Biochemical reactions of Brevibacterium flavum depending on medium stirring intensity and flow structure

Authors have studied the dependence of the physiological and biochemical characteristics of lysine producers Brevibacterium flavum on medium stirring intensity upon constant pO₂ during fermentation processes. Various factors affecting the rate of biochemical reactions in cells upon a changeable intensity of medium stirring in apparata with turbine stirrers; oxygen mass transfer intensity in the system; stirring characteristics in the fermenter; biochemical changes in the cells due to gradients of energy introduced by the stirrer in the fermenter, etc. have been studied. A comparison of the experimentally established values, characterizing macrostirring (e) and microstirring (K_R), with the physiological and chemical characteristics of bacteria during fermentation made us suppose that the character of the kinetic energy distribution in the volume of fermenter is one of the factors regulating bacterial metabolism. Besides, there exists the value e_crit, upon which there can be observed essential changes of the physiological and biochemical properties of the cells. The effect of medium flows upon the cells is characterized by index F_stress, which takes into account both, the possible presence of the cells in the zone with e ≧ e_crit, and the degree of medium flow and cell interaction, numerically equal to value (e – e_crit)^0.5.     

Design and simulation of a fuzzy controller for fed-batch yeast fermentation

In baker's yeast fermentation, the process is non-linear and the response of the system to changes in glucose feeding has a very long delay time. Therefore, a conventional system can not give satisfactory results. In this paper, a fuzzy controller designed to control a fed-batch fermenter is presented. The fuzzy controller uses Respiratory Quotient (RQ) as a controller input and produces glucose feeding rate as control variable. The controller has been tested on a simulated fed-batch fermenter. The results show that the maximum yeast production is possible by keeping the specific growth rate (μ) and the glucose concentration (C _s) at preset values (μ _Cand C _s,c) and minimizing the ethanol production.     

Gerätesystem zur Massenspektrometrischen Prozeßüberwachung in der Fermentationstechnik

A quadrupol mass spectrometer QMS c 300 developed and manufactured from the workshops of the Institute of Nuclear Research of the Hungarian Academy of Sciences, Debrecen, has been cuppled with a 12 l laboratory steril fermenter. The QMS apparatus is provided with 3 different possibilities for sampling. Via a dynamic air input system the discharged air of the fermenter can be analyzed continuously. The static sampling input allows the off-line measurement of gaseous and volatile compounds. Special membran samplers are used for measurements of volatile and gaseous substrates and microbial metabolites in the fermentation broth. The samplers can be adopted in the reactor vessel directly analogous to the pH and pO₂-electrodes.     

Modelling of the process yields of a whey fermentation

Summary The biomass yields (y) and COD reduction efficiencies (η) of a whey fermentation by Kluyveromyces fragilis were studied in a 100-1 fermenter at various stirrer speeds and lactose concentrations, and compared to those obtained in 10-1 and 15-1 fermenters at constant values of the oxygen transfer coefficient (k_La) and air velocity. The empirical models previously constructed by using the 15-1 fermenter data could be used to predict the yields on the other scales by calculating for each run the 15-1 fermenter which would provide the same oxygen transfer coefficient measured by the sulphite method on each fermenter under study. To make this model independent of stirrer speeds used in each generic fermenter, the effect of aeration and mixing was incorporated into an overall parameter (k_La) and the values of y and η were correlated only with temperature, lactose level and k_L a, since these variables were approximately orthogonal. The validity of this model was finally checked against the yields reported by Wasserman et al. (1961) in a 6-m³ fermenter, thus confirming the capability of the model to provide a reliable basis for further scale-up on the production scale.     

Energetics of the growth of Methanococcus thermolithotrophicus

Methanococcus thermolithotrophicus was grown in a mineral salts medium at 65° C in a fermenter gassed with H₂ and CO₂, which were the sole carbon and energy sources. Evolution of growth parameters during batch culture experiments showed the existence of an uncoupling phenomenon. The growth was then studied using a continuous technique and steady states for various gas flow rates were obtained. Y _{CH 4}and the maintenance coefficient varied with the gas input. The maximum Y _{CH 4} determined for Methanococcus thermolithotrophicus was 3.33 g·mol^-1 CH₄. An excess of energy and carbon sources induced uncoupling of growth.     

A kLa identification technique for a dynamic model of the coupled system: Air-lift fermenter — oxygen probes

The time delay of oxygen probe response to the signal from a fermenter makes identification of the volumetric oxygen transfer coefficient k_La by the dynamic method more complicated. A coupled model involving the transient-state oxygen balance of the fermenter together with the dynamic model of the oxygen probe must be then formulated, solved and identified. In this paper two simple models of air-lift loop fermenters have been proposed and a coupled mathematical model of the fermenter – oxygen probe system has been developed. The identification procedure was used to estimate k_La values in the fermenter with internal circulation flow on the basis of experimental measurements. A comparison of evaluated and experimental indications of the probes placed at various heights of the column proves that the model presented gives a possibility of the first-step approximation of k_La in loop fermenters.     

Studies of insufficient mixing in bioreactors: Effects of limiting oxygen concentrations and short term oxygen starvation on Penicillium chrysogenum

The effect of oxygen limitation on the respiration rate of Penicillium chrysogenum was studied. The results show that measurements of critical oxygen tensions within a process that on morphological or on physical grounds exhibits an inhomogenous structure are not likely to resemble the Monod model.In order to study the effects of short term oxygen starvation on the respiratory capacity of Penicillium chrysogenum, a two compartment fermenter was constructed. This fermenter consists of one well mixed aerobic part (CSTR) and one minor anaerobic part (CPFR). In the latter the circulation time as well as the volume can be varied. After passage of the whole cell culture volume through the anaerobic part, irreversible inhibition of the respiration was observed. This was caused by a circulation time of 5 and 10 min in the plug flow reactor and with a volume of 6% of the stirred tank reactor volume. However, circulation times of 1 and 2 min with an anaerobic zone of 1% of the stirred tank reactor volume did not give any irreversible effects on the respiratory capacity.This was compared with the results of the previously established model ln(1 — I _OUR//100)^–1 = kt [1]. The I _OUR is the percentage irreversible inhibition of the respiration, t is the anaerobic circulation time and k is a constant. The two compartment fermenter results agree with the earlier model at circulation times of 5 and 10 min, but not with the shorter times, and this suggests that a lag phase exists in the inactivation kinetics.     

Optimisation of agitation and aeration in fermenters

The problem of optimising agitation and aeration in a given fermenter is addressed. The objective function is total electric power consumed for agitation, compression and refrigeration. The major constraint considered is to ensure that the dissolved oxygen concentration is above the critical value. It is shown that it is possible to analytically calculate the optimal pair (air flowrate, stirrer speed) and that, at least for the industrial antibiotics fermentation used as case-study, the optimum lies within a window for satisfactory operation, limited by other possible constraints to the problem. Savings achievable by optimal operation as compared with current industrial procedure were found to be around 10% at pilot plant scale (0.26 m³) and 20% at full scale (85 m³).List of Symbols A fermenter cross sectional area (m²) - C dissolved oxygen concentration (mole m^–3) - C ^* DO concentration in equilibrium with the gas (mole m^–3) - C _crit critical DO concentration (mole m^–3) - C _p specific heat of air at constant pressure (J kg^–1 K^–1) - C _sp dissolved oxygen set point (mole m^–3) - C _v specific heat of air at constant volume (J kg^–1 K^–1) - D agitator diameter (m) - f pressure correction of air flow-rate - (Fl _g)_F aeration number at flooding - (Fr _g)_F froude number at flooding - k coefficient in expression for mass transfer coefficient - K _La volumetric oxygen transfer coefficient (s^–1) - m power exponent in expression for mass transfer coefficient - n gas flow rate exponent in expression for mass transfer coefficient - n ^* number of impellers - N rotation speed (s^–1) - N _F rotation speed at flooding (s^–1) - N _p unaerated power number - N _pg aerated power number - OUR Oxygen Uptake Rate (mole m^–3 s^–1) - p ₀ atmospheric pressure (N m^–2) - p ₁ compressor exit pressure (N m^–2) - p ₂ pressure at the bottom of the fermenter (N m^–2) - p ₃ pressure at the top of the fermenter (N m^–2) - P _c compression power (W) - P _d power added by expansion (W) - P _ev power removed by evaporation (W) - P _g agitation power (W) - P _m power added by metabolism (W) - P _r power removed by refrigeration (W) - P _t total power (W) - Q air flow-rate at atmospheric conditions (m³ s^–1) - Q _f air flow-rate at average fermenter conditions (m³ s^–1) - s ₀ absolute humidity at atmospheric conditions - s ₃ absolute humidity at fermenter exit - T tank diameter (m) - V liquid volume (m³) - v _s gas superficial velocity (m s^–1) - _i parameter defined in the text - safety margin for dissolved oxygen (mole m^–3) - ratio of specific heats of air - _g agitation efficiency - _c compression efficiency - _r refrigeration efficiency - liquid density (kg m^–3) - _g air density (kg m^–3) - latent heat of vaporisation of water (J kg^–1) The authors are grateful to Elsa Silva, Carlos Lopes, Carlos Aguiar, Fernando Mendes, and Alexandre Cardoso, who helped with parts of this work, and to CIPAN for permission to publish these data.     

Optimization of exopolysaccharide production from Armillaria mellea in submerged cultures

Aims: To study the optimization of submerged culture conditions for exopolysaccharide (EPS) production by Armillaria mellea in shake‐flask cultures and also to evaluate the performance of an optimized culture medium in a 5‐l stirred tank fermenter. Methods and Results: Shake flask cultures for EPS optimal nutritional production contained having the following composition (in g l^?1): glucose 40, yeast extract 3, KH₂PO₄ 4 and MgSO₄ 2 at an optimal temperature of 22°C and an initial of pH 4·0. The optimal culture medium was then cultivated in a 5‐l stirred tank fermenter at 1 vvm (volume of aeration per volume of bioreactor per min) aeration rate, 150 rev min^?1 agitation speed, controlled pH 4·0 and 22°C. In the optimal culture medium, the maximum EPS production in a 5‐l stirred tank fermenter was 588 mg l^?1, c. twice as great as that in the basal medium. The maximum productivity for EPS (Q_p) and product yield (Y_P/S) were 42·02 mg l^?1 d^?1 and 26·89 mg g^?1, respectively. Conclusions: The optimal culture conditions we proposed in this study enhanced the EPS production of A. mellea from submerged cultures. Significance and Impact of the Study: The optimal culturing conditions we have found will be a suitable starting point for a scale‐up of the fermentation process, helping to develop the production of related medicines and health foods from A. mellea.     

Lycopene production from synthetic medium by <Emphasis Type="Italic">Blakeslea trispora</Emphasis> NRRL 2895 (+) and 2896 (−) in a stirred-tank fermenter

The dissolved oxygen tension of 20% of air saturation, pH-shift from 4.0 to 5.5 on day 3, and a moderate shear stress (calculated as an impeller tip speed, V_\texttip = 0. 9 2 6- 2. 1 6 1  \textm/\texts V_{\text{tip}} = 0. 9 2 6- 2. 1 6 1 \, {\text{m}}/{\text{s}} ) were identified to be the key factors in scaling-up the mated fermentation of Blakeslea trispora NRRL 2895 (+) and 2896 (−) for lycopene production from a shake flask to a stirred-tank fermenter. The maximal lycopene production of 183.3 mg/L was obtained in 7.5-L stirred-tank fermenter, and then the mated fermentation process was successfully step-wise scaled-up from 7.5- to 200-L stirred-tank fermenter. The comparability of the fermentation process was well controlled and the lycopene production was maintained during the process scale-up. Furthermore, with the integrated addition of 150 μmol/L abscisic acid on day 3, 0.5 g/L leucine and 0.1 g/L penicillin on day 4, the highest lycopene production of 270.3 mg/L was achieved in the mated fermentation of B. trispora in stirred-tank fermenter.     

Dissolved oxygen as principal parameter for conidia production of biocontrol fungi Trichoderma viride in non-Newtonian wastewater

Dissolved oxygen (DO) concentration was selected as a principal parameter for translating results of shake flask fermentation of Trichoderma viride (biocontrol fungi) to a fermenter scale. All fermentations were carried out in a 7.5 l automated fermenter with a working volume of 4 l. Fermentation performance parameters such as volumetric oxygen transfer coefficient (k _L a), oxygen uptake rate (OUR), rheology, conidia concentration, glucose consumption, soluble chemical oxygen demand, entomotoxicity and inhibition index were measured. The conidia concentration, entomotoxicity and inhibition index were either stable or improved at lower DO concentration (30%). Variation of OUR aided in assessing the oxygen supply capacity of the fermenter and biomass growth. Meanwhile, rheological profiles demonstrated the variability of wastewater during fermentation due to mycelial growth and conidiation. In order to estimate power consumption, the agitation and the aeration requirements were quantified in terms of area under the curves, agitation vs. time (rpm h), and aeration vs. time (lpm h). This simple and novel strategy of fermenter operation proved to be highly successful which can be adopted to other biocontrol fungi.     

Photoautotrophic growth of cell suspension cultures fromChenopodium rubrum in an airlift fermenter

Summary This communication describes the construction and operation of an airlift fermenter for the photoautotrophic growth of cell suspension cultures fromChenopodium rubrum. The basic batch culture unit provides a culture of 1.51 volume, sufficient to permit frequent aseptic sampling. It can be maintained at any desired temperature and aerated to different extents. Using an initial cell density of about 400,000 cells per ml suspension, the increase in cell number is 270% after a 14 days' growth period, although the stationary phase of growth is not yet reached. The transfer of photoautotrophic cell suspensions fromChenopodium rubrum from stationary growth into the large volume of fresh culture medium in the airlift fermenter results in an immediate protein formation, followed by an exponential phase of cell division, whereas rapid chlorophyll accumulation is delayed by 2 days.The growth capacities of photoautotrophic fermenter cultures including protein and chlorophyll formation as well asin vitro activities of the ribulosebisphosphate carboxylase and the phosphoenolpyruvate carboxylase are greatly lower as compared to photoautotrophic cells propagated in standard two-tier culture vessels using 30 ml culture medium. However the pattern of change in the activities of carboxylation enzymes is quite similar in both culture systems.Photoautotrophic cell suspensions fromChenopodium rubrum grown in an airlift fermenter assimilate about 90 mol CO₂/mg chlorophyll × hour. Dark CO₂ fixation is about 1.5% of the light values.Abbreviations PEF phosphoenolpyruvate - RuDP ribulosebisphosPhate - NS ground glass joints of standardized size made from Duran glass, Schott, Germany     

Intraspecific scaling of flight power in the bat Glossophaga soricina (Phyllostomidae)

Aerodynamic theory predicts that power output during flight should vary with body mass by an exponent of 1.56 when wing morphology remains constant (within an individual), and by an exponent of 1.19 when wing morphology changes with body mass (within a species or between species). I tested these predictions by estimating the power input during horizontal flight in three pregnant and two subadult Glossophaga soricina using a multivariate regression model. This analysis yielded power input during resting and flight as well as the energetic equivalent of change in body mass. A comparison of the estimated flight power for pregnant G. soricina, with published data on flight power of non-pregnant adults, revealed that energy turnover in flight is highest for pregnant G. soricina. Flight power of a 13-g pregnant G. soricina was even higher than that of a 16-g non-pregnant Glossophaga longirostris. A least-squares regression analysis yielded the following equations for the intraspecific scaling of flight power with body mass: power input during horizontal flight (P _f )=24099 body mass (bm; kg)^2.15 (r ²=0.97) for the intra-individual allometry (pregnancy) and P _f =113 bm(kg)^0.95 (r ²=0.99) for the inter-individual allometry (ontogeny). Both mass exponents are not significantly different from the predicted values for the scaling relationship of flight power within an individual (1.56) and within a species (1.19). This is the first measurement of power input during flight for subadult and pregnant bats. Accepted: 11 May 2000     

Mass propagation of ornamental gentian in liquid medium

An efficient system for clonal mass propagation in liquid culture was established for the propagation of ornamental gentian. In a test of the requirements for three cytokinins [6-benzylaminopurine, N-(2-chloro-4-pyridyl)-N′-phenylurea and N-phenyl-N′-1,2,3-thiadiazol-5-yl urea (TDZ)] in combination with 1-naphthaleneacetic acid (NAA), we found that effective propagation of shoots occurred with 0.01 mg l^–1 TDZ in a 300 ml conical flask that contained 100 ml of medium. The propagation of shoots was also affected by the concentrations of macronutrients (KNO₃, NH₄NO₃ and CaCl₂) and sucrose in Murashige and Skoog's (MS) medium, and it was influenced to some extent by the speed of agitation on an orbital shaker. The most efficient propagation of shoots was achieved in full-strength MS medium supplemented with 0.01 mg l^–1 TDZ and 20 g l^–1 sucrose with agitation at 150 rpm. The propagation of shoots was maximal after 6 weeks of culture (140 shoots from five nodal segments in one flask). Large-scale propagation in a 5-l fermenter was attempted using 3 l of MS medium that contained 0.01 mg l^–1 TDZ and 20 g l^–1 sucrose. More than 2,000 shoots were obtained in the fermenter in 5 weeks following the initial cultivation of five nodal segments for 6 weeks in one 300-ml flask. The shoots that had propagated in the fermenter were transferred directly to soil without prior rooting in vitro and were easily acclimatized within 1 month. Received: 7 October 1997 / Revision received: 16 January 1998 / Accepted: 30 January 1998     

Improved performance in γ-polyglutamic acid production by Bacillus subtilis LX on industrial scale by impeller retrofitting and its unstructured microbial growth kinetics model

Abstract

We conducted industrial scale γ-polyglutamic acid (γ-PGA) production by Bacillus subtilis (B. subtilis) LX and modeled its microbial growth kinetics based on a logistic regression. We found that the use of a three-layer impeller including a lower semicircular disc impeller and two-layers of six-wide-leaf impellers were able to both increase γ-PGA yields and decrease fermentation time as compared with two-layer Rushton impellers. Indeed, our results revealed that the optimal γ-PGA yield (20.67?±?2.19?g/L) was obtained after 40?hr in the impeller retrofitted fermenter, and this yield was 29.7% higher than that in Rushton impellers fixed fermenter. The microbial growth kinetics of B. subtilis LX in this system were established, and the model was consistent with the experimental data (R² = 0.924) suggesting that it was suitable for describing the microbial growth kinetics underlying γ-PGA production on an industrial scale. In addition, biomass yield (Y_x/s-glucose), γ-PGA yield (Y_p/s-glucose), γ-PGA yield (Y_{p/s-glutamate}), and the correlation between γ-PGA production and B. subtilis LX (Y_p/x) were found to be 0.043, 0.133, 0.743, and 3.090?g/g, respectively, in the impeller retrofitted fermenter, as compared with 0.036, 0.103, 0.629, and 2.819?g/g, respectively, in the two-layer Rushton impeller fermenter.     

Yield regulation of lysine biosynthesis in Brevibacterium flavum

A scheme for lysine biosynthesis using variants of the Brevibacterium flavum intermediary metabolite synthesis is discussed. The main precursor of lysine that we are concerned with here is oxalacetate, which can be synthesized through the TCA or glyoxylate cycles or by carboxylation of PEP. Material energy balances for the main pathways of lysine biosynthesis from glucose and acetate have been formulated. Energy consumption, in the from of ATP – P_ATP (number of mol ATP consumed/1 mol lysine synthesized), was calculated for the main pathways of lysine biosynthesis. Theoretical conversion yields Y_p^max (g product/g substrate) were estimated. Experimental data were presented concerning the increase of Y_p by means of metabolism regulation: (a) by TCA-and glyoxylate-cycle enzyme induction; (b) by maintaining PEP carboxylase activity; (c) by eliminating by-product synthesis.     

Scale-up of PUF-immobilized fungal chitosanase–lipase preparation production

Mucor circinelloides IBT-83 mycelium that exhibits both lipolytic (A_L) and chitosanolytic (A_CH) activities was immobilized into polyurethane foam in a 30?L laboratory fermenter. The process of immobilization was investigated in terms of the carrier porosity, its type, amount, and shape, location inside the fermenter, mixing, and aeration parameters during the culture, as well as downstream processing operations. The selected conditions allowed for immobilization of approximately 7?g of defatted and dried mycelium in 1?g of carrier, i.e., seven times more than achievable in 1?L shake-flasks. Enzymatic preparation obtained by this method exhibited both the chitosanolytic (A_CH 432.5?±?6.8?unit/g) and lipolytic (A_L 150.0?±?9.3?U/g) activities. The immobilized preparation was successfully used in chitosan hydrolysis to produce chitooligosaccharides and low molecular weight chitosan, as well as in waste fats degradation and in esters synthesis in nonaqueous media. It was found that the half-life of immobilized preparations stored at room temperature is on average of 200 days.     

Fluid dynamics of anaerobic fermentation

In beer fermentation, yeast cells are kept in suspension, despite their higher density, by natural agitation created by ascending CO₂ bubbles. Yeast cells are unable to nucleate bubbles but instead release CO₂ in a soluble form in such a way that the medium tends to become supersaturated. A higher concentration of yeast cells and the presence of solid particles cause the formation of bubbles at the bottom of the fermenter and practically only there. The rising bubbles grow and accelerate by sweeping the CO₂ formed throughout the fermenter by the suspended yeast cells, thereby creating a fluid regime. A mathematical expression relating the bubble agitation power to the fermentation parameters was obtained and used to design more efficient fermenter shapes.     

Mixing performance of air-lift fermenters against working volume and draft tube dimensions

Mixing characteristics of a laboratory scale internal loop air-lift fermenter has been investigated. The effects of different draft tube dimensions and positions as well as varying levels of liquid height over the draft tube, on mixing time were determined. The results indicate the existance of an optimum liquid height and thus liquid volume with respect to mixing performance especially for the taller draft tubes.List of Symbols A mm distance between draft tube and reactor base - A _D mm² area of the downcomer region - A _R mm² area of the riser region - B mm width of annulus - D _d mm draft tube diameter - D _t mm fermenter diameter - H _d mm draft tube height - H _l mm liquid height in the fermenter - H _t mm fermenter height - V _d m³ draft tube volume - V _t m³ fermenter volume - D _d /D _l - _B H _d /H _l - _F H _l /D _t      

Rapid assessment of oxygen transfer impact for Corynebacterium glutamicum

Oxygen supply is crucial in industrial application of microbial systems, such as Corynebacterium glutamicum, but oxygen transfer is often neglected in early strain characterizations, typically done under aerobic conditions. In this work, a new procedure for oxygen transfer screening is presented, assessing the impact of maximum oxygen transfer conditions (OTR_max) within microtiter plate-based cultivation for enhanced throughput. Oxygen-dependent growth and productivity were characterized for C. glutamicum ATCC13032 and C. glutamicum DM1933 (lysine producer). Biomass and lysine product yield are affected at OTR_max below 14 mmol L^?1 h^?1 in a standardized batch process, but not by further increase of OTR_max above this threshold value indicating a reasonable tradeoff between power input and oxygen transfer capacity OTR_max. The described oxygen transfer screening allows comparative determination of metabolic robustness against oxygen transfer limitation and serves identification of potential problems or opportunities later created during scale-up.