Isolation and purification of protease from human placenta by foam fractionation

The effect of operating parameters like pH, protein concentration, column geometry, and gas flow rate on the separation efficiency of proteolytic enzymes from crude human placental homogenate has been studied in a batch foam column. Purification has been found to be optimum at pH 8.0, close to the isoelectric pH, at which the surface adsorption of the protein on the foam bubbles is maximum. Both purification and recovery varied significantly with total protein concentration. Stable bubble formation was hindered at lower protein concentrations, while extraneous proteins rather than the protease were preferentially adsorbed at higher protein concentrations, decreasing the purification efficiency. Column diameter and column height should be optimized for any specific feed protein concentration and gas flow rate. However, the enrichment ratio was found to decrease with the increase in flow rate. The results indicate that foam fractionation is an effective separation process for recovering valuable biochemicals from biological materials.     

Foam fractionation of globular proteins

Foam fractionation of bovine serum albumin (BSA) was studied as a model system for potato wastewater. The effects of feed concentration, superficial gas velocity, feed flow rate, bubble size, pH, and ionic strength on the enrichment and recovery of BSA were investigated in a single-stage continuous foam fractionation column. Enrichments ranged from 1.5 to 6.0 and recoveries from 5 to 85%. The feed concentrations were varied from 0.01 to 0.2 wt %, and enrichments were found to increase with lower feed concentrations. Enrichments also increased with lower superficial gas velocities and larger bubble sizes. At sufficiently low feed flow rates, enrichment was found to increase with an increase in the flow rate, eventually becoming insensitive to the feed flow rate at higher values. The pH was varied from 3.5 to 7.0 and ionic strength from 0.001M to 0.2M. The effects of pH and ionic strength were found to be coupled with bubble size. A minimum bubble size was found at pH 4.8, the isoelectric point of BSA, resulting in a minimum in the enrichment. Bubble size, and thus enrichment, was found to increase as the ionic strength decreased from 0.2M to 0.01M. Previous models(1,2) for the hydrodynamics of foam column were extended for a singlestage continuous foam fractionation column for the prediction of enrichment and recovery. The model assumed adsorption equilibrium, infinite surface viscosity, and bubbles of the same size. Though coalescence was formally accounted for in the model by considering bubble size as a function of foam height, calculations for the experimental runs were performed only for the case of no coalescence. Quantitative predictions of enrichment and recovery could not be made with a single representative bubble size because of the broad inlet bubble size distribution as well as broadening of the distribution as a result of coalescence. The experimental enrichments were higher and recoveries were lower than the model predictions, the discrepancy being more pronounced at lower feed concentrations because of increased coalescence. The higher enrichments are due to the predominant effect of internal reflux as a result of coalescence whereas the lower recoveries are a result of detrimental effects of broadening bubble size distributions.     

Enrichment in axial direction of aqueous foam in continuous foam separation

Estimation of overhead production enrichment in continuous foam separation was conducted with a surfactant: sodium n-dodecylbenzenesulfonate (SDBS) and soluble proteins: ovalbumin (OA) and hemoglobin (HB). Axial profiles of the volumetric flow rate and the concentration of the collapsed foam liquid within the column were measured, and the enrichment ratio and the liquid holdup in axial direction were determined experimentally. The proposed model was fitted to the experimental results obtained with various experimental conditions (superficial gas velocity, feed concentration and pH) and was in reasonable agreement with the experimental data by using the least square regression. The present model makes it possible to estimate the foamate concentration at a desired foam height.     

Continuous foaming for protein recovery: part I. Recovery of beta-casein

Foam separation is known to have potential for separation of biological molecules with a range of surface activities. A statistical study (factorial design) was carried out to establish the optimum operating conditions for the continuous foam separation of beta-casein. Maximum values of enrichment of beta-casein into the foam phase were found for low levels of initial feed protein concentration, gas flow rate, feed-flow rate, and high foam heights. Maximum values of protein recovery, were generally found at high levels of initial feed protein concentration, gas-flow rate, feed-flow rate, and low foam heights. The highest values obtained for enrichment and separation ratio were 54.7 and 181.3, respectively, with a simultaneous protein recovery of 62%; thus, illustrating the potential effectiveness of this technique. The effect of foaming on protein conformation is also important, and in this study protein structure was analyzed before and after foam separation experiments. Techniques used were: native polyacrylamide gel electrophoresis (PAGE), UV absorbance spectroscopy, circular dichroism, and fluorescence. Native PAGE showed no detectable changes in protein structure. However, absorbance scanning, fluorimetry, and circular dichroism revealed some conformational changes over a range of concentration effects.     

泡沫分离技术研究进展

本综述了泡沫分离技术的研究进展,介绍了分离过程中操作参数（气流速度,泡沫区高度,液相高度,温度）,溶液体系性质（进料浓度,pH值,离子强度,表面活性剂种类）,分离设备等因素对分离效果的影响,并介绍了泡沫分离在固体粒子,溶液中的离子分子,废水处理以及生物产品的分离过程中的应用,指出了泡沫分离技术目前存在的问题及发展方向。     

Effects of kinetics of adsorption and coalescence on continuous foam concentration of proteins: Comparison of experimental results with model predictions

Protein enrichment and recovery were measured in a continuous foam concentration column for bovine serum albumin (BSA) for different pool heights, foam heights, superficial gas velocities, bubble sizes, feed flow rates, pH, and ionic strengths. Protein enrichment was found to decrease with an increase in pool height for low pool heights, reach a minimum at an intermediate pool height, and subsequently increase with pool height for sufficiently large pool heights eventually approaching an asymptotic value. Such a behavior was due to the combined effects of kinetics of adsorption of protein and coalescence. The increase in protein enrichment with pool height was due to the predominant effect of kinetics of adsorption of protein, whereas the opposite behavior at low pool heights was due to the predominant effect of coalescence in the foam. Protein enrichment was found to be higher for smaller feed concentrations, smaller gas velocities, larger bubble sizes, and larger foam heights. Enrichment at pH values different from the isoelectric point was found to be higher because of more coalescence. A model for foam concentration of proteins was employed to predict enrichment and recovery. The model predictions agreed well with the experimental data. (c) 1996 John Wiley & Sons, Inc.     

Mechanical control of foaming in a bubble column

This study was performed to evaluate the effects of the air sparge rate, working liquid volume, liquid feed rate onto the disk, and disk diameter on the foam-breaking performance of foam-breaking apparatus with a rotating disk (FARD) installed in the bubble column. Experimental results showed that the smaller the air sparge rate and working liquid volume were, and the larger the liquid feed rate and disk diameter, the lower the critical disk rotational speed required for reduced foam-breaking. The presence of the effective ranges of the disk diameter and liquid feed rate for foam breaking was also confirmed. Furthermore, the quantitative predictions of the upper limits of the liquid feed rate, foam-breaking regions, and the required foam-breaking power were carried out, based on the results obtained above. Comparison of the FARD with two conventional mechanical foam-breaking spray-type apparati also demonstrated the highest level of the FARD in respect not only to foam-breaking performance but also to power requirements.     

Foam separation of microbial cells

Batch foam separation has been employed to separate Saccharomyces carlsbergensis cells from their broth without the use of any external surface-active agent. A model has been developed to predict the foamate cell concentration as well as the variation of cell concentration in the bulk liquid in the foam column as a function of time. The model assumes a linear equilibrium relation between the cell concentrations at the interface and the bulk. The foam has interface as well as interstitial liquid. The interface is assumed to be in equilibrium with the interstitial liquid, which in turn is assumed to have the same concentration as the bulk. The interfacial area is calculated by assuming the foam bubbles to be pentagonal dodecahedral in shape. The model has been found to explain the results of foam separation of cells quite well, particularly with respect to the effect of bubble size and aeration rate.     

Purification of alkaline protease of Rhizopus oryzae by foam fractionation

Studies on the cost effective purification method is very much essential for the industrially important enzyme like protease. As foam fractionation is an important technique in downstream processing of the biologicals, purification of the crude proteolytic enzyme produced by Rhizopus oryzae has been attempted using converging-diverging foam fractionator. The effects of different parameters studied on the purification efficiency by foam fractionation were pH of the broth, air flow rate, initial liquid height. The results obtained were found quite encouraging at pH 10 with 1 LPM of air flow rate at low initial liquid height.     

The influence of polymeric membrane gas spargers on hydrodynamics and mass transfer in bubble column bioreactors

Gas sparging performances of a flat sheet and tubular polymeric membranes were investigated in 3.1 m bubble column bioreactor operated in a semi batch mode. Air–water and air–CMC (Carboxymethyl cellulose) solutions of 0.5, 0.75 and 1.0 % w/w were used as interacting gas–liquid mediums. CMC solutions were employed in the study to simulate rheological properties of bioreactor broth. Gas holdup, bubble size distribution, interfacial area and gas–liquid mass transfer were studied in the homogeneous bubbly flow hydrodynamic regime with superficial gas velocity (U _G) range of 0.0004–0.0025 m/s. The study indicated that the tubular membrane sparger produced the highest gas holdup and densely populated fine bubbles with narrow size distribution. An increase in liquid viscosity promoted a shift in bubble size distribution to large stable bubbles and smaller specific interfacial area. The tubular membrane sparger achieved greater interfacial area and an enhanced overall mass transfer coefficient (K _La) by a factor of 1.2–1.9 compared to the flat sheet membrane.     

Flotation for cell recovery from small volumes of yeast cultures

Flotation or cell recovery in foams (proportion of the total cells in the medium transferred to the foam) and flotation efficiency (proportion of the cells transferred from an initial volume of medium equal to the residual volume after flotation) are functions of time, aeration rate, initial volume of medium, and initial concentration of cells. Cell recovery reached constant values (around 96.4 ± 6.3%) and flotation efficiency decreased (owing to increases in the liquid content of the foam), with increases in air flow rate (above 6–7 ml air s^–1) and volumes of medium (above 11 ml) added to the column. Increases in concentration of cells in the medium led to increases in the concentration of cells in the foam.     

Separation of gentamicin by foaming

In order to develop a more economical separation method and to determine the feasibility of such a method for the recovery of gentamicin from fermentation broth, a foam separation process was evaluated using a batch system. The effects of such process variable as surface-active agent, pH, collector–colligent ratio, and the gas flow rate on the separation efficiency of gentamicin were studied. Form the experimental results, the optimal operating conditions selected were: pH below 9.0, collector-to-colligent ratio of 3, and airflow rate at 0.5 vol air/vol liquid/min. Under these operation conditions, the average recovery efficiency of gentamicin was 73% when sodium dodecyl sylfate was used as a collector. A mathematical expression for the foam separation rate was derived. The theoretically predicted values of separation efficiencies agreed reasonably well with the experimental results.     

High oxygen transfer rate in a new aeration system using hollow fiber membrane

A new type of bubble aeration column called a hollow fiber membrane (HFM) aeration column was proposed, which was featured in the use of hollow fiber membranes and gave a high bubble density in the column. The value of k(L)a was increased by modifying the membrane surface for making the pore size smaller. The Sauter mean diameter of bubbles (D(vs)) was 2.0 +/- 0.1 mm in the range of the superficial gas velocity from 0.02 m s(-1) to 0.065 m s(-1), while that obtained for the bubbles near the membrane was 811 mum at the superficial gas velocity of 4.0 x 10(-4) m s(-1). The difference was ascribed to the effect of coalescence of bubbles. The value of K(L)a increased in proportion to the superficial gas velocity up to 0.02 m s(-1), and was almost constant above 0.03 m s(-1). The maximum value of k(L)a, 2.5 s(-1), was higher than those of the other aeration columns reported previously. The pneumatic power consumption per unit liquid volume (P(v)) for obtaining the same k(L)a was the smallest in the HFM aeration columns. P(v), for obtaining the same interfacial area of bubbles per liquid volume, was also lower than those for other types of aeration columns. It was suggested from the measurement of bubble diameter that the larger interfacial area generated in the HFM aeration column ascribes to the larger gas holdup than the smaller D(vs). (c) 1992 John Wiley & Sons, Inc.     

Cell recovery by continuous flotation

Summary Cell recovery by means of continuous flotation of the Hansenula polymorpha cultivation medium without additives was investigated as a function of the cultivation conditions as well as of the flotation equipment construction and flotation operational parameters. The cell enrichment and separation is improved at high liquid residence times, high aeration rates, small bubble sizes, increasing height of the aerated column, and diameter of the foam column. Increasing cell age and cultivation with nitrogen limitation reduce the cell separation.Symbols C_P cell mass concentration in medium g·l^–1 - C_R cell mass concentration in residue g·l^–1 - C_S cell mass concentration in foam liquid g·l^–1 - V equilibrium foam volume cm³ - V gas flow rate through the aerated liquid column cm³·s^–1 - V_F feed rate to the flotation column ml/min - ¹ V _S/V foaminess s - mean liquid residence time in the column s     

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.     

Technology of streptomycin sulfate separation by two-stage foam separation

Industrial discharges from manufacturing streptomycin sulfate (SS) are inhibitory to biological wastewater treatment and need to be stripped of residual SS. For effective SS recovery from the wastewater, a two-stage foam separation technology was investigated using a column with a vertical ellipsoid-shaped channel (VEC) and a conventional one, and sodium dodecyl sulfate (SDS) served as the collector. The mechanism of enhancing foam drainage by VEC was theoretically analyzed. In the first stage, the column with VEC was used and under the optimal conditions of the liquid-loading volume 300 mL, volumetric airflow rate 100 mL/min, the initial pH 7.0 and the molar ratio of SDS to SS 8.0, an improved SS enrichment ratio of 16.7 was obtained. In the second stage, a conventional column was used and with a volumetric airflow rate of 450 mL/min, the foamate had a SS concentration of about 0.5 g/L, so it was used as the feed solution of the first stage. By the two-stage technology, the total SS recovery percentage reached as high as 99.7%. Thus, it was significantly effective for the two-stage foam separation technology to recover SS from the simulative wastewater.     

Variables in the high-pressure cation-exchange chromatography of proteins

The use of cation-exchange high-pressure liquid chromatography for the separation of proteins has been investigated. Several factors, including solvent composition, pH, flow rate, and temperature, were examined for their effects on the resolution of protein standards (insulin, β-lactoglobulin, and carbonic anhydrase B; molecular weight range, 6000 to 30,000 and pI range, 5.3 to 6.5). An initial comparison was made of the recovery of these proteins from three commercially available columns (Whatman Partisil SCX, Separation Industry CM silica, and MCB Reagents Lichrosorb KAT). In general, under the conditions employed, the SCX column gave the highest recovery of applied protein. Based on this recovery data, the Partisil SCX column was chosen for subsequent examination of chromatographic parameters that would optimize protein resolution. An increase in temperature decreased retention and resolution but increased recovery, with some proteins being affected more than others. A decrease in pH in the final eluant or an increase in pH in the initial eluant caused an increase in retention times. For some proteins, the decrease in pH resulted in a greater total recovery of protein. This information has been applied to the purification by cation-exchange high-pressure liquid chromatography of transforming growth factors from a human tumor cell line.     

Death rate in a small air-lift loop reactor of vero cells grown on solid microcarriers and in macroporous microcarriers

The death rate of Vero cells grown on Cytodex-3 microcarrierswas studied as a function of the gas flow rate in a smallair-lift loop reactor. The death rate may be described byfirst-order death-rate kinetics. The first-order death-rateconstant as calculated from the decrease in viable cells, theincrease in dead cells and the increase in LDH activity islinear proportional to the gas flow rate, with a specifichypothetical killing volume in which all cells are killed ofabout 2.10(-3)m(3) liquid per m(3) of air bubbles.In addition, an experiment was conducted in the sameair-lift reactor with Vero cells grown inside porous Asahimicrocarriers. The specific hypothetical killing volumecalculated from this experiment has a value of 3.10(-4)m(3) liquid per m(3) of air bubbles, which shows thatthe porous microcarriers were at least in part able to protectthe cells against the detrimental hydrodynamic forcesgenerated by the bubbles.     

Effect of pH on successive foam and sonic droplet fractionation of a bromelain-invertase mixture

A droplet fractionation method was previously developed to concentrate a dilute nonfoaming protein solution. In that earlier study with invertase, it was demonstrated that droplets created by ultrasonic energy waves could be enriched up to 8 times that of the initial dilute invertase solution. In this study, a mixture of bromelain (a foaming protein) and invertase (a nonfoaming protein) is investigated as a preliminary step to determine if droplet fractionation can also be used to separate a non-foaming protein from foaming proteins. The foaming mixture containing bromelain is first removed by bubbling the binary mixture with air. After the foam is removed, the protein rich air-water interfacial layer is skimmed off (prior to droplet fractionation) so as not to interfere with the subsequent droplet production from the remaining bulk liquid, rich in non-foaming protein. Finally, sonic energy waves are then applied to this residual bulk liquid to recover droplets containing the non-foaming protein, presumed to be invertase. The primary control variable used in this droplet fractionation process is the pH, which ranged for separate experiments between 2 and 9. It was observed that the maximum overall protein partition coefficients of 5 and 4 were achieved at pH 2 and 4, respectively, for the initial foaming experiment followed by the post foaming droplet fractionation experiment.     

Minimization of aggregation of secreted bivalent anti-human T cell immunotoxin in Pichia pastoris bioreactor culture by optimizing culture conditions for protein secretion

In a bioreactor culture of genetically engineered Pichia pastoris secreting a bivalent immunotoxin, 64% of the secreted immunotoxin was present in aggregate forms and this resulted in a loss of bioactivity. Biochemical analyses of the secreted immunotoxin and an in vitro aggregation study using purified monomeric immunotoxin suggested that aggregation was primarily an extracellular event. By employing limited methanol feeding at 0.75 mlmin(-1) per 10l initial medium, oxygen consumption was reduced, permitting a lowering of the bioreactor agitation speed from 800 to 400 rpm. By increasing the anti-foam reagent to 0.6 mll(-1), the thickness of the air/liquid interfacial foam layer was reduced by 80%. These steps reduced the immunotoxin aggregates from 64% to 5%. Consequently immunotoxin purification yield was increased from 53.0% to 73.8%. Simultaneously this methodology enhanced immunotoxin secretion to 120 mgl(-1) at 163 h of methanol induction in a toxin resistant production strain. We conclude that minimizing shearing force and reducing the air/liquid interfacial foam area are crucial factors in reducing hydrophobic protein aggregation upon secretory expression in yeast bioreactor cultures.