Dependency of growth yield,maintenance and K s-values on the dissolved oxygen concentration in continuous cultures of Azotobacter vinelandii

Azotobacter vinelandii was grown diazotrophically in sucrose-limited chemostat cultures at either 12, 48, 108, 144 or 192 M dissolved oxygen. Steady state protein levels and growth yield coefficients (Y) on sucrose increased with increasing dilution rate (D). Specific rate of sucrose consumption (q) increased in direct proportion to D. Maintenance coefficients (m) extrapolated from plots of q versus D, as well as from plots of 1/Y versus 1/D exhibited a nonlinear relationship to the dissolved oxygen concentration. Constant maximal theoretical growth yield coefficients (Y ^G) of 77.7 g cells per mol of sucrose consumed were extrapolated irrespective of differences in ambient oxygen concentration. For comparison, glucose-, as well as acetate-limited cultures were grown at 108 M oxygen. Fairly identical m- and Y ^G-values, when based on mol of substrate-carbon with glucose and sucrose grown cells, indicated that both substrates were used with the same efficiency. However, acetate-limited cultures showed significantly lower m- and, at comparable, D, higher Y-values than cultures limited by either sucrose or glucose. Substrate concentrations (K _s) required for half-maximal growth rates on sucrose were not constant, they increased when the ambient oxygen concentration was raised and, at a given oxygen concentration, when D was decreased. Since biomass levels varied in linear proportion to K _s these results are interpreted in terms of variable substrate uptake activity of the culture.Abbreviations D dilution rate - K _s substrate concentration required for half maximal growth rate - m maintenance coefficient - q specific rate of substrate consumption - Y growth yield coefficient - Y ^G maximum theoretical growth yield coefficient     

Biotransformation of cephalosporin C to 7-aminocephalosporanic acid with coimmobilized biocatalyst in a batch bioreactor

Biotransformation of cephalosporin C (CPS-C) to 7-aminocephalosporanic acid (7-ACA) was carried out with coimmobilized permeabilized cells of Trigonopsis variabilis and Pseudomonas species entrapped in Ca-pectate gel beads. Good aeration and stirring during the process was assured. The analysis of this complicated biochemical process in a heterogeneous system was based on the identification of individual effects (internal diffusion, reaction) running simultaneously. A spectrophotometric method was proposed for the determination of 7-(-ketoadipyl amido) cephalosporanic acid (CO-GL-7-ACA) and 7-ACA. The reaction-diffusion model containing dimensionless partial differential equations was solved by using the orthogonal collocation method. A good agreement between experimental values and values predicted by the mathematical model was obtained. Numerical simulations were performed on the basis of following the two assumptions:- several times higher activity of both cells,- hydrogen peroxide was continuously supplied in the bioreactor.List of Symbols A m² surface of the bead - c _i mol/dm³ concentration of component in the bead and/or in the solution - c _i0 mol/dm³ initial concentration of component in the solution - c _l0 mol/dm³ initial concentration of CPS-C in the solution - C _jl orthogonal collocation weights of the first derivation - D _ei m²/s effective diffusion coefficient of the components - D _jl orthogonal collocation weights of the second derivation - k ₅ dm³/(mol · s) kinetic parameter of non-enzyme reaction - K _inh mol/dm³ inhibition parameter for the first enzyme reaction - K _i dimensionless Michaelis constant for the first and second enzyme reaction, defined in Eq. (7) - K _l dimensionless inhibition parameter for the first enzyme reaction, defined in Eq. (7) - K _mi mol/dm³ Michaelis constant for the first and second enzyme reaction - n number of beads - P( _i ) symbol of dimensionless reaction rate, defined in Eq. (13) - r m radial coordinate inside the bead - R m radius of the bead - R(c _i ) mol/(dm³ · s) symbol for reaction rate, defined in Eq. (6) - t s time - V _max mol/(dm³ · s) max. reaction rate for the first and second enzyme reaction - V _L dm³ volume of solution excluding the space occupied by beads - voidage in batch bioreactor - _P porosity of the bead - i dimensionless effective diffusion coefficient of the components, defined in Eq. (7) - dimensionless time, defined in Eq. (7) - _mi Thiele modulus, defined in Eq. (7) - _i dimensionless concentration, defined in Eq. (7) - dimensionless radial position inside the bead, defined in Eq. (7) - _l0 initial dimension concentration of CPS-C, defined in Eq. (9), (10) - _i0 initial dimension concentration of component, defined in Eq. (9), (10) The authors wish to thank Dr. P. Gemeiner of Slovak Academy of Sciences for rendering of pectate gel. This work is supported by Ministry of Education (Grant No. 1/990 935/93).     

Glutamic acid production in an airlift reactor with net draft tube

Cultivation of Brevibacterium divaricatum for glutamic acid production in an airlift reactor with net draft tube was developed. Cell concentration gave an index for adding penicillin G. On-line estimation of total sugar concentration yielded an identified model which was used for determination of the substrate addition. Fermentation for glutamic acid production requires high oxygen concentration in the broth. The proposed reactor has the capability to provide sufficient oxygen for the fermentation. Since the reactor is suitable for fed-batch culture, the cultivation of B. divaricatum for glutamic acid production in the proposed reactor is successfully carried out.List of Symbols a system parameter - b system parameter - C _c,in mole fraction carbon dioxide in the gas inlet - C _c,out mole fraction carbon dioxide in the gas outlet - C _L mole/dm³ oxygen concentration in liquid phase - C _L ^* mole/dm³ saturated oxygen concentration in liquid phase - C _0,in mole fraction of oxygen in the gas inlet - C _0,out mole fraction of oxygen in the gas outlet - CPR mole/h/dm³ carbon dioxide production rate based on total broth - E(t) error signal - F _in mole/h inlet gas flow rate - k ₁ constant defined by Eq. (4) - k ₂ constant defined by Eq. (5) - k _L a 1/h volumetric mass transfer coefficient of gas-liquid phase - OUR mole/h/dm³ oxygen uptake rate based on total broth - P atm pressure in the reactor - t h time - TS _c g total sugar consumption - TS _s g/dm³ set point of total sugar concentration - TS _* g/dm³ reference value of total sugar concentration - TS(t) g/dm³ total sugar concentration in the broth at timet - u(t) cm³/min feed rate at timet - V dm³ total broth volume - VVM (dm³/min)/dm³ flow rate per unit liquid volume - a negative constant defined by Eq. (7)     

A method for estimating oxygen availability of stationary plant cell cultures in liquid media

A method for estimating the oxygen availability in plant cell cultures grown in stationary liquid media (e.g. many protoplast cultures) was developed. The method is based on short-term measurements of respiration rate versus oxygen concentration on a sample of cells, suspended in liquid media. From such data it is possible to estimate the oxygen concentration at the bottom of a stagnant liquid culture, by calculating the amount of oxygen reaching the cells by diffusion. As an example, rape (Brassica napus L. cv. Omega) hypocotyl protoplasts were grown with different oxygen concentrations at the site of the cells, obtained by varying the cell density, the height of the liquid layer and the oxygen content of the gas phase. The number of surviving calli was positively correlated with the estimated oxygen availability in the range between 60 and 350 M O₂, below 60 M all cells died. This indicates that oxygen availability can be a limiting factor in the range usually encountered in protoplast cultures, and that the method can be useful when designing optimal growth conditions for stationary cultures of plant cells.Abbreviations C₁ bulk oxygen concentration in agitated medium - C_o oxygen concentration in medium at the gas-liquid interface, in equilibrium with the gas - C_x oxygen concentration at cell level - D diffusion constant of oxygen in water - K_La oxygen transfer rate - l height of liquid above cells - n number of cells per ml - R_x respiration rate per cell     

The reduction of xylose to xylitol by Candida guilliermondii and Candida parapsilosis: Incidence of oxygen and pH

Summary The ability of C. guilliermondii and C. parapsilosis to ferment xylose to xylitol was evaluated under different oxygen transfer rates in order to enhance the xylitol yield. In C. guilliermondii, a maximal xylitol yield of 0.66 g/g was obtained when oxygen transfer rate was 2.2 mmol/l.h. Optimal conditions to produce xylitol by C. parapsilosis (0.75 g/g) arose from cultures at pH 4.75 with 0.4 mmoles of oxygen/l.h. The response of the yeasts to anaerobic conditions has shown that oxygen was required for xylose metabolism.Nomenclature max maximum specific growth rate (per hour) - qSmax maximum specific rate of xylose consumption (g xylose per g dry biomass per hour) - qpmax maximum specific productivity of xylitol (g xylitol per g dry biomass per hour) - Qp average volumetric productivity of xylitol (g xylitol per liter per hour) - Y_P/S xylitol yield (g xylitol per g substrate utilized) - Y_P'/S glycerol yield (g glycerol per g substrate utilized) - Y_X/S biomass yield (g dry biomass per g substrate utilized)     

A rationale for the appropriate amount of inoculum in ready biodegradability tests

Several screening methods at the so-called ready biodegradability level are suitable to test poorly soluble substances. Typical for these tests is that mineralization is evaluated from monitoring oxygen uptake or carbon dioxide production. Unfortunately, they suffer from a rather low precision in the calculated percentage of mineralization caused by subtracting a too high inoculum control measurement from the response in the test system. Criteria for blank oxygen consumption, due to the metabolic activity of the inoculum, are proposed from which maximum amounts of activated sludge or secondary effluent per litre test medium can be derived to be used as an appropriate inoculum. Both for current and future standardized tests the precision of the method can be kept within acceptable margins. Inoculum material was sampled from 40 communal biological waste water treatment plants. From endogenous respiration rates it was derived that the concentration of secondary effluent in the Closed Bottle Test can be increased up to 50 mL/L but that in respirometry tests inoculated with activated sludge the appropriate concentration is 10 mg/L dry matter or below, depending of the design of the test system.List of abbreviations BOD biological oxygen demand - CBT Closed Bottle Test - C _as inoculum concentration in mg dry solids of activated sludge per litre test medium - C _ef inoculum concentration in ml secondary effluent per litre test medium - C _ss dry weight content of activated sludge (g/L) - CFU colony forming units - DO_7d dissolved oxygen concentration (mg/L) after 7 days - ISO International Organization for Standardization - NEN Dutch Organization for Standardization - O _c oxygen capacity in mg oxygen per litre vessel volume - OECD Organisation for Economic Co-operation and Development - Ox _as oxygen consumption after one week in mg oxygen per mg dry weight activated sludge - Ox _ef oxygen consumption after one week in mg oxygen per mL secondary effluent - Ox _ef [n] oxygen consumption after one week in mg oxygen per n mL secondary effluent - Ox _flask oxygen uptake in mg per litre flask volume - RBT Ready Biodegradability Test - SLR sludge loading rate in kg O₂/kg dry weight·d - ThOD theoretical oxygen demand - TPCBT Two Phase Closed Bottle Test - V _a volumes of air and water per litre vessel - V _w volume, respectively - _a concentration of oxygen in air at 20° C and 101.5 kPa - _s saturation oxygen concentration in te aqueous phase     

Applications of modelling for bioprocess design and control in industrial production

The on-line measurement of the relevant parameters and the control conception for three production processes for fine chemicals by fermentation and biotransformation at the 15 m³ scale were developed. The models describe the bioprocesses which successfully result in fully automated manufacturing steps. Modelling also proved to be a valuable tool for a better insight into biochemical fundamentals of the processes. Moreover, proper use of data logging, modelling and process control was important for quality, since two processes were controlled on-line and quality relevant deviations were registered early. Finally, combining modelling with simulation, we could drastically reduce both development time and cost.List of Symbols F l/h flux - V l volume - U ₀ g/l nicotinonitrile concentration influx - U g/l actual nicotinonitrile concentration - q _ug/gh specific educt (=nicotinonitrile) transformation rate - x g/l biocatalyst concentration - p ₀ g/l nicotinamide concentration influx - p g/l actual nicotinamide concentration - q _pg/gh specific product (=nicotinamide) formation rate - k parameter loss of activity - q _{u, max}g/gh max. specific educt transformation rate - K _ug/l saturation constant for nicotinonitrile - K _ig/l inhibition constant for nicotinonitrile - K _iig/l inhibition constant for nicotinamide - MW _Ag/mol molecular weight for nicotinonitrile - MW _Bg/mol molecular weight for nicotinamide - NS Nicotinic acid - 6-HNS 6-Hydroxynicotinic acid - r _{NS, 6HNS} g/lh 6-HNS production rate - r _{6HNS, X} g/lh biomass production rate - r _{NS, 6HNS, max} g/lh max. 6-HNS production rate - S _NS g/l actual NS concentration - K _{S, NS} g/l saturation constant for NS - K _{i, 6HNS} g/l inhibition constant for 6-HNS - K _o2 g/l saturation constant for oxygen - r _{6HNS, X, max} g/lh max. biomass production rate - S _6HNS g/l actual 6-HNS concentration - K _{ii, NS} g/l inhibition constant for NS - RQ mol/mol respiration quotient - S _xylg/l actual xylene concentration - K _{i, xyl}g/ inhibition constant for xylene - K _{i, DMPY}g/ inhibition constant for 2,5-dimethylpyrazine - r _Xg/lh biomass production rate - r _{X, max}g/lh max. biomass production rate - K _{s, xyl}g/l saturation constant for xylene - S _DMPYg/l actual concentration of DMPY - K _{i, MPCA}g/ inhibition constant for MPCA - K _O2g/ saturation constant for oxygen - S _MPCAg/l actual MPCA concentration - S _O2g/l actual oxygen concentration - r _MPCAg/lh MPCA production rate - r _{MPCA, max}g/lh max. MPCA production rate - k _lgl inhibition constant for the intermediates - k _{s, DMPY}gl saturation constant for DMPY     

A theoretical model for studying the rate of oxygenation of blood in pulmonary capillaries

A mathematical analysis of the process of gas exchange in the lung is presented taking into account the transport mechanisms of molecular diffusion, convection and facilitated diffusion of the species due to haemoglobin. Since the rate at which blood gets oxygenated in the pulmonary capillaries is very fast, it is difficult to set up an experimental study to determine the effects of various parameters on equilibration rate. The proposed study is aimed at determining the effects of various physiological parameters on equilibration rate in pathological conditions.Among the significant results are that 1. dissolved oxygen takes longer to achieve equilibration across the pulmonary membrane and carbon dioxide attains equilibration faster, 2. the equilibration length increases with increase in blood velocity, haemoglobin concentration, calibre of pulmonary capillaries and fall in alveolar PO₂, 3. the alveolar PCO₂ and forward and backward reaction rates of haemoglobin with CO₂ do not materially affect the equilibration rate or length. 4. At complete equilibration, by the end of the pulmonary capillary 92% of the total haemoglobin has combined with oxygen and 8% free pigment is left which is present as carbamino haemoglobin, met haemoglobin, carboxy haemoglobin etc.These results are of some importance for anaemic conditions, muscular exercise, meditation, altitude physiology, hypo-ventilation, hyperventilation, etc.Symbols H⁺ hydrogen ion - O₂ oxygen - CO₂ carbondioxide - HbO₂ oxyhaemoglobin - HbCO₂ carbaminohaemoglobin - PO₂ partial pressure of O₂ - PCO₂ partial pressure of CO₂ - PaO₂ O₂ tension in arterial blood - PaCO₂ CO₂ tension in arterial blood - k₁ forward rate constant for Eq. (1) - k₂ backward rate constant for Eq. (1) - m₁ forward rate constant for Eq. (2) - m₂ backward rate constant for Eq. (2) - k equilibration rate - a radius of the capillary - Q velocity of blood - L length of the capillary - D₀ diffusion coefficient of O₂ - D_c diffusion coefficient of CO₂ - D_H diffusion coefficient of Hb - H total haemoglobin concentration - A matrix - c₁ concentration of dissolved O₂ in blood - c₂ concentration of HbO₂ in blood - c₃ concentration of dissolved CO₂ in blood - c₄ concentration of HbCO₂ in blood - c₅ concentration of haemoglobin - c1alv concentration of O₂ in the alveolar region - c_3alv concentration of CO₂ in the alveolar region - c_iven concentration of the ith species in venous blood - c_iart concentrations of the ith species in arterial blood - F _is concentrations of the species in dimensionless form - J₀, I₀ Bessel's functions - P_alvO₂ tension of O₂ in alveolar region - P_alvCO₂ tension of CO₂ in alveolar region.     

The effect of pH on kinetic and yield parameters during the ethanolic fermentation of D-xylose with Pachysolen tannophilus

We have studied the ethanolic fermentation of D-xylose with Pachysolen tannophilus in batch cultures. We propose a model to predict variations in D-xylose consumed, and biomass and ethanol produced, in which we include parameters for the specific growth rate, for the consumption of D-xylose and production of ethanol either related or not to growth.The ideal initial pH for ethanol production turned out to be 4.5. At this pH value the net specific growth rate was 0.26 h^–1, biomass yield was 0.16 g.g^–1, the cell-maintenance coefficient was 0.073 g.g^–1.h^–1, the parameter for ethanol production non-related to growth was 0.064 g.g^–1,h^–1 and the maximum ethanol yield was 0.32 g.g^–1.List of Symbols A _c Carbon atomic weight - a _d1/h Specific cell-maintenance rate defined in Eq. (8) - c Mass fraction of carbon in the biomass - E g/l Ethanol concentration - f _x Correction factor defined in Eq. (13) - f _x Correction factor defined in Eq. (13) - f _xi Correction factor defined in Eq. (14) - k _d1/h Death constant - M _E Ethanol molecular weight - M _s Xylose molecular weight - M _xi Xylitol molecular weight - m g xylose/g biomass Maintenance coefficient for substrate - m _dg xylose/g biomass Maintenance coefficient when k _d - q _Eg ethanol/g biomass. Specific ethanol production rate - s g/l Residual xylose concentration - s ₀ g/l Initial xylose concentration - t h Time - x g/l Biomass concentration - x ₀ g/l Initial biomass concentration - Y _E/sg ethanol/g xylose Instantaneous ethanol yield - ¯Y _E/sg ethanol/g xylose Mean ethanol yield - Y _E ^s/T g ethanol/g xylose Theoretical ethanol yield - Y _E ^s/* g ethanol/g xylose Corrected instantaneous ethanol yield - ¯Y _E ^s/* g ethanol/g xylose Corrected mean ethanol yield - Y _x/sg biomass/g xylose Biomass yield - ¯Y _xi/sg xylitol/g xylose Mean xylitol yield Greek Letters g ethanol/g biomass Growth-associated product formation parameter - g ethanol/g biomass.h Non-growth-associated product formation parameter - _dg ethanol/g biomass.h Non-growth-associated product formation parameter when k _d0 - h Variable defined in Eq. (6) or Eq. (7) - 1/h Specific growth rate - _m1/h Maximum specific growth rate     

Regulation of intracellular H+ balance in Zymomonas mobilis 113 during the shift from anaerobic to aerobic conditions

Summary The energetics, enzyme activities and end-product synthesis of Zymomonas mobilis 113 in continuous culture were studied after the shift from an anaerobic to an aerobic environment. Aeration diminished ethanol yield and lactic acid concentration, but increased glucose consumption rate and production of acetic acid. After the shift to aerobic conditions reduced nicotinamide adenine dinucleotide (phosphate) [NAD(P)H]-oxidase activity was stimulated. Washed cell suspensions consumed oxygen with glucose, lactate and ethanol as substrates. The aerobic Z. mobilis 113 regulated their intracellular redox balance by production and reoxidation of the end products, coupled with the formation of NAD(P)H. An increase in transmembrane pH gradient (pH) and a decrease in intracellular ATP concentration were observed after the shift to aerobic conditions. At low medium redox potential (Eh) values the H⁺ balance was regulated in an energy-independent way via end-product excretion. Under aerobic conditions this was supplemented by ATP-dependent H⁺ excretion by the membrane H⁺-ATPase.Abbreviations D dilution rate (h^-1) - S ₀ initial glucose concentration (g/l) - Y _x/s growth yield (g/mol) - Y _p/s product yield (g/g) - q _s specific rate of substrate utilization (g/g per hour) - q _p specific rate of ethanol formation (g/g per hour) - qo ₂ specific rate of CO₂ production (mmol/g per hour) - specific growth rate (h^-1) - X dry biomass concentration (g/l) - Eh redox potential of culture medium (mV) - pH transmembrane pH gradient (pH units) - pH_in intracellular pH - SASE sum of activities of specific enmymes of Entner-Doudoroff pathway     

A mathematical model for solid state fermentation in tray bioreactors

A simple mathematical model for the interaction of mass transport with biochemical reaction in solid state fermentations (SSF) in static tray type bioreactors under isothermal conditions has been developed. The analysis has enabled scientific explanations to a number of practical observations, through the concept of critical substrate bed thickness. The model will be most useful in the prediction of the concentration gradients as also in efficient design of these bioreactors.List of Symbols C g/cm³ Oxygen concentration in the bed - C _g g/cm³ Atmospheric oxygen concentration - C ^* Dimensionless oxygen concentration, C/C _g - D _e cm²/h Effective diffusivity - H cm Bed thickness or height - H _c cm Critical bed thickness or height - H _m cm Maximum height of zone of zero oxygen concentration - p _i mg/(g · h) Productivity (Eq. 13) - R g/(cm³ · h) Biochemical reaction rate - t h Fermentation time - t ^* Dimensionless time, D _e t/H² - X mg/cm³ Biomass concentration - X _max mg/cm³ Maximum biomass concentration - y Dimensionless thickness or height, (y = z/H) - y cm Thickness of zone of zero oxygen concentration (Eq. 12) - Y Yield coefficient - z cm Bed thickness or height along tray axis - Bed void fraction - _max h^–1 Specific growth rate - Thiele modulus      

Biotransformation of cephalosporin C to 7-aminocephalosporanic acid with coimmobilized biocatalyst in a batch bioreactor

The permeabilized cells of Trigonopsis variabilis CCY 15-1-3 having D-amino acid oxidase (DAAO) activity were used to convert cephalosporin C (CPS-C) into 7-(-ketoadipyl amido) cephalosporanic acid (CO-GL-7-ACA) in a batch bioreactor with good aeration and stirring during the process. The deacylation of 7--(4-carboxybutanamido)-cephalosporanic acid (GL-7-ACA) to 7-cephalosporanic acid (7-ACA) by permeabilized cells of Pseudomonas species 3635 having 4--(4-carboxybutamido)-cephalosporanic acid acylase (GL-7-ACA acylase) activity was performed in a batch bioreactor. A spectrophotometric method for the determination of CO-GL-7-ACA and 7-ACA was proposed. Experimental data were fitted by non-linear regression with parameters optimization. The sorption method (without reaction) was applied for the determination of cephalosporin effective diffusion coefficients in Ca-pectate gel beads. These beads were prepared by dropping a potassium pectate gel suspension of inactive permeabilized cells of Trigonopsis variabilis and Pseudomonas species, crosslinked with glutaraldehyde, into a stirred 0.2 M calcium chloride solution. Concentrations of appropriate cephem components were measured by the refractive method. Values of effective diffusion coefficients were calculated by the Fibbonacci optimization method.List of Symbols c _L mol/dm³ concentration on the surface of a bead - c _L0 mol/dm³ initial cephalosporin concentration - c _L mol/dm³ equilibrium cephalosporin concentration in the solution - c _s1 mol/dm³ concentration of CPS-C - c _s2 mol/dm³ concentration of GL-7-ACA - D _ei m²/s effective diffusion coefficient of the components - K _i mol/dm³ inhibition parameter in Eq. (2) - K _{m i} mol/dm³ Michaelis constant in Eq. (1) - K _{m 2} mol/dm³ Michaelis constant in Eq. (2) - n number of beads - q _n nonzero positive roots in Eq. (7) - r ₁ mol/(dm³·s) rate of the conversion of CPS-S to CO-GL-7-ACA - r ₂ mol/(dm³·s) rate of the conversion of GL-7-ACA to 7-ACA - R m radius of the bead - S( ) symbol for total residual sum of squares in Eq. (1) - t s time - V _{m 1} mol/(dm³·s) max. reaction rate in Eq. (1) - V _{m 2} mol/(dm³·s) max. reaction rate in Eq. (2) - V _L dm³ volume of the solution excluding the space occupied by beads - V _s dm³ volume of beads - y _i mol/(dm³ · s) symbol for experimental data in Eq. (1) - _i mol/(dm³· s) symbol for calculated data in Eq. (1) - _P porosity, defined by Eq. (5) - dimensionless parameter, defined by Eq. (6) The authors wish to thank Dr. P. Gemeiner of Slovak Academy of Sciences for rendering of pectate gel. This work is supported by Ministry of Education (Grant No. 1/990 935/93)     

Hyperkinetic nutrient uptake byCandida intermedia

Summary After pulsing steady state cultures ofCandida intermedia with pure sucrose, or sucrose adequately supplemented with minerals (2–4 g/l), high substrate uptake rates and both an elevated oxygen consumption and CO₂-production rate were observed.The rate at which the concentration of the residual sugar in the culture broth fell rapidly to reach the original steady state concentration depended on the amount of sugar administered. The added sucrose is stored by the yeast cell until it is metabolized.This phenomenon known as adsorption, has also been observed in the activated sludge process. An elevated O₂-demand can approximately be deduced from the sucrose uptake followed by storage in the cell. According to existing models in waste water technology the substrate uptake after a pulse shows saturation behaviour.Since oxygen uptake and CO₂-evolution are widely used parameters in computer controlled fermentations, the consequences of this behaviour will be discussed.In contrary to existing models about monosaccharide and disaccharide uptake by yeast cells, we found, that sucrose is incorporated in the cell as such and not hydrolyzed outside the cell as postulated by de la Fuente and Sols (1962).     

Conversion of cellulose into fungal cell mass

Summary Chaetomium cellulolyticum (ATCC 32319) was cultivated on glucose, Avicel and/or Sigmacell in a 20-1 stirred tank batch reactor. The substrate (cellulose) concentration, the cell mass concentration (through protein and/or nitrogen content), reducing sugar concentration, the enzyme activity, the alkali consumption rate, the dissolved O₂ and CO₂ concentrations in the outlet gas were measured. The specific growth rate, the substrate yield coefficient, cell productivity, the oxygen consumption rate, the CO₂ production rate and the volumetric mass transfer coefficient were determined. At the beginning of the growth phase the oxygen utilization rate exhibits a sharp maximum. This maximum could be used to start process control. Because of the long lag phase periodic batch operation is recommended.Symbols CP cell protein concentration (g l^–1) - FPA FP enzyme activity (IU l^–1) - GP dissolved protein concentration (g l^–1) - IU international unit of enzyme activity - k_La volumetric mass tranfer coefficient (h^–1) - LG alkali (1 n NaOH) consumption (ml) - LGX specific alkali consumption rate per cell mass (ml g^–1 h^–1) - P cell mass productivity (g l^–1 h^–1) - specific oxygen consumption rate per cell mass (g g^–1 h^–1) - Q aeration rate (volumetric gas flow rate per volume of medium, vvm) (min^–1) - N impeller speed (revolution per minute, rpm) (min^–1) - S substrate concentration (g l^–1) - S⁰ S at t_F=0 (g l^–1) - S₀ S in feed (g l^–1) - SR acid consumption (ml) - TDW total dry weight (g l^–1) - T temperature (° C) - t_F cultivation time (h) - U substrate conversion - X cell mass concentration (g l^–1) - Y_X/S vield coefficient - specific growth rate (h^–1) - _m maximum specific growth rate (h^–1)     

Effect of bioreactor configuration on substrate uptake by cell suspension cultures of the plant Eschscholtzia californica

Summary The uptake of carbohydrates and oxygen by cell suspension cultures of the plant Eschscholtzia californica (California poppy) was studied in relation to biomass production in shake flasks, a 1-1 stirred-tank bioreactor and a 1-1 pneumatically agitated bioreactor. The sequence of carbohydrate uptake was similar in all cases, with sucrose hydrolysis occurring followed by the preferential uptake of glucose. The uptake of fructose was found to be affected by the oxygen supply rate. Carbohydrate utilization occurred at a slower rate in the bioreactors. Apparent biomass yields, Y _X/S, ranged from 0.42 to 0.50 g biomass/g carbohydrate, while true biomass yields, Y _X/S, were about 0.69 g/g. The maintenance coefficient for carbohydrate, m _S, ranged between 0.002 and 0.008 g/dry weight (DW) per hour. The maximum measured specific oxygen uptake rate was 0.56 mmol O₂/g DW per hour and occurred early in the growth stage. The decline in specific uptake rate coincided with a decline in cell viability. The oxygen uptake rate was faster in shake flasks, corresponding to the higher growth rate obtained. The true growth yield on oxygen, YX/O₂, was calculated to range from 0.83 to 1.23 g biomass/g O₂, while the maintenance coefficient, mO₂, ranged from 0.15 to 0.25 mmol O₂/g DW per hour. The growth yields for oxygen determined from the stoichiometry of an elemental balance were within 10% of those calculated from experimental data. Offprint requests to: Raymond L. Legge     

Identification and physiological characterization of the nitrogen fixing bacterium Corynebacterium autotrophicum GZ 29

The coryneform hydrogen bacterium strain GZ 29, assigned to Corynebacterium autotrophicum fixed molecular nitrogen under autotrophic (H₂, CO₂) as well as under heterotrophic (sucrose) conditions. Physiological parameters of nitrogen fixation were measured under heterotrophic conditions. The optimal dissolved oxygen concentration for cells grown in a fermenter with N₂ was rather low (0.14 mg O₂/l) compared with cells grown in the presence of NH ₄ ⁺ (4.45 mg O₂/l). C. autotrophicum GZ 29 had a doubling time of 3.7 h at 30°C with N₂ as N-source and sucrose as carbon source and at optimal pO₂. Acetylene reduction reached values of 12 nmoles of ethylene produced/minxmg protein. Although the oxygen concentration in the growing culture was kept constant, the optimal dissolved oxygen tension for the acetylene reduction assay shifted to higher pO₂-values. The overall efficiency of nitrogen fixation amounted to 22 mg N fixed/g sucrose consumed; it reached a maximal value of 65 mg N fixed/g sucrose consumed at the beginning of the exponential growth phase. Intact cells reduced acetylene even under anaerobic test conditions; further anaerobic metabolic activity could not be ascertained so far.     

Optimization of fed-batch culture by dynamic programming and regression analysis

Summary An algorithm for the optimization of a fermentation process was studied using the combination of dynamic programming and linear predictive procedure by regression analysis. It was applied to the fed-batch culture for glutamic acid production with ethanol feeding, the results of which proved that it was effective for the optimization problems.Nomenclature a _i , b _i , c _i , d _i ;i = 1 2 or 3: Partial regression coefficients derived by multiple regression analysis ( - ) - E : Euclid distance ( - ) - F : Volumetric feed rate (l/hr) - f : Defined by Eq. (13) (g-glutamic acid) - G : Concentration of glutamic acid (g/l) - G* : Aeration rate (l/hr) - J : Objective function defined by Eq. (12) (g-glutamic acid) - N : Number of stage ( - ) - P : Defined by Eq. (14) (g-glutamic acid) - Q : Metabolic activity of the culture, in this case Q = Q _{CO 2} (mole CO₂/g-cell hr) - S : Ethanol concentration in culture broth (g/l) - S _Q : Ethanol concentration in feed (g/l) - S* : Ethanol concentration in effluent gas (g/l) - t : Culture time (hr) - t _o : Initial culture time (hr) - V : Volume of culture broth (l) - X : Cell concentration (g/l) - X : State vector (X, S, Q, V) - : Rate of Q _{CO 2} change (mole CO₂/g-cell·h²) - : Specific growth rate of microorganisms (hr^–1) - : Specific production rate of glutamic acid (g-glutamic acid/g-cell·hr) - : Specific consumption rate of ethanol (g-ethanol/g-cell·hr) - : Standard deviation ( - ) This optimization procedure was presented in preliminary form at the 45th Annual Meeting of the Soc. of Chem. Engrs., Japan, Osaka, C105 (1980).     

Simulation of the dynamics in the Baker's yeast process

Simulation of the dynamics in a fed batch process for production of Baker's yeast is discussed and applied. Experimental evidences are presented for a model of the energy metabolism. The model involves the concept of a maximum respiratory capacity of the cell. If the sugar concentration is increased above a critical value, corresponding to a critical rate of glycolysis and a maximum rate of respiration, then all additional sugar consumed at higher sugar concentrations is converted into ethanol.In a fed batch process with constant sugar feed the sugar concentration declines slowly. If ethanol is present when the sugar concentration declines below the critical value of 110 mg/dm³ fructose +glucose the metabolism switches rapidly into combined oxidation of sugar and ethanol. Thus, no diauxic growth is involved under process conditions. The rate of ethanol consumption is determined by the free capacity of respiration under these conditions. The invertase activity of the cells was found to be so high that mainly fructose and glucose were present in the medium, typically in the concentration range around 100 mg/dm³. These components are consumed at the same rate but with fructose at a higher concentration, indicating a higher K _s for fructose consumption.The model was used in simulation experiments to demonstrate the dynamics of the Baker's yeast process and the influence of different process conditions.List of Symbols DOT % air sat dissolved oxygen tension - F dm³/h rate of inlet medium flow - H kg/(dm³ % air sat.) oxygen solubility - K kg/m³ saturation constant specified by index - K _L a 1/h volumetric oxygen transfer coefficient - m g/(g · h) maintenance coefficient specified by index - P kg/(m³ · h) mean productivity of biomass in the process - q g/(g · h) specific consumption or production rate - S kg/m³ concentration of sugar in reactor - S ₀ kg/m³ concentration of inlet medium sugar medium t h process time - V dm³ medium volume - X kg/m³ concentration of biomass - Y g/g yield coefficient specified by index - 1/h specific growth rate Index aa anaerobic condition - c critical value - e ethanol - ec ethanol consumption - ep ethanol production - max maximum value - o oxygen - oe oxygen for growth on ethanol - os oxygen for growth on sugar - s sugar - x biomass     

Data consistency,yield and maintenance coefficient for the growth of Candida lypoytica and Pseudomonas aeruginosa on n-hexadecane

Summary When more than the minimum number of variables are measured, and measurement error is taken into account, the results of parameter estimation depend on which of the measured variables are selected for this purpose. The reparameterization of Pirt's models for growth produces multiresponse models with common parameters. By using the covariate adjustment technique, a unit variate linear model with covariates is obtained. This allows a combined point and interval estimates of biomass energetic yield and maintenance coefficient to be obtained using standard multiple regression programmes. When this method was applied using form I and form II of the Pirt's models, good combined estimates were obtained and compared. Using data from the literature for Candida lipolytica produced reliable results. However, for Pseudomonas aeruginosa, which has been known to produce intermediate products, a modified Pirt's model is required for a good estimate of the biomass energetic yield.Nomenclature a Mole of ammonia per quantity of organic substrate containing 1 g atom carbon, g mole/g atom carbon - b Moles of oxygen per quantity of organic substrate containing 1 g atom carbon, g mole/g atom carbon - c Moles of water per quantity of organic substrate containing 1 g atom carbon, g mole/g atom carbon; no of covariates included in model - d Moles of carbon dioxide per quantity of organic substrate containing 1 g atom carbon, g mole/g atom carbon - e _i Error terms in Eqs. (6–8) - l Atomic ratio of oxygen to carbon in organic substrate, dimensionless - m Atomic ratio of hydrogen to carbon in organic substrate, dimensionless - m _e Rate of organic substrate consumption for maintenance, g equiv. of available electrons in biomass (h) or kcal/Kcal of biomass(h) - n Atomic ratio of oxygen to carbon in biomass, dimensionless - p Atomic ratio of hydrogen to carbon in biomass, dimensionless - Q _{CO 2} Rate of evolution of carbon dioxide, g moles/g dry wt (h) - Q _{O 2} Rate of oxygen consumption, g moles/g dry wt (h) - Q _s Rate of organic substrate consumption g/g dry wt (h) - q Atomic ratio of nitrogen to carbon in biomass, dimensionless - r Atom ratio of hydrogen to carbon in products, dimensionless; the number of parameters of interest - s Atomic ratio of oxygen to carbon in products, dimensionless - t Atomic ratio of nitrogen to carbon in products, dimensionless - r Mean of k responses in Eq. (10) - x _ki Kth response in the ith observation - y _c Biomass carbon yield (fraction of organic substrate carbon in biomass), dimensionless - z _i Covariate matrix - z Fraction of organic substrate carbon in products, dimensionless - a _i Parameters associated with covariates - _s Reductance degree of biomass, equivalents of available electrons per gram atom carbon - Reductance degree of organic substrate, equivalents of available electrons per gram atom carbon - Fraction of energy in organic substrate which is evolved as heat, dimensionless - Fraction of available electrons transferred to biomass; biomass energetic yield - True growth yield - Specific growth rate, h^-1 - _p Fraction of available electrons incorporated into products; product energetic yield - Correlation coefficient - Mass fraction carbon - ² Mean square error of model (10)     

Continuous mass spectrometric measurement of dissolved H2, O2, and CO2 during chemolithoautotrophic growth of Alcaligenes eutrophus strain H 16

Summary Polarographic oxygen electrodes, a mass spectrometer with a membrane inlet system, and a redox electrode were used to measure dissolved H₂, O₂, and CO₂ continuously during chemolithoautotrophic cultivation of Alcaligenes eutrophus H 16. A mass spectrometer is a versatile instrument for measuring dissolved gases. Its dynamic characteristics are comparable to conventional sterilizable oxygen electrodes. A redox electrode combined with an oxygen electrode is a simple but somewhat limited sensor to measure dissolved H₂.Symbols and Abbreviations a Empirical constant [Eq. (1)] - b Empirical constant [Eq. (1)] - c Concentration - D Diffusion coefficient - E Redox potential direct electrode measurement - F Flow velocity - I Signal from amis spectrometer - k_La Volumetric transport coefficient - k_Lá Apparent volumetric transport coefficient - Q_max Maximal specific gas uptake rate - q Mean value of ratios of apparent k_Lá-values of two gases - q_F Ratio of diffusion coefficients - q_S Square root of ratio of diffusion coefficients - S Limiting substrate concentration - t Time - v Velocity - X Cell dry mass concentration - DSM Deutsche Sammlung für Mikroorganismen, Göttingen, F.R.G. - IL Polarographic electrode, Instrumentation Laboratories, SpA., Milan, Italy - WTW Polarographic electrode, Wissenschaftlich-Technische Werkstätten, Weilheim, FRG - MS Mass spectrometer - PHB Poly--hydroxybutyric acid Presented at the 1st European Congress on Biotechnology; Interlaken, Switzerland September 25–29, 1978