. Assuming a sigmoidal variation with time of specific growth rate previously validated, the new production model matched well the entire experimental production kinetics. It has been successfully tested for a wide range of nitrogen supplementations, i.e. from an almost total coupling between growth and production for largely supplemented media, to a high decoupling in case of few available nitrogen. Since all the parameters of this model have an obvious biologic meaning, it may be an unvaluable tool for the comprehension of the phenomenon. The model accounted also well for the variation of the specific production rate versus specific growth rate, avoiding the noise due to the direct differentiation of experimental data.     

Production of solvents (ABE fermentation) from whey permeate by continuous fermentation in a membrane bioreactor

A continuous bioreactor where cells were recycled using a cross-flow microfiltration (CFM) membrane plant was investigated for the production of solvents (ABE fermentation) from whey permeate using Clostridium acetobutylicum P262. A tubular CFM membrane plant capable of being backflushed was used.The continuous fermentations were characterized by cyclic solventogenic and acidogenic behaviour, and ultimately degenerated to an acidogenic state. Steady-state solvent production was obtained for only short periods. This degeneration is attributed to the complex morphological behaviour of this strain of organism on this substrate.It is postulated that to achieve steady-state solvent production over extended periods of time, it is necessary to maintain a balance among the various morphological cell forms, i.e. acid-producing vegetative cells, solvent-producing clostridial cells, and inert forms, e.g. spores.     

Scaling-up of a batch whey fermentation by Kluyveromyces fragilis

Summary A whey fermentation by Kluyveromyces fragilis was scaled-up to a 1000-dm³ stirred fermentor, by varying the stirrer speed, the air-flow rate and the initial concentration of lactose. Its evolution was simulated by applying the same unstructured model (consisting of a microbial specific growth rate of pseudo-first order with respect to the COD concentration and constant biomass yield per unit COD removed) set up in previous experiments using 8- to 80-dm³ fermentors. Despite the great scale-up ratios, very different operating conditions, and geometric dissimilarity, a series of empirical regressions previously developed allowed approximate, but acceptable prediction of the stoichiometric and kinetic coefficients of the above mathematical model, thus confirming the capability of this model to provide a reliable basis for further scale-up of this fermentation process to a production scale.     

Production of glucosyl-transferring enzyme by Aspergillus niger in batch cultures

Aspergillus niger produced an extracellular glucosyltransferase with a high transglucosylating activity. Among carbon sources tested, maltose gave the highest enzyme production: 0.20-0.26 units/ml.     

Production of butyric acid by batch fermentation of cheese whey withClostridium beijerinckii

Summary The effect of pH on the fermentation of butyric acid byClostridium beijerinckii using cheese whey as a substrate was studied. Maximum concentrations of the acid were produced when the pH was controlled at 5.5. Raising or lowering of pH was found to reduce the total acid formation. This particular strain ofC. beijerinckii produced insignificant amounts of butanol in all the pure culture cases investigated. A comparative study of the fermentation in a synthetic glucose medium and in cheese whey showed the whey to produce more butyric acid.     

Production of propionic acid from whey permeate by sequential fermentation, ultrafiltration, and cell recycling

This article deals with the production by fermentation of a mycostatic and aromatic food additive based on propionic acid. Membrane bioreactors have been used from laboratory scale up to pilot and industrial production plants. Due to the high cell densities achieved by the sequential recycling mode of operation, a mixed acids solution was rapidly produced from whey permeate. The sterile fermented broth obtained was subsequently concentrated at different levels by evaporation and spray drying according to the projected use. Concentrated Propionibacterium cells (200 g . L(-1) DW) were obtained from the process by periodic bleeds and could be used to good effect as cheese starters, silage preservatives, or probiotics. Propionic acid concentrations from 30 to 40 g . L(-1) were easily achieved with no residual lactose. The highest volumetric productivity was 1.6 g . L(-1) . h(-1) for total acid and 1.2 g . L(-1) . h(-1) for propionic acid with a specific productivity of 0.035 h(-1). (c) 1993 John Wiley & Sons, Inc.     

Production of propionic acid by mixed cultures ofPropionibacterium shermanii andLactobacillus casei in autoclave-sterilized whey

Summary Pure cultures ofPropionibacterium freudenreichii ss.shermanii did not grow in autoclave-sterilized cheese whey (121°C, 15 psi, 20 min) at whey concentrations greater than 2% (w/v) spray-dried sweet dairy whey. Propionic acid was produced from autoclave-sterilized whey by growingP. shermanii in mixed culture withLactobacillus casei. In medium containing 5–12% autoclaved whey solids and 1% yeast extract, the mixed culture produced 1.3–3.0% propionic acid, 0.5–1.0% acetic acid, and 0.05–0.80% lactic acid. All the lactose was consumed. Using pH-controlled fermentors (pH=7.0), mixed cultures produced at least 30% more propionic acid than cultures in which pH was not controlled.     

Continuous production of lactic acid from whey permeate by Lactobacillus helveticus in two chemostats in series

The effect of dilution rate on the production of lactic acid from whey permeate by Lactobacillus helveticus has been investigated. In the first chemostat of a two-stage system, total conversion (98.1%) and maximum lactic acid concentration (43.7 g l⁻¹) were obtained at a dilution rate (D_Itot) of 0.06 h⁻¹. Maximum volumetric productivities of lactic acid (8.27 g l⁻¹ h⁻¹) and biomass (1.90 g l⁻¹ h⁻¹) occurred at D_Itot of 0.40 h⁻¹. The fraction of -lactate in the product was found to increase with dilution rate and reached a maximum of 66% at the same dilution rate. The maximum specific growth rate (μ_max) on this medium was 0.7 h⁻¹. A Y_ATP (max) value of 22.4 g dry weight (mol ATP)⁻¹ and a maintenance coefficient of 8.0 mmol ATP (g dry weight h)⁻¹ were determined. The second stage, in series with the first, confirmed these results and further showed that the total residence time could be reduced by 50%, compared with a single chemostat for the same nearly complete level of substrate conversion.     

Anaerobic digestion of high-strength acidic whey in a pH-controlled up-flow fixed film loop reactor

Summary A fixed film loop reactor was developed for the stabilization of undiluted sour whey. Porous clay beads were used to immobilize the population. The fermentation system was self-supporting with the aid of a pH-titrator. Within 2 months; the loading increased automatically to its maximum of 14 kg COD (chemical oxygen demand)/m³ per day. Parallel to this, the bacterial film was formed on the surface of the support material. For a pH of 6.7 the steady state was reached at a hydraulic retention time of 5 days equivalent to a loading of 14 kg COD/m³ per day. An amount of 5.6 m³ biogas was produced per m³ digester content and day and the COD-reduction was 95%. The pH-controlled whey addition led to only minor disturbances when overloading or oxygenation occured and a fast recovery of methanogenesis was observed. The economics of anaerobic whey digestion compared with conventional whey utilization is estimated by a simple cost/benefit calculation.     

Optimal conditions for production of lactic acid from cheese whey permeate by Ca-alginate-entrapped Lactobacillus helveticus

Whole cells of Lactobacillus helveticus were immobilized in calcium-alginate beads to produce lactic acid from cheese whey ultrafiltrate. Ca-alginate-entrapped cells were characterized by higher fermentation rates and optimum pH than free cells. No difference could be observed in the profile of cell activity against temperature for either type of cells. After a heat treatment, cell activity was higher for free cells than for immobilized cells. Continuous lactic acid fermentation using a packed bed reactor was investigated.     

Production of the macrolide antibiotic tylosin in batch and chemostat cultures

The production of tylosin and related compounds by Streptomyces fradiae NRRL 2702 was studied in batch and chemostat cultures using a soluble synthetic medium. In batch culture, a trophophase–idiophase kinetic pattern was observed with tylosin, macrocin, and relomycin accumulating in the idiophase. When the organism was grown in chemostat culture, the specific rate of production of tylosin and related compounds (q_tylosin) was found to be a function of the growth rate. The maximum value of (q_tylosin) was observed when D = 0.017 hr^?1. At this growth rate only tylosin and relomycin accumulated in the medium. By varying the concentration of glucose in the ingoing medium it was possible to study the effects of glucose on tylosin synthesis in chemostat cultures. At a growth rate of 0.017 hr^?1, the maximum value of q_tylosin was 0.71 mg tylosin/g dry weight (DW)/hr when the glucose uptake rate was 7 mg glucose/g DW-hr. This value of q_tylosin was 40% greater than the maximum q_tylosin observed in batch culture. When glycerol was substituted for glucose in the medium, it was possible in chemostat culutures to get values of q_tylosin approximately 20% greater than those obtained with glucose at the same uptake rate. By varying the concentration of sodium glutamate in the ingoing medium it was possible to show that increasing the specific uptake rate of sodium glutamate increased the values of q_tylosin obtained. Similar chemostat experiments where the inorganic phosphate concentration in the ingoing medium was varied showed that increased the uptake of phosphate decreased the values of q_tylosin obtained. Also increasing the uptake rate of phosphate increased the relomycin-to-tylosin ratio. By taking into consideration the suppressing effects of glucose and the stimulating effects of sodium glutamate on tylosin synthesis, it was possible to formulate a medium that resulted in a value of q_tylosin of 1.1 mg/g/hr being obtained at a growth rate of 0.03 hr^?1. Batch fermentations with this medium did not follow a trophophase–idiophase kinetic pattern, but instead tylosin was actively synthesized during a period of rapid mycelial growth.     

Kinetics of lactose transport inKluyveromyces fragilis grown in a chemostat on diluted whey permeate

Lactose transport was studied inKluyveromyces fragilis grown in lactose-limited chemostat cultures. Kinetic parameters were determined using a method based on genetic population evolution. Lactose transport was carried out via three carriers characterized respectively byK _m of 0.1 mM, 3 mM and 15.5 mM. The synthesis of these lactose carriers and their capacity (V _max) are dependent on the dilution rate (D). At D=0.12 h^–1, the high affinity transporter is prominent. For intermediate dilution rate, only the high and the medium affinity systems are present. In cells growing at D=0.4 h^–1, these carriers are absent but instead, the low affinity transporter is present. The effect on lactose transport of such metabolic inhibitors as CCCP, a proton ionophore, and Antimycin A, an energy inhibitor, were also investigated. The high affinity system is the most sensitive to the effect of these inhibitors. Lactose transport through this carrier is probably a mechanism dependent on the proton motive force.     

Hydrolysis of lactose in whey permeate by immobilized β-galactosidase from Kluyveromyces fragilis

Neutral β-galactosidase from Kluyveromyces fragilis was immobilized on silanized porous glass modified by glutaraldehyde binding, with retention of more than 90% of its activity. Marked shifts in optimum pH (from 7.0 to 6.0) and temperature (from 35°C to 50°C) of the solid-phase enzyme were observed together with high catalytic activity and reasonable stability at wider pH and temperature ranges than those of the free enzyme. Highly efficient lactose saccharification (86–90%) in whey permeate was achieved both in a batch process and in a recycling packed-bed bioreactor.     

Production of neutral and alkaline proteases in batch and chemostat cultures by bacillus mesentericus 76

The kinetics of the bacterial extracellular protease synthesis (neutral and alkaline protease of Bacillus mesentericusstrain 76, R-form) in batch and chemostat cultures under conditions of glucose limitation were investigated. When the medium was supplemented with casein the production of the proteases was significantly higher. Optimal dilution rates for obtaining of two proteases are fixed. The synthesis of both alkaline and neutral proteases is controlled by catabolite repression and induction.