A method for measuring the settling velocity distribution of large biotic particles

A simple method for measuring the settling velocity (V _s) distribution of pollen and spores 30–100 μm in diameter is detailed and evaluated. The method is called the ‘settling tower' and consists in taking sequential pictures of particles falling under gravity in calm air. The scene is illuminated by a cold light source, while a camera takes 15 pictures per second. Between 20,000 and 100,000 images are analysed to obtain the distribution of V _s for a given set of particles. The method was validated using two standard particles with mean diameters of 68 and 108 μm, respectively, as well as Lycopodium spores, with a mean diameter of 35 μm. For each set of particles, the theoretical V _s distribution was estimated from the particle diameter distribution and the volumetric mass using a non-Stokian law, as the Reynolds numbers of the particles were large. The mean V _s was measured with the ‘settling tower' with less than 12% error, while the standard deviation of the V _s distribution was estimated with less than 51% error. The maximum error on the mean V _s was 12% for the Lycopodium spores and less than 2% for the two larger particles. The mean V _s of Lycopodium spores was 4.2 cm s⁻¹, and its standard deviation was 0.7 cm s⁻¹. The reason for the small overestimation of V _s for Lycopodium spores by the ‘settling tower' method is discussed. Preliminary measurements shows that, the ‘settling tower' could be of great practical interest for measuring the distribution of V _s of maize pollen as well as other types of pollen or spores.     

Transient state analysis of biochemical reactor using coimmobilized system

The transient state analysis of the consecutive sequence of reactions S P ₁ P ₂ taking place inside a porous spherical coimmobilized biocatalyst is discussed for the case in which each step follows Michaelis Menten type kinetics. The theoretical analysis includes intraparticle diffusional limitations. The model equations are solved by the explicit finite difference method. The effect of various parameters of importance on the batch reactor performance is discussed. Comparison of the model with experimental results has been shown.List of Symbols c _p Dimensionless substrate concentration inside the particle, (s _p/ss _o) - c _{pi, j} Dimensionless substrate concentration inside the particle at i, j - c _s Dimensionless substrate concentration at the surface of the particle, (s _s/s ₀) - d _p cm particle diameter - D _s, D _p cm²/s Diffusion coefficient of the substrate S and intermediate P ₁ inside the particle respectively - h Space step size inside the particle - i Grid point inside the particle - j Grid point along the time coordinate - k Time step size - K _m1, K _m2 g/l Michaelis constants for the first and second reaction respectively - K _I1,K _I2 g/l Substrate inhibition parameters for first and second reaction respectively - P _m g/l Product inhibition parameter for the second reaction - P _1p , P _1s g/l Concentration of the intermediate inside the particle and at the surface of the particle respectively - P _2p , P _2s g/l Concentration of the product P ₂ inside the particle and at the surface of the particle respectively - p _1p Dimensionless intermediate concentration inside the particle, (p _1p/s₀) - p _1s Dimensionless intermediate concentration at the surface of the particle, (p _1s /S ₀) - P _2p Dimensionless product concentration inside the particle, (p _2p /S₀) - p _2s Dimensionless product concentration at the surface of the particle, (p _2s/S₀) - p _{1pi, j} Dimensionless intermediate concentration inside the particle at i, j - P _{2pi, j} Dimensionless product concentration inside the particle at i, j - q Ratio of diffusion coefficients, D _p/D _s - r cm Radial position inside the particle - R cm Radius of the pellet - S ₀ g/l Initial substrate concentration in the bulk liquid - S _p g/l Substrate concentration inside the particle - S _s g/l Substrate concentration at the surface of the particle - t s Time, - V _max1 g/(ls) Maximum reaction velocity for the first reaction - V _max2 g/(ls) Maximum reaction velocity for the second reaction - y Dimensionless radial distance, (r/R) - y _{1, j} Dimensionless radial distance at i, j Greek Letters ₁ Parameter, S ₀/K _m1 - ₂ Parameter, S ₀/K _m2 - _I1 Parameter, S ₀/K _I1 - _I2 Parameter, S ₀/K _I2 - _I3 Parameter, S ₀/P _m - Dimensionless time defined as (D _s t/R ²) - ₁ ² V _max1R ²/K_m1D_s - ₂ ² V _max2R ²/K_m2D_s     

Response of <Emphasis Type="Italic">Tisochrysis lutea</Emphasis> [Prymnesiophycidae] to aeration conditions in a bench-scale photobioreactor

The effects of superficial gas velocity (U_gr), gas entrance velocity (ν), and bubble size on the growth of Tisochrysis lutea was investigated in 600-mL photobioreactors operated with airlift pumps. Superficial gas velocities, calculated from measured air flow rates, ranging from 7 to 93 mm s^?1 were created using a 1.6-mm diameter syringe. We tested the effects of sparger velocity over a range of 2.48 to 73.4 m s^?1 and the effects of bubble size by using two styles of air stones and an open glass pipette, which created a bubble sizes in the range of 0.5 to 5 mm. We calculated oxygen mass transfer coefficient, k_La, values for all experimental conditions. Cell growth increased linearly with increased superficial gas velocity and decreased with increased sparger velocity. Results indicated that smaller bubble size leads to some initial cell damage, but after time, the increased gas transfer as reflected by the k_La value produced higher growth than larger bubbles. Two mechanisms were observed to correlate with cell damage in T. lutea: increasing velocity at the sparger tip and bubble bursting at the surface. These results demonstrate a method to test sensitivity of T. lutea to aeration, which is important for the design of airlift systems.     

Flow characteristics of a pilot-scale airlift fermentor

The effects of aeration on the flow characteristics of water in a glass pilot-scale airlift fermentor have been examined. The 55-L capacity fermentor consisted of a 15.2-cm-i.d. riser column with a 5.1-cm-i.d. downcomer tube. It was found that the average bubble size diminished with increased aeration. Typically, average bubble sizes ranged from 4.32 mm at a superficial gas velocity of 0.64 cm/s to 1.92 mm at 10.3 cm/s. A gas holdup of 0.19 was attained with superficial gas velocities (v_s) on the order of 10 cm/s, indicating the highly gassed nature of the fluid in the riser section of the fermentor. Circulation velocities of markers placed in the fermentor decreased with increasing aeration rates due to increased turbulence and axial liquid back mixing within the riser section. Actual volumetric liquid circulation rates remained relatively constant (0.36–0.49 L/s) for values of (v_s) up to 10 cm/s. Based on theoretical calculations, the ascending velocity of bubbles in a swarm reached 54 cm/s in the range of (v_s) values studied.     

Citric acid production in submerged and solid state culture of Aspergillus niger

In this work, the citric acid production in solid state culture was performed, evaluating the isolated effect and interactions of particle size and liquid phase employed, by means of the factorial design of first order. The results indicate that the particle size is the most determinant variable. An analysis comparing submerged and solid state in optimal conditions was performed. When solid state culture was used, the productivity of citric acid was doubled, reducing the fermentation time from 14 to 6 days, compared to the submerged culture, obtaining a maximum citric acid concentration of 21.24 g/l.List of Symbols B _s , B _v main effects - B _sv crossed effects - s cm particle size - S coded particle size - v ml liquid phase volume - V coded liquid phase volume     

Protein mass transfer studies on a spray column using the PEG-Reppal PES 100 aqueous two-phase system

The characterization of Bovine Serum Albumin mass transfer mechanisms in a spray column using an aqueous two-phase system composed of poly(ethylene glycol) and a modified starch-Reppal PES 100-is done. The poly(ethylene glycol) rich phase is used as the dispersed phase and protein transfer takes place from the dispersed phase to the continuous phase. The effect of dispersed phase superficial velocity, system composition, continuous phase height and distribution system design on either overall protein mass transfer coefficient or column hold-up is described. It is shown that continuous phase superficial velocity and phase composition are the main controlling factors for protein transfer. It is also observed that, with the tested system, only at very low dispersed phase superficial velocities is it possible to operate the spray column as an extraction column. In this system the upper operating limit of the dispersed phase velocity is ten times smaller than in other aqueous two-phase systems.List of Symbols ATPS Aqueous Two-Phase System - BSA Bovine Serum Albumin - C _i kg m^–3 inlet dispersed phase protein concentration - C ₀ kg m^–3 outlet dispersed phase protein concentration - C _d kg m^–3 dispersed phase protein concentration - C _c kg m^–3 continuous phase protein concentration - D m column internal diameter - H hold-up - h, h _d m dispersion height - h ₀ m initial dispersion height (initial continuous phase height) - k _da s^–1 overall mass transfer coefficient - m protein partition coefficient - n number of holes of distribution system - PEG Poly(ethylene glycol) - Q m³ s^–1 dispersed phase volumetric flow rate - S m² column internal area - V m³ dispersion volume A. Venâncio was supported by a JNICT (Junta Nacional de Investigaçäo Científica e Tecnológica) grant.     

Effect of aggregate size in cell cultures of Tagetes patula on thiophene production and cell growth

Summary The effect of the size of Tagetes patula (marigolds) cell aggregates on growth and thiophene production in MS-medium was studied. A heterogeneous aggregate suspension was aseptically divided into 7 fractions, each with a defined aggregate diameter range, with subsequent inoculation of the fractions into MS growth medium. Growth occurred in all aggregate fractions and thiophene production increased with increasing aggregate diameter starting at about 3 mm, an effect possibly due to an increasing lack of oxygen in the aggregate centre. Calculations of oxygen concentration profiles in the aggregates showed namely, that the critical aggregate diameter where the oxygen concentration in the aggregate centre becomes very low, is about 3 mm. Aggregates with a diameter exceeding 1.2 cm showed a decreased thiophene production, however, these aggregates were hollow. The thiophenes produced mainly consisted of 5-(4-hydroxy-1-butenyl)1-2,2-bithienyl, which was excreted into the medium.Nomenclature ID _e effective diffusion coefficient (m²s^-1) - c oxygen concentration (mol m^-3) - c _s substrate concentration at surface (mol m^-3) - c _s.exp experimental value of c _s (mol m^-3) - c _eq substrate concentration at equilibrium (mol m^-3) - r _s consumption rate (mol m^-3 s^-1) - d _crit critical aggregate diameter (m) - d _agg aggregate diameter (m) - L length of aggregate (m) - W width of aggregate (m) - t time (s) - r distance from aggregate centre (m) - R radius of aggregate (m) - R(c) oxygen consumption (mol m^-3 s^-1) - V _c convection velocity (m s^-1) - V _m intrinsic maximum consumption rate (mol kg^-1 s^-1) - K _m intrinsic Michaelis Menten constant (mol m^-3) - V _m apparent maximum consumption rate (mol kg^-1 s^-1) - K _m apparent Michaelis Menten constant (mol m^-3) - * multiplication sign     

A pulsing device for packed-bed bioreactors: II. Application to alcoholic fermentation

When the immobilized cells are employed in packed-bed bioreactors several problems appear. To overcome these drawbacks, a new bioreactor based on the use of pulsed systems was developed [1]. In this work, we study the glucose fermentation by immobilized Saccharomyces cerevisiae in a packed-bed bioreactor. A comparative study was then carried out for continuous fermentation in two packed-bed bioreactors, one of them with pulsed flow. The determination of the axial dispersion coefficients indicates that by introducing the pulsation, the hydraulic behaviour is closer to the plug flow model. In both cases, the residence time tested varied from 0.8 to 2.6 h. A higher ethanol concentration and productivity (increases up to 16%) were achieved with the pulsated reactors. The volumes occupied by the CO₂ were 5.22% and 9.45% for fermentation with/without pulsation respectively. An activity test of the particles from the different sections revealed that the concentration and viability of bioparticles from the two bioreactors are similar. From the results we conclude that the improvements of the process are attributable to a mechanical effect rather than to physiological changes of microorganisms.List of Symbols D m²/s dispersion coefficient - K _is l/g inhibition substrate constant - K _ip l/g inhibition ethanol constant - K _s g/l Apparent affinity constant - P g/l ethanol concentration - q _p g/(gh) specific ethanol productivity - Q _p g/(lh) overall ethanol productivity - q _s g/(gh) specific glucose consumption rate - Q _s g/(lh) glucose consumption rate - S g/l residual glucose concentration - S(in0) g/l initial glucose concentration - V _max g/(lh) maximum rate - Y _p/s g/g yield in product     

The role of phytoplankton in the removal of arsenic by sedimentation from surface waters

The role of phytoplankton in the removal of arsenic (As) by particle adsorption and sedimentation was investigated in Moira Lake, Canada. Sampling water and suspended particles over one year illustrated significant variation in As partitioning between particulate and aqueous phases, but failed to establish a correlation between the partition coefficient, K _d, and indicators of phytoplankton biomass. A highly significant inverse logarithmic relationship was noted between K _d and the concentration of suspended particles (log K _d = 5.1 – 1.4 log SS; p = 0.0001) in an apparent demonstration of the particle concentration effect (O' Connor & Connolly, 1980).Particle deposition, measured by means of sediment traps, appeared to include a substantial component of resuspended surficial sediment making sediment trap results unreliable for quantifying the removal of substances from the water column. The As concentration of particles from deep traps deployed during late summer and early fall exceeded the As concentrations of suspended particles and surficial sediment, and may indicate that a highly contaminated nepheloid layer acts as a temporary sink for As.     

Reactor design for the enzymatic isomerization of glucose to fructose

A comprehensive methodology is presented for the design of reactors using immobilized enzymes as catalysts. The design is based on material balances and rate equations for enzyme action and decay and considers the effect of mass transfer limitations on the expression of enzyme activity. The enzymatic isomerization of glucose into fructose with a commercial immobilized glucose isomerase was selected as a case study. Results obtained are consistent with data obtained from existing high-fructose syrup plants. The methodology may be extended to other cases, provided sound expressions for enzyme action and decay are available and a simple flow pattern within the reactor might be assumed.List of Symbols C kat/kg specific activity of the catalyst - D m²/s substrate diffusivity within the catalyst particle - Dr m reactor diameter - d d operating time of each reactor - E kat initial enzyme activity - E _i kat initial enzyme activity in each reactor - F m³/s process flowrate - F _i m³/s reactor feed flowrate at a given time - F ₀ m³/s initial feed flowrate to each reactor - H number of enzyme half-lives used in the reactors - K mole/m³ equilibrium constant - K _S mole/m³ Michaelis constant for substrate - K _P mole/m³ Michaelis constant for product - K _m mole/m³ apparent Michaelis constant f(K, K _s, K_p, s₀) - k mole/s · kat reaction rate constant - k _d d^–1 first-order thermal inactivation rate constant - L m reactor height - L _r m height of catalyst bed - N _R number of reactors - P _i kg catalyst weight in each reactor - p mole/m³ product concentration - R m particle radius - R _P ratio of minimum to maximum process flowrate - r m distance to the center of the spherical particle - s mole/m³ substrate concentration - s _0i mole/m³ substrate concentration at reactor inlet - s ₀ mole/m³ bulk substrate concentration - s mole/m³ apparent substrate concentration - T K temperature - t d time - t _i d operating time for reactor i - t _s d time elapsed between two successive charges of each reactor - V m³ reactor volumen - V _m mole/m³ s maximum apparent reaction rate - V _p mole/m³ s maximum reaction rate for product - V _R m³ actual volume of catalyst bed - V _r m³ calculated volume of catalyst bed - V _S mol/m³ s maximum reaction rate for substrate - v mol/m³ s initial reaction rate - v _i m/s linear velocity - v _m mol/m³ s apparent initial reaction rate f(K_m, s,V_m) - X substrate conversion - X _eq substrate conversion at equilibrium - =s/K dimensionless substrate concentration - ₀=s₀/K bulk dimensionless substrate concentration - _eq=s_eq/K dimensionless substrate concentration at equilibrium - local effectiveness factor - mean integrated effectiveness factor - Thiéle modulus - =r/R dimensionless radius - _s kg/m³ hydrated support density - substrate protection factor - s residence time     

Microcalorimetric investigations of the metabolism of yeasts. growth in batch and chemostat cultures on ethanol medium

Summary In the presence of protein, Hansenula polymorpha cultivation medium exhibits a maximum volumetric mass transfer coefficient, k_La, as function of the employed antifoam agents (soy oil and Desmophen 3600). With diminishing superficial gas velocity this maximum disappeas.Symbols E_G Relative gas holdup - k_La Volumetric mass transfer coefficient (s^–1) - w_SL Superficial liquid velocity (cm s^–1) - w_SG Superficial gas velocity (cm s^–1)     

Development of reactor model for glucose isomerization catalyzed by whole-cell immobilized glucose isomerase

Based on the kinetic constants determined and the mathematical model of the reactor system developed, the performance of axial flow packed bed continuous enzyme reactor system was studied experimentally and also simulated with the aid of a computer for ultimate objective of optimization of the glucose isomerase reactor system.A reactor model was established analogous to heterogeneous catalytic reactor model taking into account the effect of fluid mass transfer and reversible kinetics. The investigated catalyst system consists of immobilized Streptomyces bambergiensis cells containing the enzyme glucose isomerase, which catalyzes the isomerization of glucose to fructose.List of Symbols A ₀, A ₁, A ₂ parameters in axial dispersion reactor model - c _go, c_g, c_gemol m^–3 glucose concentration at time t=0, at any time and at equilibrium conditions - c _gsmol m^–3 glucose concentration at particle surface - C dimensionless glucose concentration - d _pm particle diameter - d _rm diameter of reactor tube - Da Damkohler number - D _eff m² s^–1 effective glucose diffusion coefficient in Ca-alginate gel beads - k _fm s^–1 film transfer coefficient - K _e equilibrium constant - K _mg, K_mfmol m^–3 Michaelis-Menten constant for glucose and fructose, respectively - K _mmol m^–3 modified Michaelis-Menten constant - K dimensionless parameter - K ^* dimensionless parameter - L m length of reactor tube - Pe Peclet number - Pe _p particle Peclet number - Q m³ s^–1 volumetric flow rate - (-r _g) mol m^–3 s^–1 reaction rate - Re _p Reynolds particle number - Sc Schmidt number - Sh Sherwood number - t s time - v ₀ m s^–1 linear superficial fluid velocity - V _mg, V_mfmol g^–1 s^–1 maximal reaction rate for glucose and fructose, respectively - V _mmol m^–3 s^–1 modified maximal reaction rate for glucose - V _mg ^x mol m^–2 s^–1 maximal reaction rate for glucose - X _g, X_ge glucose conversion and glucose conversion at equilibrium conditions - X normalized conversion - Y dimensionless glucose concentration - void fraction of fixed bed - effectiveness factor of biocatalyst - Pa s kinematic viscosity of substrate - ₁ s first absolute weighted moment - ₂ s² second central weighted moment - _gkg m^–3 substrate density - _pkg m^–3 particle density - ² dimensionless variance of RTD curve - s residence time     

Effects of elevated O3 and CO2 concentrations on photosynthesis and stomatal conductance in Scots pine

Naturally regenerated Scots pines (Pinus sylvestris L.), aged 28–30 years old, were grown in open-top chambers and subjected in situ to three ozone (O₃) regimes, two concentrations of CO₂, and a combination of O₃ and CO₂ treatments From 15 April to 15 September for two growing seasons (1994 and 1995). The gas exchanges of current-year and 1-year-old shoots were measured, along with the nitrogen content of needles. In order to investigate the factors underlying modifications in photosynthesis, five parameters linked to photosynthetic performance and three to stomatal conductance were determined. Elevated O₃ concentrations led to a significant decline in the CO₂ compensation point (Г^*), maximum RuP₂-saturated rate of carboxylation (V_cmax), maximum rate of electron transport (J_max), maximum stomatal conductance (g_smax), and sensitivity of stomatal conductance to changes in leaf-to-air vapour pressure difference (?g_s/?D_v) in both shoot-age classes. However, the effect of elevated O₃ concentrations on the respiration rate in light (R_d) was dependent on shoot age. Elevated CO₂(700 μmol mol^?1) significantly decreased J_max and g_smax but increased R_d in 1-year-old shoots and the ?g_s/?D_v in both shoot-age classes. The interactive effects of O₃ and CO₂ on some key parameters (e.g. V_cmax and J_max) were significant. This may be closely related to regulation of the maximum stomatal conductance and stomatal sensitivity induced by elevated CO₂. As a consequence, the injury induced by O₃ was reduced through decreased ozone uptake in 1-year-old shoots, but not in the current-year shoots. Compared to ambient O₃ concentration, reduced O₃ concentrations (charcoal-filtered air) did not lead to significant changes in any of the measured parameters. Compared to the control treatment, calculations showed that elevated O₃ concentrations decreased the apparent quantum yield by 15% and by 18%, and the maximum rate of photosynthesis by 21% and by 29% in the current-year and 1-year-old shoots, respectively. Changes in the nitrogen content of needles resulting from the various treatments were associated with modifications in photosynthetic components.     

Anchorage-dependent animal cell culture by using a porous microcarrier

CHO-K1 cells were cultured by using a porous microcarrier. The effects of microcarrier concentration and agitation rate on cell growth in porous microcarrier cultures were investigated. The specific growth rate of 0.041 h^–1 in porous microcarrier cultures was independent of both microcarrier concentration and agitation rate. By estimating the total surface area occupied by cells from the maximum cell number, it was found that not all the surface area of the porous microcarrier was utilizable for cell growth.The maximum cell number decreased with increasing the microcarrier concentration and the agitation rate. From this result, it was also found that not all the cells grown on the interior surface of the porous microcarrier were protected against mechanical damage due to agitation. The protection capacity of the porous microcarrier was estimated to be 300 cells/carrier. The direct gas sparging into the culture broth in porous microcarrier cultures improved the cell density without mechanical damage to animal cells.List of Symbols d m microcarrier diameter - d _i m impeller diameter - d _p m mean pore diameter - n _i s^–1 agitation rate - p Pa pressure difference - v m/s velocity of microcarrier - v _p m/s average velocity flowing through cyclinder - Pa · s viscosity of medium - angle measured from stagnant point - Pa average shear stress - Pa shear stress distribution     

EVALUATION OF COMPETITIVE ABILITY OF STAURASTRUM LUETKEMUELLERII (CHLOROPHYCEAE) AND MICROCYSTIS AERUGINOSA (CYANOPHYCEAE) UNDER P LIMITATION1

The desmid Staurastrum luetkemuellerii Donat et Ruttner and the cyanobacterium Microcystis aeruginosa Kütz. showed pronounced differences in chemical composition and ability to maintain P fluxes. The cellular P:C ratio (Q_p) and the surplus P:C ratio (Q_sp) were higher in M. aeruginosa, indicating a lower yield of biomass C per unit of P. The subsistence quota (Q_p) was 1.85 μg P·mg C^?1in S. luetkemuellerii and 6.09 μg P·mg C^?1in M. aeruginosa, whereas the respective Q_p of P saturnted organisms (Q_s) were 43 and 63 μg P·mg C^?1. These stores could support four divisions in S. luetkemuellerii and three divisions in M. aeruginosa, which suggests that the former exhibited highest storage capacity (Q_s/Q₀). M. aeruginosa showed a tenfold higher activity of alkaline phosphatase than S. luetkemuellerii when P starved. The optimum N:P ratio (by weight) was 5 in S. luetkemuellerii and 7 in M. aeruginosa. The initial uptake of P_i pulses in the organisms was not inhibited by rapid (<1 h) internal feedback mechanisms and the short term uptake rote could be expressed solely as a function of ambient P_i. The maximum cellular C-based uptake rate (V_m) in P starved M. aeruginosa was up to 50 times higher than that of S. luetkemuellerii. It decreased with increasing growth rate (P status) in the former species and remained fairly constant in the latter. The corresponding cellular P-based value (U_m= V_m/Q_p) decreased with growth rate in both species and was about 10 times higher in P started M. aeruginosa than in S. luetkemuellerii. The average half saturation constant for uptake (K_m) was equal for both species (22 μg P·L^?1) and varied with the P status. S. luetkemuellerii exhibited shifts in the uptake rate of P_i that were characterized by increased affinity (U^m/K^m) at low P_i, concentrations (<4 μg P·L^?1) compared to that at higher concentrations. The species thus was well adapted to uptake at low ambient P_i, but M. aeruginosa was superior in P_i uptake under steady state and transient conditions when the growth rate was lower than 0.75 d^?1. Moreover, M. aeruginosa was favored by pulsed addition of P_i. M. aeruginosa relpased P_i at a higher rate than S. luetkemuellerii. Leakage of P_i from the cells caused C-shaped μ vs. P_i curves. Therefore, no unique K_s for growth could be estimated. The maximum growth rate (μ_m) (23° C) was 0.94 d^?1for S. luetkemuellerii and 0.81 d^?1for M. aeruginosa. The steady state concentration of P_i (P*) was lower in M. aeruginosa than in S. luetkemuellerii at medium growth rates. The concentration of P_i at which the uptake and release of P_i was equal (P_c was, however, lower in S. luetkemuellerii.     

A study of the effect of low-frequency conditioning on the size distribution properties and centrifugal recovery of human albumin precipitate

The effect of low-frequency conditioning on the particle size distribution of ethanol-precipitated human albumin protein has been examined. Laboratory-scale data has been extrapolated to the pilot-plant scale recovery of conditioned precipitates by high-speed centrifugation.Data comparing batch ageing, low-frequency and static mixer conditioning is presented together with data exploring the relationship between pretreatment and the effectiveness of conditioning. Conditioning systems appear to be satisfactorily described in terms of the levels of mixing produced and the associated mechanisms of aggregation and breakage of large aggregates. Observed changes in size-distribution properties due to conditioning are seen to be translated into improved centrifugal recovery. The extent of pretreatment of the material to be conditioned is critical to the efficiency of the conditioning processes.List of Symbols CRX conditioning ratio a x% oversize - d m amplitude of displacement - DX m volumetric oversize diameter of aggregate where x=% oversize - f s^—1 frequency of oscillation - G s^–1 mean shear rate - k, k ¹ rate constants describing aggregation and breakage respectively, Eqs. (1) and (2) - N _f m^–3 number concentration of fine-sized particles - N _L m^–3 number concentration of large-size particles - Re _f flow Reynolds number - t s time - V ₀ m/s peak velocity of flow - W m channel half-width Greek Symbols response factor (see [5]) - m² s^–1 fluid kinematic viscosity - Ns/m² fluid viscosity - _V volume fraction of precipitate particles     

Particulate pollution capture by urban trees: effect of species and windspeed

Particulate pollution is a serious health problem throughout the world, exacerbating a wide range of respiratory and vascular illnesses in urban areas. The use of trees to reduce the effects of these pollutants has been addressed in the literature, but has rarely been quantified. The aim of the present study was to quantify the effectiveness of five tree species ? pine (Pinus nigra var. maritima), cypress ( × Cupressocyparis leylandii), maple (Acer campestre), whitebeam (Sorbus intermedia), poplar (Populus deltoides × trichocarpa‘Beaupré’) ? in capturing pollutant particles. This was achieved by exposing them to NaCl droplets of approximately 1 μm diameter at a range of windspeeds in two windtunnels. The deposition velocity (V_g) and particle trapping efficiency (C_p) were calculated from these exposures. In addition, a variable dependent on foliage structure [Stokes number (St)] was correlated with C_p to gauge the effect of tree morphology on particle capture. Maximum C_p values ranged from 2.8% for P. nigra, to 0.12% and 0.06% for P. trichocarpa×deltoides and A. campertre, respectively. The finer, more complex structure of the foliage of the two conifers (P. nigra and C. leylandii) explained their much greater effectiveness at capturing particles. The data presented here will be used to model the effectiveness of tree planting schemes in improving urban air quality by capturing pollutant particles.     

Interpretation of gas residence time distributions in large airlift tower loop reactors

Gas-residence time distribution (RTD) response curves measured in a 23 m high pilot plant airlift tower loop reactor, which consisted of a riser, a special downcomer construction and at the top of the riser a large head. The measurements were evaluated by means of a deterministic dispersion model, which yielded the following particular parameters for the riser, downcomer and the head: Gas-Bo numbers, gas-mean residence times, gas holdups, liquid velocities, gas and liquid circulation times as well as a fraction of the large and small bubbles in a model medium (water) and during cultivation of baker's yeast.List of Symbols A cross section - Bo Bodenstein number - Bo _d (= l _d w _G,d /D _d ) - Bo _h (= l _h w _G,h /D _h ) - Bo _r (= l _r w _G,r /D _r ) - D longitudinal dispersion coefficient - E gas holdup - E(t) RTD-density function - L, l length parameter - q fraction of the gas throughput which is not recirculated (approximately equal to fraction of the large bubbles) - r fraction of the throughput which is recirculated (approximately equal to the fraction of the small bubbles) - t _c circulation time - t _cL liquid circulation time - t _c,L ^* liquid circulation time calculated from the measured w _Ld in the downcomer - V ^h hydrodynamical calculated gas-liquid volume - V _d ^h (=V _d+0.75/2 V _k ) - V _k ^h =(0.25V _k ) - V _r ^h = (V _r+0.75/2 V _k ) - V _L liquid volume - V _G dispersed gas volume - V _G ^* gas throughput at the gas distributor (given in m³/h) under standard conditions, 1 bar and 25°C) - V _G,d ^* gas throughput in downcomer (=V _G ^* ) - V _G,h ^* gas throughput in head (=V _G ^* ) - V _G,r ^* gas throughput in riser (V _G ^* (1+) - w _g gas velocity - w _G,rel relative gas velocity with respect to the liquid velocity w _L - w _G,d gas velocity in the downcomer (=w _G,rel –w _Ld ) - w _G,h gas velocity in the head (=w _G,rel ) (since wLh = o) - w _G,r gas velocity in the riser (=w _G,rel +w _Lr ) - w _L liquid velocity - w _L,d liquid velocity in the downcomer measured with mass flow meter - w _sg ·w _SL superficial gas and liquid velocities - first moment of the response curve - mean residence time Indices d downcomer - G gas phase - h head - L liquid phase - r riser - h hydrodynamic (upper position) Dedicated to the 65th birthday of Proffessor Fritz Wagner.The authors gratefully acknowledge the financial support by the Krupp Industrietechnik, Grevenbroich and the support of Pleser Co, Darmstadt. H. M. Rüffer thanks the Verband der Chemischen Industrie for a Fond der Chemie scholarship, and W. Liwei thanks the government of Lower Saxony for a graduate scholarship.     

Comparison of the hydrodynamics and mass transfer characteristics in internal-loop airlift bioreactors utilizing either a novel membrane-tube sparger or perforated plate sparger

Two gas spargers, a novel membrane-tube sparger and a perforated plate sparger, were compared in terms of hydrodynamics and mass transfer (or oxygen transfer) performance in an internal-loop airlift bioreactor. The overall gas holdup ε _T, downcomer liquid velocity V _d, and volumetric mass transfer coefficient K _L a were examined depending on superficial gas velocity U _G increased in Newtonian and non-Newtonian fluids for the both spargers. Compared with the perforated plate sparger, the bioreactor with the membrane-tube sparger increased the values of ε _T by 4.9–48.8 % in air–water system when the U _G was from 0.004 to 0.04 m/s, and by 65.1–512.6 % in air–CMC solution system. The V _d value for the membrane-tube sparger was improved by 40.0–86.3 %. The value of K _L a was increased by 52.8–84.4 % in air–water system, and by 63.3–836.3 % in air–CMC solution system. Empirical correlations of ε _T, V _d, and K _L a were proposed, and well corresponding with the experimental data with the deviation of 10 %.     

Separation of proteins by ion-exchange chromatography using gradient elution

Chromatographic separation of proteins by the gradient elution method using DEAE Toyopearl 650^® was carried through. The concentration gradient was effected by changing the ionic strength of NaCl in the carrier buffer solution. Bovine serum albumin and hemoglobin were used as model proteins for separation. The experimental chromatogram was compared with theoretical results of Yamamoto et al. [1, 2]. Adsorption equilibria of the proteins onto the carrier were measured and expressed by a function of the ionic strength. The retention volume and peak width of the resulting chromatogram can be calculated from the equilibrium data using the Yamamoto theory. The calculated results agreed well with the experimental data.The method presented in this paper will be useful to predict the viability of ion-exchange chromatography in protein separation.List of Symbols c kg m^–3 concentration in the liquid phase - c _s kg m^–3 concentration in the solid phase - D _s m² s^–1 intraparticle diffusivity - d _p m particle diameter - E _z m² s^–1 longitudinal diffusivity of the protein - E _{z I} m² s^–1 longitudinal diffusivity of ionic strength - H /(1 – ) - I kmol m^–3 ionic strength - I _O kmol m^–3 initial ionic strength - I _p kmol m^–3 ionic strength at the peak - I _s kmol m^–3 ionic strength in the solid phase - I/V mol (dm³)^–2 slope of the ionic gradient elution - m distribution coefficient - m distribution coefficient at I - m _I distribution coefficient for ionic strength - Q cm³s^–1 flow rate - R m particle radius - R _s degree of separation - r m radial position inside particles - t s time - u m s^–1 linear velocity - V cm³ eluted volume of liquid - V _p cm³ eluted volume of liquid at the peak - V _T cm³ volume of the packed bed - W cm³ peak width - Z m bed height - z m vertical position in the bed - z _p m peak position from the inlet of the bed - (t) delta input at time - void fraction - ₁ s first moment - ₂ s² second central moment - s superficial space time