Two-substrates packed-bed bioreactors: inhibition of enzyme and competitive binding of substrate and product to a ligand

An analytical model is developed to describe the performance of a packed-bed immobilized enzyme reactor in which parallel processes take place. In particular, two-substrate reaction, inhibition of the enzyme by one of the reaction products, and binding of one substrate and/or one product to an added ligand are taken into account. In addition, substrates and product diffusion into the porous catalyst are also considered. Using this model, numerical simulations were performed. The results point to the fact that, when all the above processes occur concomitantly, a variety of performance characteristics can be obtained, depending on the particular values of the related parameters. Moreover, under certain conditions, the reactor performance can be improved by controlled addition of ligand.List of Symbols A total concentration of ligand - C _1,i concentration of Substrate-1 in the pores of stage i - C _2,i concentration of Substrate-2 in its free form in the pores of stage i - _2,i concentration of the Substrate-2-Ligand Complex in the pores of stage i - total concentration of Substrate-2 in the pores of stage i - _i concentration of the Product-Ligand Complex in the pores of stage i - concentration of the free Product in the pores of stage i - total concentration of the Product in the pores of stage i - internal (pore) diffusion coefficient for the Substrate-Ligand Complex - D ₁ internal (pore) diffusion coefficient of Substrate-1 - D ₂ internal (pore) diffusion coefficient of Substrate-2 - effective (pore) diffusion coefficient for Substrate-2 - internal (pore) diffusion coefficient for the Product - internal (pore) diffusion coefficient for the Product-Ligand Complex - effective (pore) diffusion coefficient for the Product - K thermodynamic equilibrium constant for binding Substrate-2 to Ligand - K _m,1,K _m,2 Michaelis constants for Substrates-1 and 2, respectively - effective Michaelis constant for Substrate-2 - K _p thermodynamic equilibrium constant for binding the reaction Product to Ligand - effective equilibrium constant for binding Substrate-2 to Ligand - effective equilibrium constant for binding the reaction Product to Ligand. - K _b inhibition constant - K _q inhibition constant - effective inhibition constant - effective inhibition constant - k _a, k _d association and dissociation rate constants for Substrate-2 — Ligand complex - association and dissociation constants for Product —Ligand complex - n total number of elementary stages in the reactor - Q volumetric flow rate throughout the reactor - R _j,i reaction rate of Substrate-j in stage i, in terms of volumetric units - S _1,0 concentration of Substrate-1 in the reactor feed - total concentration of Substrate-2 in the reactor feed - S _1,i–1,S _1,i concentration of Substrate-1 in the bulk phase leaving stages i–1 and i, respectively - S _2,i concentration of Substrate-2 in its free form, in the bulk phase leaving stage i - _2,i–1, _2,i concentration of Substrate-2 in the bulk phase leaving stage i–1 and i, respectively - total concentration of Substrate-2 in the bulk phase leaving stages i–1 and i, respectively - _i concentration of the Product-Ligand Complex in the bulk phase of stage i - concentration of free Product in the bulk phase of stage i - total concentration of Product in the bulk phase of stage i - V total volume of the reactor - V _m maximal reaction rate in terms of volumetric units - y axial coordinate of the pores - y ₀ depth of the pores Greek Symbols ₁ dimensionless parameter - dimensionless parameter - dimensionless parameter - ₁ dimensionless parameter - dimensionless parameter - _1,i dimensionless concentration of Substrate-1 in pores of stage i - dimensionless total concentration of Substrate-2 (in both free and bound form) in pores of stage i - dimensionless total concentration of the reaction product in the pores of stage i - ₁ dimensionless parameter - dimensionless parameter - dimensionless parameter - dimensionless parameter - dimensionless parameter - dimensionless position along the pore - volumetric packing density of catalytic particles (dimensionless) - porosity of the catalytic particles (dimensionless) - _1,i dimensionless concentration of Substrate-1 in the bulk phase of stage i - dimensionless total concentration of Substrate-2 (in both free and bound form) in the bulk phase of stage i     

Oxygenation of cell cultures

Submersed cultures are increasingly being used for fermentation with animal cells. Reactor design is particularly important in these operations, because of the sensitivity of the cells to shear. In addition to the usual aeration methods, open-pore membranes or pure diffusion membranes are used for oxygenation in order to avoid gas bubbles. The various oxygenation methods are described in the present article [1]. Design principles for surface aeration, bubble columns, loop reactors, and stirred tanks, as well as oxygenation with Accurel or silicone membranes, are presented and discussed specifically for the low oxygen inputs desired in cell cultures. The scale laws are formulated, and special reference is made to problems of scale up. The various oxygenation methods are finally compared on the basis of the design principles presented, with particular attention to mechanical stress on the cells and to the laws of scale translation.List of Symbols A Interfacial area - a =A/V, Specific interfacial area - c ^* Saturation concentration - c Gas concentration in the liquid phase - d Impeller diameter - d ₂ Outside diameter of tubular membrane - d ₁ Inside diameter of tubular membrane - d Diameter under stretched conditions - d _p Particle diameter - d _L Diameter of sparger holes - D Reactor diameter - D _L Draught tube diameter - Gas/liquid diffusion coefficient - e Eccentricity - Fr Froude number - G Mass flow - g Acceleration due to gravity - h Height of impeller blade - H Filling height - Hy Henry constant for the liquid phase - Hy _s Henry constant of the membrane material - k Overall mass transfer coefficient - k _L Gas-liquid interface mass transfer coefficient - L Length of the tubular membrane - L Length of the streched turbulare membrane - n Impeller speed - Ne P/ n³d⁵, Newton number - O₂-partial pressure in the membrane - O₂-partial pressure in the reactor - P Impeller power - q Gas throughput - r Cell specific respiration rate - Re Reynolds number - Sc , Schmidt number - Sh , Sherwood number - u Liquid velocity - Root mean square velocity of turbulent fluctuations Superficial gas velocity - V Filled reactor volume - V _s Sparged volume - X Cell concentration - Energy dissipation - Dynamic viscosity - Temperature - Kinematic viscosity - Density of the liquid - Surface tension - Shear stress     

Heat transfer in vertical perl mills

A model of heat transfer during grinding in vertical multi-disk perl mills has been proposed. Heat transfer intensity in such mills depends on thermal resistance in a boundary layer formed at the inner surface of mill tank wall. The layer thickness changes depending on process variables. Results obtained are presented in the form of a dimensionless correlation equation.List of Symbols C ball filling of the mill, - c _pw specific heat of cooling water, kJ/(kg K) - d disk diameter, m - d _k ball diameter, m - D inner diameter of the mill tank, m - G _w mass flow rate of cooling water, kg/s - h distance between impeller disks, m - n revolutions frequency of the impeller shaft, s^–1 - q heat flux density, kW/m² - Q _c total heat energy emitted in the mill, W - T temperature, K - T _w1 temperature of cooling water at the cooling jacket inlet, K - T _w2 cooling water temperature at the outlet, K - T _m average temperature inside the mill, K - T _s average temperature of the tank wall, K - u peripheral speed of the impeller disk, m/s - heat transfer coefficient, kW/(m²K) - boundary layer thickness, m - porosity of the lying bed, - _m porosity of the suspended bed, - _c liquid dynamic viscosity, Pa s - _cs liquid dynamic viscosity at wall temperature, Pa s - _c thermal conductivity coefficient of liquid, W/(mK) - _c liquid density, kg/m³ - _s solid density, kg/m³ Dimensionless Numbers Reynolds number for mixing process - Reynolds number for liquid parameters - Nusselt number for liquid parameters - Prandtl number for liquid parameters - modified Euler number     

On the appropriateness of use of a continuous formulation for the modelling of discrete multireactant systems following Michaëlis–Menten kinetics

The possibility of solving the mass balances to a multiplicity of substrates within a CSTR in the presence of a chemical reaction following Michaelis-Menten kinetics using the assumption that the discrete distribution of said substrates is well approximated by an equivalent continuous distribution on the molecular weight is explored. The applicability of such reasoning is tested with a convenient numerical example. In addition to providing the limiting behavior of the discrete formulation as the number of homologous substrates increases, the continuous formulation yields in general simpler functional forms for the final distribution of substrates than the discrete counterpart due to the recursive nature of the solution in the latter case.List of Symbols C{N. M} mol/m³ concentration of substrate containing N monomer residues each with molecular weight M - {N, M} normalized value of C{N. M} - C {M} mol/m³ da concentration of substrate of molecular weight M - _in normalized value of C {M} at the i-th iteration of a finite difference method - {M} normalized value of C {M} - C ₀{N.M} mol/m³ inlet concentration of substrate containing N monomer residues each with molecular weight M - {N ·M} normalized value of C₀{N. M} - _{0 i} normalized value of C ₀ {M} at the i-th iteration of a finite difference method - C ₀ {M} mol/m³ da initial concentration of substrate of molecular weight M - C _tot mol/m³ (constant) overall concentration of substrates (discrete model) - C _tot mol/m³ (constant) overall concentration of substrates (continuous model) - D deviation of the continuous approach relative to the discrete approach - i dummy integer variable - I arbitrary integration constant - j dummy integer variable - k dummy integer variable - K _m mol/m³ Michaëlis-Menten constant for the substrates - l dummy integer variable - M da molecular weight of substrate - M normalized value of M - M da maximum molecular weight of a reacting substrate - N number of monomer residues of a reacting substrate - N maximum number of monomer residues of a reacting substrate - N total number of increments for the finite difference method - Q m³/s volumetric flow rate of liquid through the reactor - S inert product molecule - S _i substrate containing i monomer residues - V m³ volume of the reactor - v _max mol/m³ s reaction rate under saturating conditions of the enzyme active site with substrate - v _max{N. M} mol/m³ s reaction rate under saturating conditions of the enzyme active site with substrate containing N monomer residues with molecular weight M - _max{N · M} dimensionless value of v_max{N. M} (discrete model) - _max{M} dimensionless value of v _max {M} (continuous model) - mol/m³ s molecular weight-averaged value of v_max (discrete model) - mol.da/m³s molecular weight-averaged value of v_max (continuous model) - v _max {M} mol.da/m³s reaction rate under saturating conditions of the enzyme active site with substrate with molecular weight M - _max {M} dimensionless value of v_max{M} - _{max, (i)} dimensionless value of v_max{M} at the i-th iteration of a finite difference method - v _max mol/m³ s reference constant value of v _max Greek Symbols dimensionless operating parameter (discrete distribution) - dimensionless operating parameter (continuous distribution) - M da (average) molecular weight of a monomeric subunit - M selected increment for the finite difference method - auxiliary corrective factor (discrete model)     

The electrochemical H+ gradient in the yeastRhodotorula glutinis

The electrochemical gradient of protons, , was estimated in the obligatory aerobic yeastRhodotorula glutinis in the pH₀ range from 3 to 8.5. The membrane potential, , was measured by steady-state distribution of the hydrophobic ions, tetraphenylphosphonium (TPP⁺) for negative above pH₀ 4.5, and thiocyanate (SCN^–) for positive below pH₀ 4.5. The chemical gradient of H⁺ was determined by measuring the chemical shift of intracellular P_i by³¹P-NMR at given pH₀ values. The values of pH_i increased almost linearly from 7.3 at pH₀ 3 to 7.8 at pH₀ 8.5. In the physiological pH₀ range from 3.5 to 6, was fairly constant at values between 17–18 KJ mol^–1, gradually decreasing at pH₀ above 6. In deenergized cells, the intracellular pH_i decreased to values as low as 6, regardless of whether the cell suspension was buffered at pH₀ 4.5 or 7.5. There was no membrane potential detectable in deenergized cells.     

A study on Na+-coupled oxidative phosphorylation: ATP formation supported by artificially imposed ΔpNa and ΔpK inVibrio alginolyticus cells

Addition of Na⁺ to the K⁺-loadedVibrio alginolyticus cells, creating a 250-fold Na⁺ gradient, is shown to induce a transient increase in the intracellular ATP concentration, which is abolished by the Na⁺/H⁺ antiporter, monensin. The pNa-supported ATP synthesis requires an additional driving force supplied by endogenous respiration or, alternatively, by a K⁺ gradient (high [K⁺] inside). In the former case, ATP formation is resistant to the protonophorous uncoupler. Dicyclohexylcarbodiimide and diethylstilbestrol, but not vanadate, completely inhibit Na⁺ pulse-induced ATP formation. The data agree with the assumption that Na⁺-ATP-synthase is involved in oxidative phosphorylation inV. alginolyticus. Interrelation of H⁺ and Na⁺ cycles in bacteria is discussed.Abbreviations and electrochemical gradients of H⁺ and Na⁺, respectively - transmembrane electric potential difference - pH, pNa, and pK concentration gradients of H⁺, Na⁺, and K⁺, respectively - CCCP carbonyl cyanidem-chlorophenylhydrazone - DCCD N,N-dicyclohexylcarbodiimide - DES diesthylstilbestrol - HQNO 2-heptyl-4-hydroxyquinolineN-oxide - Tricine N[2-hydroxy-1,1-bis(hydroxymethyl)ethyl]glycine     

Der hemmende Einfluß gleichzeitig bewegter Beuteattrappen auf das Beutefangverhalten der Erdkröte (Bufo bufo L.)

Zusammenfassung Durch simultane visuelle Bewegungsreize, die von mehreren Beutetieren (z.B. Mehlkäferlarven) ausgehen, wird der Beutefang der Erdkröte (Bufo bufo L.) gehemmt. An diese Verhaltensheobaehtung anknüpfend, wurde die Abhängigkeit dieses inhibitorischen Umfeldeffektes von verschiedenen visuellen Reizparametern im Attrappen versuch quantitativ gemessen: Im frontalen Gesichtsfeld der Kröte rotierte vor dunklem Hintergrund eine weiße, rechteckige, 2,5 × 20° große Beuteattrappe (Zentralattrappe, z) mit dem Rechteckzentrum im Drehpunkt. Zusätzlich konnten mehrere Kreisscheiben von 5 bzw. 10° (Peripherattrappen, p) um die Zentralattrappe bewegt werden.Die Beutefangaktivität R _z [Beutefangreaktionen x min^–1] auf die allein gebotene Zentralattrappe war bei einer Sehwinkelgeschwindigkeit v _s der distalen Attrappenkanten 10v _s30 [grad x see^–1] maximal und sank für kleinere oder größere Winkelgeschwindigkeiten wieder ab. Eine mit v _s=25 [grad x sec^–1] allein bewegte Peripherattrappe löste maximale Beutefangaktivität R _p aus. Mit zunehmender Anzahl n _p simultan bewegter Peripherattrappen sank die Beutefangaktivität ab.Mehrere, um den gleichen Drehpunkt bewegte Peripherattrappen, deren Abstand untereinander =10° betrug, blieben von der Kröte unbeantwortet. Sie bildeten ein inhibitorisches Umfeld und hemmten dadurch die Reaktion auf die gleichzeitig bewegte Zentralattrappe z. — Die im Simultanreizungsversuch gemessene Beutefangaktivität R _zp war abhängig vom Abstand [grad] zwischen Zentralattrappe und Peripherattrappen ( : Kürzester Abstand zwischen z und p): Für =10° war R _zp0 und stieg für >10° an. — Kontrollversuche, die jeweils auf die Simultanreizung mit z allein folgten (R _z), ließen eine -abhängige Nachhemmung erkennen. — Die hemmende Wirkung auf die Beantwortung von z war auch von der Sehwinkelgeschwindigkeit v _s der Peripherattrappen abhängig; sie war bei derjenigen Sehwinkelgeschwindigkeit (v _s=25 [grad × sec^–1]) maximal, mit der die Zentralattrappe, allein geboten, maximale Beutefangaktivität auslöste; für v _sg25 [grad × sec^–1] nahm die Hemmung wieder ab.Die Versuchsergebnisse lassen auf inhibitorische Verknüpfungen innerhalb des zentralen visuellen Systems schließen. Es wird vermutet, daß die Reiz-Verhaltens-reaktionsbeziehungen in den visuellen Simultanreizungsversuchen durch eine Art zentrale laterale Inhibition bestimmt werden.

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Inhibitory effect of simultaneously moved prey dummies on the prey catching behaviour of the common toad (Bufo bufo L.)

Summary The prey catching behaviour of the toad (Bufo bufo L.) is generally inhibited by simultaneously visual moving stimuli caused by a group of prey animals (mealworms). According to this behavioural observation the dependence of this inhibitory effect on several visual parameters were quantitatively measured in dummy experiments: in the frontal visual field of the toad a white rectangular prey dummy of 2,5×20° (central dummy, z) was rotating in a centre against dark background. In addition several disks of 5 or 10° diameter (peripheral dummies, p) could simultaneously rotate around the central dummy (Figs. 1 and 7).The prey catching activity R _z [catching reactions x min^–1] released by rotation of only the central dummy z increased with increasing angular velocity v _s of the stimulus distal edges, reaching a maximum for 10v_s30 [degrees x sec^–1] and decreasing for v _s>30 [degrees x sec^–1] (Fig. 5).A single peripheral dummy p, moved at v _s=25 [degrees x sec^–1], released maximal catching activity R _p. The activity R _p decreased with the increasing number n _p of simultaneously offered dummies (Fig. 6).The prey catching behaviour of the toad was inhibited, when several peripheral dummies p were moved around the centre with a distance =10° from each other. They caused an inhibitory field and they also inhibited the response to a simultaneously moved central dummy z. The prey catching activity, measured in experiments in which z and p rotated simultaneously, depends on the distance [degrees] between z and p ( being the shortest distance between z and p). For =10°, R _zp was zero; R _zp increased for >10° (Figs. 9 and 10). — Control experiments carried out with z allone — after having applied the simultaneous stimulation — showed a - dependent after-inhibition (Fig. 9). — The inhibitory effect on the response to z also depended on the angular velocity v _s of p; the inhibition was at a maximum for v _s25 [degrees x sec^–1], and it decreased for v _s25 [degrees x sec^–1] (Fig. 11).The experimental results suggest inhibitory interactions within the central visual system. It is supposed that the relation between stimulus and behavioural reaction in simultaneous stimulating experiments results from some kind of central nervous lateral inhibition.

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Mit Unterstützung der Deutschen Forschungsgemeinschaft (Ew 7/4+5).     

Apparent viscosity for non-Newtonian fermentation media in bioreactors

The apparent viscosity of non-Newtonian fermentation media is examined. The present state of this subject is discussed. The energy dissipation rate concept is used for a new evaluation of the apparent viscosity in bioreactors, i.e. stirred tank and bubble column bioreactors. The proposed definition of the apparent viscosity is compared with the definitions available in the literature.List of Symbols A _d m ² downcomer cross-sectional area - A _r m ² riser cross-sectional area - a m^–1 specific surface area - C constant in eq. (13) - D m column diameter - D _I m impeller diameter - g m s^–2 gravitational acceleration - h J m^–2 s^–1 K^–1 heat transfer coefficient - K Pa s ⁿ consistency index in a power-law model - k constant in eq. (3) - k _L m s ^–1 liquid-phase mass transfer coefficient - N s^–1 impeller speed - n flow index in a power-law model - P W power input - Re Reynolds number ND _I ^/2 /(/) - U _sg m s ^–1 superficial gas velocity - (U _sg ) _r m s^–1 superficial gas velocity based on riser - V-m³ liquid volume - v ₀ m s^–1 friction velocity Greek Symbols s^–1 shear rate - _c s^–1 characteristic shear rate - W kg^–1 energy dissipation rate per unit mass - W kg^–1 characteristic energy dissipation rate per unit mass - Pa s viscosity - _app Pa s apparent viscosity - kg m^–3 density - Pa shear stress     

Relationship between the octanol-water partition coefficient of tertiary amines and their effect of ‘selective’ uncoupling of photophosphorylation

A series of tertiary amines was investigated for effects on the transmembrane proton potential difference ( H), on photophosphorylation and on electron-flux control related to the intrathylakoid proton potential ( H_I), using isolated chloroplasts ofSpinacia oleracea L. As indicated by 9-aminoacridine fluorescence and [14C]methylamine uptake, all amines studied inhibited a build-up of H and, in parallel, ATP synthesis. Even when H was low, strong H₁-dependent electron-flux control was observed under the influence of tertiary amines. The strength of flux control in the presence of low H and the effectiveness of inhibition of ATP synthesis linearly increased with the lipophilicity of the amines. The most effective of the amines tested caused 50% inhibition of ATP synthesis at a concentration of 6 M, which is about 1000-fold lower than the concentration required for inhibition by methylamine. The data presented indicate the existence of two proton domains in the thylakoid vesicles, one of them feeding the ATP-synthase, the other the sites of pH-dependent electron-flux control. It is concluded that tertiary amines develop their action in a lipophilic domain of the thylakoid membrane, in the vicinity of the ATP-synthase complex. A mechanism for selective uncoupling and for the maintenance of H_I-dependent electron flux control in the presence of low H is discussed.Abbreviations and symbols coefficient for pH-dependent electron flux control - 9-AA 9-aminoacridine - Chl chlorophyll - I₅₀ amine concentration producing 50% inhibition of ATP-synthesis - J_e flux of photosynthetic electron transport - k _H apparent rate constant for proton efflux - H₁ proton potential in the thylakoid lumen - H₁ transthylakoid proton potential difference - p partition coefficient - q _AA coefficient for 9-aminoacridine fluorescence quenching - PS photosystem - Q quantum flux of photosynthetically active light Dedicated to Professor Wilhelm Simonis, on the occasion of his 80th birthday     

Energetics of the growth of Methanobacterium thermoautotrophicum and Methanococcus thermolithotrophicus on ammonium chloride and dinitrogen

Methanobacterium thermoautotrophicum was grown in continuous culture in a fermenter gassed with H₂ and CO₂ as sole carbon and energy sources, and in a medium which contained either NH₄Cl or gaseous N₂ as nitrogen source. Growth was possible with N₂. Steady states were obtained at various gas flow rates with NH₄Cl and with and the maintenance coefficient varied with the gas input and with the nitrogen source. Growth of Methanococcus thermolithotrophicus in continuous culture in a fermenter gassed with H₂, CO₂ as nitrogen, carbon and energy sources was also examined.Abbreviations molecular growth yield (g dry weight of cells per mol of CH₄ evolved) - growth rate (h^-1) - D dilution rate (h^-1) - rate (h_-1); relation of Neijssel and Tempest and of Stouthamer and Bettenhaussen - energy     

Drug induced changes in cardio-vascular parameters in the Atlantic cod,Gadus morhua

Summary Ventral (VAP) and dorsal (DAP) aortic blood pressure, heart rate (HR) and cardiac output ( ) were recorded simultaneously in unanaesthetized Atlantic cod, and the effects of vasoactive drugs on the cardio-vascular parameters studied. Mean resting values for the parameters were VAP=4,39 kPa, DAP=2,49 kPa, HR=41 beats/min, and = 29,1 ml/min×kg. Adrenaline constricted the systemic vasculature, dilated the branchial vasculature and caused a decrease of HR and due to a cholinergic reflex. After atropine pre-treatment this reflex was abolished, and the effect of adrenaline on blood pressure enhanced. A small decrease in persisted after atropine, presumably reflecting the effect of an increased end-systolic afterload.Phenylephrine produced a weak increase in systemic vascular resistance, while isoprenaline lowered both systemic and branchial vascular resistance. The effect of isoprenaline is probably mediated by beta adrenoceptors in both vascular beds, since propranolol antagonizes the effect.Acetylcholine in low doses produces a drop in without affecting HR, while higher doses also stop the heart. There is no significant change in either branchial and systemic vascular resistance after acetylcholine.Abbreviations VAP mean ventral aortic blood pressure - DAP mean dorsal aortic blood pressure - TBPD trans-branchial blood pressure drop - HR heart rate - SV stroke volume - cardiac output (ventral aortic blood flow) - VR _g branchial vascular resistance - VR _s systemic vascular resistance     

Ventilatory responses to exercise and carbon dioxide in elderly and younger humans

The present investigation examined the relationship between CO₂ sensitivity [at rest (S _R) and during exercise (S _E)] and the ventilatory response to exercise in ten elderly (61–79 years) and ten younger (17–26 years) subjects. The gradient of the relationship between minute ventilation and CO₂ production ( _E/ CO₂) of the elderly subjects was greater than that of the younger subjects [mean (SEM); 32.8 (1.6) vs 27.3 (0.4); P<0.01]. At rest, S _R was lower for the elderly than for the younger group [10.77 (1.72) vs 16.95 (2.13) 1 · min^–1 · kPa^–1; 1.44 (0.23) vs 2.26 (0.28) 1 · min^–1 · mmHg^–1; P<0.05], but S _E was not significantly different between the two groups [17.85 (2.49) vs 19.17 (1.62) l · min^–1 · kPa^–1; 2.38 (0.33) vs 2.56 (0.21) 1 · min^–1 · mmHg^–1]. There were significant correlations between both S _R and S _E, and _E/ CO₂ (P<0.05; P<0.001) for the younger group, bot none for the elderly. The absence of a correlation for the elderly supports the suggestion that _E/ CO₂ is not an appropriate index of the ventilatory response to exercise for elderly humans.     

Emission of microorganisms from biofilters

Experiments are reported on the discharge of microbial germs by biofilter systems used for the treatment of waste gases containing volatile organic compounds. The systems investigated concern six full-scale filter installations located in the Netherlands in several branches of industry, as well as a laboratory-scale installation used for modelling the discharge process. It is concluded that the number of microbial germs (mainly bacteria and to a much smaller extent moulds) in the outlet gas of the different full scale biofilters varies between 10³ and 10⁴ m^–3, a number which is only slightly higher than the number encountered in open air and of the same order of magnitude encountered in indoor air. It is furthermore concluded that the concentration of microorganisms of a highly contaminated inlet gas is considerably reduced by the filtration process. On the basis of the experiments performed in the laboratory-scale filter bed, it is shown that the effect of the gas velocity on the discharge process results from two distinctive mechanisms: capture and emission. A theoretical model is presented describing the rate processes of both mechanisms. The model presented and the experimentally determined data agree rather well.List of Symbols a _s m^–1 specific area of the packing material - C m^–3 microbial gas phase concentration - C _e , C _i m^–3 microbial concentration in the exit and inlet gas resp. - CFU colony-forming-units - d _c , d _m m diameter of collecting and captured particle resp. - D m diameter of the filter bed - E single particle target efficiency - H m bed height - k _c s^–1 first order capture rate constant per unit of bedvolume - k _e m^–3 emission rate constant per unit of bedvolume - n number of observations - r _c , r _e m^–3 s^–1 capture and emission rate per unit of bed-volume - Re = Reynolds number - S _t = Stokes number - u m s^–1 superficial gas velocity - u _m m s^–1 superficial gas velocity at which C _e = C _i Greek Symbols void fraction of the filter bed - kg m^–3 density of the gas phase - _m kg m^–3 density of captured particle - Pa s dynamic gas phase viscosity - = filter bed efficiency     

Waves in a simple,excitable or oscillatory,reaction-diffusion model

A simple one variable caricature for oscillating and excitable reaction-diffusion systems is introduced. It is shown that as a parameter, , varies the system dynamics change from oscillatory ( > ₀) to excitable ( < ₀) and the frequency of the oscillation vanishes as for ₀. When such dynamics are coupled by continuous diffusion in a ring geometry (1-space dimension), propagating wave trains may be found. On an infinite ring excitable devices lead to unique solitary waves which are analogous to pulse waves. A solvable example is presented, illustrating properties of dispersion, excitability, and waves. Finally it is shown that the caricature arises in a natural way from more general excitable/oscillatory systems.     

The effects of fermentation conditions on yeast cell debris particle size distribution during high pressure homogenisation

Experiments were performed to characterize the particle size distribution of bakers' yeast cells during high pressure homogenisation. Results were obtained for mechanically agitated batch and continuously grown cultures under a range of operating conditions. It was found that the dependency of cell debris size distribution on the number of passes through the homogeniser and the homogeniser pressure was independent of the cell properties and culture conditions, but for a fixed pressure and number of passes the extent of disruption was strongly affected by the operating conditions in the fermenter. The entire cell debris size distributions were successfully simulated using the mean and variance of the distributions and a previously published model equation which related these parameters to the operating pressure and number of passes through the homogeniser.List of Symbols k breakage coefficient in Eq. 1 - d cell diameter - d ₅₀ median diameter of homogenate size distribution - d ₅₀ dimensionless d ₅₀ defined as - D dilution rate - F(d _NP) cumulative undersize distribution (volume basis) - N number of passes - P total pressure - P _threshold threshold pressure - P (P-P _threshold) - w Boltzmann parameter, Eq. 4 - w dimensionless standard deviation defined as Greek Letters exponent in Eq. 1 - exponent in Eq. 1 UCL is the Biotechnology and Biological Sciences Research Council's Interdisciplinary Research Centre for Biochemical Engineering and the Council's support to the participating UCL departments is gratefully acknowledged. The provision of continuous fermentation material from Dr. M. Gregory, Process System Engineering IRC, is gratefully acknowledged.     

The relationship between smoothness and economy during walking

The purpose of this study was to test a theoretical model (Stein et al. 1986) which suggested that minimizing the rate of metabolic energy consumption ( O₂) is related to minimizing jerk (third derivative of position) during human movement. At a given speed of walking, O₂ has been shown to increase curvilinearly as stride length (SL) is varied from freely chosen stride length (FCSL). It was hypothesized that the jerk-cost, or JC (area under squared jerk curve), would exhibit similar behavior. Subjects (n=24) walked (1.75 m ·. s^–1) on a treadmill at FCSL, and at SL derivations at ± 10 and ±20% of leg length from FCSL until steady-state O₂ was attained. Videotaping (60 Hz) in the sagittal plane and subsequent digitizing of relevant markers produced position coordinates which were smoothed and normalized in both distance and time before calculating the third time derivative to obtain two-dimensional JC values. The expected response of O₂ to deviations in SL was found (minimum at FCSL), but JC increased with SL except at the two longest SL conditions. A weak but statistically significant negative correlation was found between O₂ and JC, suggesting that smoothness and economy are not complementary performance criteria during walking.     

On-line parameter and state estimation of continuous cultivation by extended Kalman filter

Summary The on-line estimation of biomass concentration and of three variable parameters of the non-linear model of continuous cultivation by an extended Kalman filter is demonstrated. Yeast growth in aerobic conditions on an ethanol substrate is represented by an unstructured non-linear stochastic t-variant dynamic model. The filter algorithm uses easily accessible data concerning the input substrate concentration, its concentration in the fermentor and dilution rate, and estimates the biomass concentration, maximum specific growth rate, saturation constant and substrate yield coefficient. The microorganismCandida utilis, strain Vratimov, was cultivated on the ethanol substrate. The filter results obtained with the real data from one cultivation experiment are presented. The practical possibility of using this method for on-line estimation of biomass concentration, which is difficult to measure, is discussed.Nomenclature D dilution rate (h^-1) - DO₂ dissolved oxygen concentration (%) - E identity matrix - F Jacobi matrix of the deterministic part of the system equations g - g continuousn-vector non-linear real function - h m-vector non-linear real function - K Kalman filter gain matrix - K _S saturation constant (kgm^-3) - K_S expectation of the saturation constant estimate - M Jacobi matrix of the deterministic part of the measurement equations h - P(t₀) co-variance matrix of the initial values of the state - P(t_k/t_k) c-variance matrix of the error in (t _k|t _k) - P(t_k+1/t_k) co-variance matrix of the error in (t _k+1|t _k - Q co-variance matrix of the state noise - R co-variance matrix of the output noise - S substrate concentration (kgm^-3) - S _i input substrate concentration - t time - t _k discrete time instant with indexk=0, 1, 2,... - u(t) input vector - v(t_k) measurement (output) noise sequence - w(t) n-vector white Gaussian random process - x(t₀) initial state of the system - (t₀) expectation of the initial state values - x(t) n-dimensional state vector - x(t_k) state vector at the time instantt _k - (t_k|t_k) expectation of the state estimate at timet _k when measurements are known to the timet _k - (t_k+1|t_k) expectation of the state prediction - X biomass concentration (kgm^-3) - expectation of the biomass concentration estimate - y(t_k) m-dimensional output vector at the time instantt _k - Y _XIS substrate yield coefficient - _X|S expectation of the substrate yield coefficient estimate - specific growth rate (h^-1) - _M maximum specific growth rate (h^-1) - expectation of the maximum specific growth rate estimate - state transition matrix     

Maximal oxygen uptake,sweating and tolerance to exercise in the heat

The purpose of this experiment was to determine if tolerance to exercise in the heat is related to maximal oxygen uptake (max ₀₂) and sweating. Seven men with max ₀₂ between 42 and 66 ml/(min·kg) underwent one 2-hr exposure at 24°C T_q while working on a bicycle ergometer at rel ₀₂ of 28% ( ₀₂ = 1.23 1/min). In the hot exposures the high capacity subjects had maximal sweat rates of 800 to 1,000 g/(hr·m²) while the lower capacity men sweated 300 to 400 g/(hr·m²). These differences in sweating were not related to neuromuscular stimuli, ₀₂ (metabolic rate), T_re, T_re, _s, _s or tolerance time. Tolerance to exercise in the heat was not related to maximal ₀₂ capacity when the subjects worked at the same relative load in spite of large differences in sweating. These results question the importance of the rate of sweating for predicting work performance in hot environments.

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Zusammenfassung Das Ziel dieser Untersuchung war, zu prüfen, ob die Toleranz bei Arbeit in der Hitze in einer Beziehung steht zur maximalen O₂-Aufnahme und Schwitzen. Sieben Männer mit V₀₂ zwischen 42 – 66 ml/(min·kg) wurden belastet während 2 Stunden bei T_a 24°C und 3 × 2 Stunden bei 47°C mit Arbeit auf dem Fahrrad-Ergometer bei im Mittel von 28% V₀₂ = 1.23 1/min. Während der Hitzebelastung zeigten die leistungsfähigen Personen Schweissekretionsraten von 800 – 1000 g/(hr·m²) und die wenig leistungsfähigen 300 – 400 g/(hr·m²). Diese Unterschiede waren ohne Beziehung zu neuromuskulären Stimuli, Stoffwechselrate, T_re, T_re, _s, _s oder der Toleranzzeit. Ausdauer bei Arbeit in der Hitze war ohne Beziehung zur maximalen V₀₂-Kapazität, wenn die Personen bei der gleichen relativen Belastung arbeiteten tro grosser Unterschiede im Schwitzen. Die Ergebnisse stellen den Wert der Schweissekretionsrate zur Voraussage der Arbeitsleistung in der Hitze in Frage.

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Resume Dans cette étude, on a cherché à voir si la tolérance au travail sous contrainte de chaleur était en relation avec la possibilité maximum d'absorption de O₂ ( ₀₂) d'une part, de transpirer d'autre part. 7 hommes présentant des ₀₂ compris entre 42 et 66 ml/(min · kg) ont pédalé sur un ergomètre pendant 2 heures par une T_a de 24°C et 3 × 2 heures par 47°C et cela par une ₀₂ relative de 28% ( ₀₂ = 1,25 1/min). Durant l'effort sous contrainte de chaleur, les plus actifs ont eu des sécrétions de sueur de 800 à 1.000 g h^–1 m^–2 et les moins actifs de 300 à 400 g/h · m². Ces différences étaient sans rapport avec les stimulus neuro-musculaires, le taux de métabolisme, T_re, T_re, T_s et T_s ou la durée de tolérance. L'endurance au travail sous contrainte de chaleur n'a pas été fonction de la capacité maximum de ₀₂, lorsque les personnes travaillaient dans des conditions analogues, même si l'on a noté de grandes différences dans la transpiration. Ces résultats mettent en doute la représentativité du taux de sécrétion de sueur comme indicatif des possibilités de travailler en atmosphère chaude.

     

Liquid-phase axial mixing in a bubble column bioreactor containing yeast suspensions

Summary Liquid-phase axial mixing coefficients were evaluated in a 0.15 m x 2.0 m batch bubble column containing water and yeast-in-water suspensions of different concentrations. Air superficial velocities ranged from 0 to 0.06 m/s. Axial mixing coefficients were calculated from the residence time distribution to an NaCl tracer pulse using the Ohki and Inuoe model. No specific variations in the calculated coefficients were observed to result from the presence of yeast cells. There was fair agreement between the data thus obtained and the only available data on mixing in non-Newtonian CMC solution.Nomenclature C _E equilibrium tracer concentration g/l - C tracer concentration at time t g/l - d_h sparger hole diameter m - D _t tube diameter m - D _z axial mixing coefficient m²/s - g acceleration of gravity m/s² - H _B bubbling layer heigh m - L longitudinal dustance between tracer injection and detection points m - n 1,2,6 Eq. (3) - t time s - U_g gas superficial velocity m/s - U_t liquid superficial velocity m/s - V _r bubble relative velocity = m/s - V _t Linear relative velocity m/s - z axial distance m Greek _c wet cell volume farction - _g gas holdup - _l liquid holdup - _l viscosity of the liquid phase Pa/s - _l density of liquid or continuous phase g/ml