Effect of serum concentration on production of monoclonal antibodies and on shear sensitivity of a hybridoma

The effect of serum content of culture medium on the specific production rate of monoclonal antibodies (Mab's) and on shear sensitivity has been studied with hybridoma's, cultured in a continuous stirred tank reactor (CSTR). No decrease in specific Mab-production was found when the serum concentration was reduced from 10 to 2.5%, while steady state cell concentrations were hardly affected as well. In contrast the cell death rate in a bubble column strongly increased when the serum concentration was lowered, which could be ascribed to a reduced physical protective effect by the serum.List of Symbols k _d s^–1 death-rate constant - k _g s^–1 growth-rate constant - D m diameter of bubble column - d m diameter of air bubble - H m height of bubble column - X m³ hypothetical killing volume - X (m³/m³) specific hypothetical killing volume - F m³/s volumetric air-flow rate - C cells/m³ number of viable cells - C₀ cells/m³ number of viable cells at t=0 - t s time     

Bubble coalescence behaviour in biological media

Summary Volumetric mass transfer coefficients (k_La) were measured by a steady state method in a twin bubble column to characterize the coalescence behaviour of the medium. Employing Hansenula polymorpha cultivation broths, k_La values were compared with those measured in model media in the presence and absence of antifoam agents. The ratio of the volumetric mass transfer coefficient in the system investigated to that in water, , was employed to characterize the cultivation medium.Symbols a Specific gas/liquid interfacial area with regard to the liquid volume in reactor - d_e Dynamical equilibrium bubble diameter - d_H Perforated plate hole diameter - d_p Primary bubble diameter - d_S Sauter bubble diameter - F_v Liquid feed rate - H Bubbling layer height - k_L Gas/liquid mass transfer coefficient - k_La Volumetric mass transfer coefficient - m k_La/(k_La)_r coalescence index - m_corr Corrected coalescence index [Eq. (3)] - OTR Oxygen transfer rate - P_O Dissolved O₂-partial pressure in BS2 - P₁ Dissolved O₂-partial pressure in BS1 - P_O P_O/P_S relative oxygen saturation in BS2 - P₁ P₁/P_S relative oxygen saturation in BS1 - P_S Saturation dissolved oxygen partial pressure - R_c dn_B/dt coalescence rate - S Substrate concentration - t_F Time since the beginning of the cultivation - X Biomass concentration - V₁ Liquid volume in BS1 - w_SG Superficial gas velocity in BS1 - G Gas holdup in BS1 - ₁ V₁/F_v mean liquid residence time in BS1 - BS1 O₂ absorber column - BS2 O₂ desorber column - D Desmophen (antifoam agent) - NS Nutrient salt solution (Table 1)     

Gas holdup and mass transfer characteristics of carboxymethyl cellulose solutions in a bubble column with a radial gas sparger

The gas phase holdup and mass transfer characteristics of carboxymethyl cellulose (CMC) solutions in a bubble column having a radial gas sparger have been determined and a new flow regime map has been proposed. The gas holdup increases with gas velocity in the bubbly flow regime, decreases in the churn-turbulent flow regime, and increases again in the slug flow regime. The volumetric mass transfer coefficient (k _La) significantly decreases with increasing liquid viscosity. The gas holdup and k _La values in the present bubble column of CMC solutions are found to be much higher than those in bubble columns or external-loop airlift columns with a plate-type sparger. The obtained gas phase holdup ( _g) and k _La data have been correlated with pertinent dimensionless groups in both the bubbly and the churn-turbulent flow regimes.List of Symbols a m^–1 specific gas-liquid interfacial area per total volume - A _d m² cross-sectional area of downcomer - A _r m² cross-sectional area of riser - d _b m individual bubble diameter - d _vs m Sauter mean bubble diameter - D _c m column diameter - D _L m²/s oxygen diffusivity in the liquid - Fr Froude number, U _g/(g D_c)^1/2 - g m/s² gravitational acceleration - G _a Galileo number, gD _c ^{3 2}/² _app - H _a m aerated liquid height - H _c m unaerated liquid height - K Pa · sⁿ fluid consistency index - k _L a s^–1 volumetric mass transfer coefficient - n flow behavior index - N _i number of bubbles having diameter d _bi - Sc Schmidt number, _app/( D _L) - Sh Sherwood number, k _L a D _c ² /D_L - U _sg m/s superficial gas velocity - U _gr m/s superficial riser gas velocity - V _a m³ aerated liquid volume - V _c m³ unaerated liquid volume - N/m surface tension of the liquid phase - _g gas holdup - _app Pa · s effective viscosity of non-Newtonian liquid - kg/m³ liquid density - ý s^–1 shear rate - Pa shear stress     

Mass transfer and liquid mixing in an airlift reactor with a net draft tube

Mass transfer and liquid mixing in an airlift reactor with a net draft tube were experimentally investigated. Four different column diameters were considered. The mass transfer was measured using the volumetric gas-liquid mass transfer coefficient which was determined by the dynamic method. The mass transfer coefficients in the airlift reactors with different column diameters were not always higher than those in the bubble columns. The liquid mixing was measured using mixing time which was determined by a pulse technique. Under the same superficial gas velocity, the mixing times of the airlift reactors with a net draft tube were always less than those of the bubble columns.List of Symbols C mol·dm^–3 bulk concentration of dissolved oxygen - C ₀ mol·dm^–3 initial concentration of dissolved oxygen - C _e mol·dm^–3 saturated concentration of dissolved oxygen - ¯C dimensionless dissolved oxygen concentration - D _c cm diameter of column - D _N cm diameter of the nozzle hole - D _T cm diameter of the net draft tube - H _L cm static liquid height - H _T cm height of the net draft tube - k _L a hr^–1 volumetric mass transfer coefficient - L _T cm length of the net draft tube - t _M sec mixing time of the liquid phase - t ₀ sec mixing time of the liquid phase in a bubble column - V _L dm³ volume of the liquid phase - U _g cm/s superficial air velocity     

Hydrolysis Rate of Resistant Pentosan of White Birch Wood in Sulfuric Acid of Medium Strength

The purpose of this study is to find optimal conditions for pre-hydrolysis in the new wood saccharification process with strong sulfuric acid. In the experiment, the hydrolysis rate of resistant fraction of pentosan of white birch (Shirakamba, Betula platyphylla Sukatchev var. japonica Hara) wood and the decomposition rate of xylose are measured in acid concentrations ranging from 30 to 60% at temperatures ranging from 30 to 90°C. The hydrolysis of resistant pentosan of white birch and the decomposition of xylose are the first-order reactions. The first-order reaction constant of hydrolysis of resistant pentosan, k_B min^-1, is expressed by the following empirical equations as the function of percentage concentration of sulfuric acid, C, and reaction temperature described by absolute temperature, T°K, ranging from 40 to 80°C:

where sulfuric acid concentrations range from 30 to 50%;

where sulfuric acid concentration is 60%.

The first-order reaction constant of decomposition of xylose, k₂ min^-1, is expressed by the following empirical equation as the function of sulfuric acid strength described by acidity function, H₀, and reaction temperature described by absolute temperature, T°K, in sulfuric acid concentrations ranging from 30 to 60% at temperatures within the range of 40 to 100°C.

where C is sulfuric acid strength described by acidity function, H₀.     

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

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

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.     

Cyclobranol: a substrate for C25-methyl sterol side chains and potent mechanism-based inactivator of plant sterol methyltransferase

Cyclobranol 8A, an analog of the cycloartenol substrate 1A for the plant sterol C24-methyltransferase (SMT), was shown to be an acceptor of the soybean SMT1 as well as an inhibitor of enzyme action. The K_m and k_cat for 8A was 37 μM and 0.006 min⁻¹, respectively. The enzyme-generated product was identified by MS and ¹H NMR to be a C24, C25-doubly alkylated Δ²⁴⁽²⁸⁾-olefin 10A. Inhibitor treatment was concentration and time-dependent affording an apparent K_i of 25 μM, a maximum rate of inactivation of 0.15 min⁻¹ and a partition ratio (k_cat/k_inact) calculated to be 0.04.     

Comparative analysis of oxygen transfer rate distribution in stirred bioreactor for simulated and real fermentation broths

Study of the distribution of the oxygen mass transfer coefficient, k _l a, for a stirred bioreactor and simulated (pseudoplastic solutions of carboxymethylcellulose sodium salt) bacterial (P. shermanii), yeast (S. cerevisiae), and fungal (P. chrysogenum free mycelia) broths indicated significant variation of transfer rate with bioreactor height. The magnitude of the influence of the considered factors differed from one region to another. As a consequence of cell adsorption to bubble surface, the results indicated the impossibility of achieving a uniform oxygen transfer rate throughout the whole bulk of the microbial broth, even when respecting the conditions for uniform mixing. Owing to the different affinity of biomass for bubble surface, the positive influence of power input on k _l a is more important for fungal broths, while increasing aeration is favorable only for simulated, bacterial and yeast broths. The influence of the considered factors on k _l a were included in mathematical correlations established based on experimental data. For all considered positions, the proposed equations for real broths have the general expression k_l a = aC_X^b ( \fracP_a V )^g v_S^d , k_{\rm l} a = \alpha C_{\rm X}^{\beta } \left( {{\frac{{P_{\rm a} }}{V}}} \right)^{\gamma } v_{\rm S}^{\delta } , exhibiting good agreement with experimental results (with maximum deviations of ±10.7% for simulated broths, ±8.4% for P. shermanii, ±9.3% for S. cerevisiae, and ±6.6% for P. chrysogenum).     

Modification of Human Erythrocyte Pyruvate Kinase by an Active Site-directed Reagent: Bromopyruvate

Human erythrocyte pyruvate kinase was modified with bromopyruvate and the kinetic behavior of the modified enzyme was investigated. When the enzyme was modified with bromopyruvate in the absence of adenosine-5′s-diphosphate, phospho-enolpyruvate or fructose-1,6-diphosphate the inactivation followed a pseudo first-order kinetics. The inactivation rate constant, k_s, was 1.84 × 0.15 min^?1. K_d of the bromopyruvate-enzyme complex was 0.14 × 0.03 mM.

The presence of adenosine-5′-diphosphate, phosphoenolpyruvate or fructose-1,6-diphosphate in the modification medium or the presence of fructose-1,6-diphosphate in the assay medium resulted in deviation of the inactivation kinetics from pseudo first-order. Phosphoenolpyruvate was better than adenosine-5′-diphosphate for protection against bromopyruvate modification whereas fructose-1,6-diphosphate was ineffective. The modified enzyme showed negative cooperativity in the presence of fructose-1,6-diphosphate whereas in the absence of it no activity was detected.     

Analysis of theD-region products ofH-2444using monoclonal antibodies reveals the expression of a new class I-like molecule

To analyze how many D-region-encoded molecules could be detected inH-2 ^q , we produced a panel of nine monoclonal antibodies from AKR (K^kD^k) anti-AKR.M (K^kD^q) immunizations. All of the D_q region antibodies cross-reacted on D^d and/or L^d, and all except one cross-reacted on D^b, confirming the previously observed serologic and amino acid sequence homology between theD-region products ofH-2 ^d ,H-2 ^b , andH-2 ^q . All of these monoclonal antibodies precipitated 46 000 dalton molecules from both cell-surface-labeled and biosynthetically labeled BIO.AKM spleen cells, indicating that all were reactive with class I-like molecules. Sequential immunoprecipitation analysis with one of these antibodies, 66-3-5, reveals the presence of a previously unidentified class I-like molecule. Tryptic peptide map analysis reveals that this molecule may be the product of a newly describedH-2D ^q -region gene.     

Mixing time and oxygen transfer characteristics of double draft tube airlift fermentor

Despite the increasing importance of airlift fermentors, very little published information is available on how the geometric configurations of the draft tubes and the air-sparging system affect the mixing and oxygen transfer characteristics of the fermentor. A 14-L air-lift fermentor was designed and build with a fixed liquid height to diameter ratio of 1.5 utilizing four equally spaced air jets at the bottom. Two jet orifice sizes were used, 1.27 and 3.81 mm i.d., and for each jet size the following four geometric configurations were used: Single inner concentric draft tube, single outer concentric draft tube, two concentric draft tubes, and no draft tubes where the fermentor was operated as a shallow bubble column. It was found that the presence of draft tubes stabilized liquid circulation patterns and gave systemically higher mixing times than those obtained in the absence of draft tubes. In addition, the double draft tube geometry resulted in higher mixing times than the single draft tubes. For the power unit volume range 20 to about 250 W/m³ the larger 3.81-mm orifices gave systemically higher k_L a values than the smaller 1.27-mm i.d. orifices. At 200 W/m³ the use of a single outer draft tube with the 3.81-mm orifices resulted in 94% increase in k_L a values over that obtained with no draft tubes. However, the effect of draft tube geometry on k_L a values when the 1.27-mm orifices were used was not significant. The air bubble formation characteristics at the jet orifices were found to be different, which reflected the differences observed in mass transfer and mixing characteristics. The power economy for oxygen transfer was found to be depend strongly on the orifice size and less on the geometric configuration of draft tubes.     

On the difference between gauss-markov and least squares estimates

For the usual full rank univariate least squares regression model y = XB + e, E(e) = 0, E(ee) = A, the equality of the estimates occurs when B-B^* = (XA^?1X)^?1XA^-1y-(XX)^?1Xy = 0. A necessary and sufficient condition for this equality is that A has some N - k + 1 roots equal where N is the rank of A and k is the rank of X.     

Interactions of highly charged colloidal cylinders with applications to double-stranded DNA

This paper presents new applications of the McMillan-Mayer solution theory to dispersions of highly charged colloidal cylinders in monovalent salt solutions. The thermodynamic solution properties are given in terms of the virial expansions relating to a Donnan membrane equilibrium. General expressions are derived for the second Donnan pressure virial coefficient B₂ and for the first two salt distribution coefficients A₁ and A₂. The effect of electric interactions is represented as an increased effective diameter d_B or d_A of the colloidal cylinder. This yields the simple excluded volume expressions B₂ = πd_BL²/4 and A₁ = πd_A²L/4 for hard cylinders of length L and diameter d_B and d_A, respectively. The coefficient A₂ is derived from the dependence of B₂ on the salt concentration. Computations are made for double-stranded DNA in sodium chloride solutions with the DNA model developed in the preceding paper: a uniformly charged cylinder, with size and charge consistent with transport experiments, and surrounded by a Gouy double layer. In 1–0.005M sodium chloride solutions d_B is found to vary from 29 Å to about 220 Å, and d_A from 30 Å to about 170 Å, with little sensitivity to the uncertainties in the kinetic diameter d ≈ 24 Å and the experimental ζ potentials of DNA. Corresponding results predicted by the classical Donnan theory are 6–167 times too high for B₂. Values of A₂ are relatively small, in line with the expected rapid convergence of the virial expansion for the salt distribution. This is consistent with a phase transition from random to parallel orientation of the cylinders predicted first by Onsager for hard cylinders on the basis of B₂, but not yet observed for DNA in simple salt solutions.     

Improved hydrogen photoproduction regulated by carbonylcyanide <Emphasis Type="Italic">m</Emphasis>-chlorophenylhrazone from marine green alga <Emphasis Type="Italic">Platymonas subcordiformis</Emphasis> grown in CO<Subscript>2</Subscript>-supplemented air bubble column bioreactor

To develop an integrated process of CO₂-fixation and H₂ photoproduction by marine green microalga Platymonas subcordiformis, the impact of algal cells grown in CO₂-supplemented air bubble column bioreactor was investigated on H₂ photoproduction regulated by carbonylcyanide m-chlorophenylhrazone. Highest cell growth (3.85 × 10⁶ cells ml⁻¹), starch content (0.25 ± 0.08 mg per 10⁶ cells) and hydrogen production (50 ± 3 ml l⁻¹) were achieved at 3% CO₂-supplemented culture, which are respectively 1.4, 2.1, 1.5-fold of the air-supplemented culture. Improved H₂ production correlated well with the increase in starch accumulation. In this process, the algal cells have been recycled for stable H₂ production of 40–50 ml l⁻¹ over five cycles.     

Biosorption of Malathion using dry cells of Bacillus species S14 in a packed bed column reactor

Abstract

The ability of dried bacterial strain Bacillus sp. S₁₄ to adsorb Malathion in a packed bed column reactor was studied. The effects of important design parameters such as bed height, flow rate and influent Malathion concentration on Malathion removal from an aqueous solution was studied using a packed bed column reactor. The optimised conditions for maximum Malathion removal were found to be: flow rate: 5 mL min^-1, bed height: 6.0 cm and influent Malathion concentration: 25 mg L^-1. The Adams-Bohart model, Wolborska model, Thomas model, Yoon and Nelson Model were employed to determine characteristic parameters such as N₀ (saturation concentration, mg L^-1), β_o (external mass transfer coefficient, min^-1), k _Th(Thomas rate constant, mL min^-1mg^-1), q₀ (maximum solid phase concentration of the solute, mg L^-1), k_YN (rate constant, min^-1) and τ (time required for 50 % adsorbate breakthrough time, min) which are useful for process design. Data were fitted with Adams-Bohart model at lower region of (C/C₀) values but more accurately fitted with Wolborska and Thomas model.     

Hierarchical Classification I: Single-Linkage Method

This is the first part of a survey of hierarchical clustering algorithms using joining methods: the Single-Linkage algorithm. Complete-Linkage and general algorithms defined by d(A_i, B) = = α,d(A_i, A_r)±α_sd(A_i, A_s)±βd(A_r, A_s) will be discussed in two subsequent papers.     

Suicide-Peroxide inactivation of microperoxidase-11: A kinetic study

The kinetics of microperoxidase-11 (MP-11) in the oxidation reaction of guaiacol (AH) by hydrogen peroxide was studied, taking into account the inactivation of enzyme during reaction by its suicide substrate, H₂O₂. Concentrations of substrates were so selected that: 1) the reaction was first-order in relation to benign substrate, AH and 2) high ratio of suicide substrate to the benign substrate, [H₂O₂]>>[AH]. Validation and reliability of the obtained kinetic equations were evaluated in various nonlinear and linear forms. Fitting of experimental data into the obtained integrated equation showed a close match between the kinetic model and the experimental results. Indeed, a similar mechanism to horseradish peroxidase was found for the suicide-peroxide inactivation of MP-11. Kinetic parameters of inactivation including the intact activity of MP-11, α_i, and the apparent inactivation rate constant, k_i, were obtained as 0.282 ± 0.006 min^{? 1} and 0.497 ± 0.013 min^{? 1} at [H₂O₂] = 1.0 mM, 27°C, phosphate buffer 5.0 mM, pH = 7.0. Results showed that inactivation of microperoxidase as a peroxidase model enzyme can occur even at low concentrations of hydrogen peroxide (0.4 mM).     

Cell wall strength of Hansenula polymorpha in continuous cultures in relation to the recovery of methanol oxidase (MOX)

Summary The changes in cell wall strength of Hansenula polymorpha have been investigated in continuous cultures with respect to the recovery of methanol oxidase (MOX). Cultures grown on several substrate mixtures that enable induction of MOX have been compared with cultures grown on methanol as the sole inducer. The effects of dilution rate (D) on lysis properties have been studied. The cell wall strength was consistently influenced by growth media and D. Media containing glycerol/methanol showed the slowest lysis kinetics, with a large fraction of non-degradable cell wall material. In continuous cultures grown on a mixture of glucose and methanol both the resistance to zymolyase and the mean cell wall thickness increased at D<0.1 h^–1. The yield of MOX by zymolyase lysis is reproducible and up to 100% higher than that of the standard ultrasonic treatment. The lysis kinetics indicated that zymolyase punctures the cell wall; since the release rate of MOX is lower than that of protein, the cell contents will leak through. At D-values>0.2 h^–1, both protein and MOX release rates increase, reflecting a change in lysis mechanism due to the increased fraction of thin daughter cells. Kinetic analysis of zymolyase lysis using both physical and enzymatic methods provides information for achieving optimal recovery of MOX.Abbreviations and symbols C _MOX MOX activity [MOX units·g X^–1] - D dilution rate [h^–1] - MOX methanol oxidase - k_c decay rate constant of A 610 nm [min^–1] - k_d decay constant of MOX activity [min^–1] - k_dis dissociation rate constant [min^–1] - k_MOX release rate constant of MOX activity [min^–1] - k_p release rate constant of protein [min^–1] - R recovery efficiency of enzyme [-] - St stability of enzyme [-]     

Comparison of photobioreactors for cultivation of Undaria pinnatifida gametophytes

Undaria pinnatifida gametophytes were grown in 2.5 l bubble column and airlift reactor at 25 °C and light intensity of 40 mol m^–2 s^–1 for 6 days. With aeration at 1 l min^–1, the airlift reactor yielded higher growth rate (0.12 mg DW ml^–1 d^–1) than a bubble column (0.08 mg DW ml^–1 d^–1). The advantages were related to the more homogeneous fluid dynamic characteristics of the airlift reactor.