Continuous cell suspension processing using magnetically stabilized fluidized beds

The behavior of a cell suspension in a continuous magnetically stabilized fluidized bed (MSFB) was investigated both experimentally and theoretically. The low, constant pressure drop and fluidity of the solids phase in the MSFB allowed a continuous countercurrent separator to be constructed. The magnetic field eliminated all motion of the solids phase (nickel spheres) and produced a device similar to a packed-bed depth filter. Yeast cells were used as the suspended solids and the performance of the MSFB filter was assessed as a function of the bed height, solids velocity, cell concentration, and liquid composition. Removal rates could be adjusted by controlling the cell/support interaction and were found to be as high as 99%. A mathematical model was used to aid in understanding this filtration and was found to agree qualitatively with all experimental observations. Comparison of the model with the data suggests that both cell/cell binding and cell shadowing are occurring.     

Application of magnetic agarose support in liquid magnetically stabilized fluidized bed for protein adsorption

A novel magnetic agarose support (MAS) was fabricated for application in a liquid magnetically stabilized fluidized bed (MSFB). It was produced by water-in-oil emulsification method using a mixture of agarose solution and nanometer-sized superparamagnetic Fe(3)O(4) particles as the aqueous phase. The MAS showed good superparamagnetic responsiveness in a magnetic field. A reactive triazine dye, Cibacron blue 3GA (CB), was coupled to the gel to prepare a CB-modified magnetic agarose support (CB-MAS) for protein adsorption. Lysozyme was used as a model protein to test the adsorption equilibrium and kinetic behavior of the CB-MAS. The dependence of bed expansion in the MSFB with a transverse magnetic field on liquid velocity and magnetic field intensity was investigated. Liquid-phase dispersion behavior in the MSFB was examined by measurements of residence time distributions and compared with that obtained in packed and expanded beds. Dynamic lysozyme adsorption in the MSFB was also compared with those in packed and expanded beds. The dynamic binding capacity at 10% breakthrough was estimated at 55.8 mg/mL in the MSFB, higher than that in the expanded bed (31.1 mg/mL) at a liquid velocity of 45 cm/h. The results indicate that the CB-MAS is promising for use in liquid MSFB for protein adsorption.     

Cell clarification and size separation using continuous countercurrent magnetophoresis

Nonmagnetic microparticles (e.g., cells, polymer beads) immersed in a magnetic fluid (ferrofluid) under a nonuniform magnetic field experience a magnetophoretic force in the direction of decreasing magnetic field strength. This phenomenon was exploited in the development of a continuous magnetophoretic countercurrent separation for the removal and concentration of micron-sized particles from aqueous suspensions, and in particular as a viable approach for cell clarification of raw fermentation broth. A magnetic fluid is added to the cell suspension, the mixture is introduced to the magnetic separator, which consists of an open flow tube passing between pairs of magnets that move in a direction counter to the flow of the suspension. The cells are pushed ahead of the magnet pairs owing to the magnetophoretic forces acting on them, collected in a tube upstream of the feed injection point, and removed as a concentrated suspension for further treatment.     

Preparation of magnetically susceptible polyacrylamide/magnetite beads for use in magnetically stabilized fluidized bed chromatography

Spherical polyacrylamide/magnetite (PAM) composite beads, suitable for use in a magnetically stabilized fluidized bed (MSFB), were manufactured by a suspension polymerization method. Yield of beads depended on the type and concentration of buffer used during polymerization as well as the pH. More stabilizer was needed to prevent bead agglomeration as magnetite concentration increased. Bead diameter ranged from less than 60 to 600 mum, depending on reaction conditions, and the bead mean diameter and size distribution decreased with increasing impeller speed. The density and roundness factor of the beads were 1.19 +/- 0.02 g cm(-3) and 1.08 +/- 0.03, respectively. The beads had high magnetization at a low applied magnetic field strength (60 mT at 75 kA m(-1)) and retained little residual magnetization (<2 mT) after the field was removed. Incorporation of magnetite did not significantly affect the physical strength of the beads: the beads' average elastic modulus was 14 +/- 4 kPa, similar to reported values for polyacrylamide gels (15.8 kPa). The beads were stable in a range of buffers from pH 1 to 10 and were resistant to microbial degradation. The fluidization and stabilization behavior of the beads was examined in a bench-scale MSFB. The minimum fluidization velocity (U(mf)) of the beads (0.035 mm s(-1)) allowed the MSFB to be operated at superficial velocities close to those used in HPLC systems. Against expectations, at high superficial velocities, the stabilized bed of the MSFB had a greater expansion than the unstabilized bed. The PAM beads could be derivatized and activated for soybean trypsin inhibitor immobilization by a standard carbodiimide method, and the affinity separation of trypsin from chymotrypsin was demonstrated. The PAM beads show excellent potential for use in MSFB chromatography. (c) 1997 John Wiley & Sons, Inc.     

A study of the influence of yeast cell debris on protein and alpha-glucosidase adsorption at various zones within the expanded bed using in-bed sampling

Expanded bed adsorption chromatography is used to capture products directly from unclarified feedstocks, thus combining solid-liquid separation, product concentration and preliminary purification into a single step. However, when non-specific ion-exchangers are used as the adsorbent in the expanded bed, there is the possibility that electrostatic interactions of cells or cell debris with the adsorbent may interfere with the adsorption of soluble products. These interactions depend on the particle size of the cell debris and its surface charge, which in turn depend on the extent of disruption used to release the intracellular products. The interactions occurring during expanded bed adsorption between the anionic ion-exchanger STREAMLINE DEAE and particulate yeast homogenates obtained by high pressure homogenisation at different intensities of disruption achieved by operating at different pressures were studied, while maintaining all other parameters constant. In-bed sampling from the expanded bed using ports fitted up the height of expanded bed was used to study the retention of yeast cells and cell debris within the bed and its influence on the adsorption of total soluble protein and alpha-glucosidase within various zones of the expanded bed. The retention of the biomass present in the homogenate obtained at a lower intensity of disruption was found to be high at the lower end of the column (17% from 13.8 MPa sample compared to 1% from 41.4 MPa sample). This interaction of the particulate material with the adsorbent was found to reduce the dynamic binding capacity of the adsorbent for total soluble protein from 3.6 mg/mL adsorbent for 41.4 MPa sample to 3.0 mg/mL adsorbent for 13.8 MPa sample. The adsorption of alpha-glucosidase was found to increase with an increase in the concentration of the enzyme in the feed, which increased with the intensity of disruption. Selective adsorption of 6,732 U alpha-glucosidase per mg of total protein bound, was noticed for the feedstock prepared at a higher disruption intensity at 41.4 MPa compared to adsorption of 1,262 U/mg of total protein bound for that prepared at 13.8 MPa. The selective adsorption of alpha-glucosidase due to its high concentration together with simultaneous high specific activity of the enzyme in the feed indicated the significance of selective release of enzymes during microbial cell disruption for efficient expanded bed adsorption processes.     

Continuous protein separations in a magnetically stabilized fluidized bed using nonmagnetic supports

Continuous protein separations were performed using a magnetically stabilized fluidized bed (MSFB) and a commercially available affinity adsorption resin that contained no magnetically susceptible material. These nonmagnetic materials can be stabilized at relatively low fields (<75 G requiring <30 W) if sufficient magnetically susceptible particles are also present in the stabilized bed. The minimum amount of magnetic particles necessary to stabilize the bed is as low as 20% by volume and is a function of various parameters including the size and density of both particles, the magnetic field strength, and the fluidization velocity. Advantages of these beds for performing separations include true continuous, countercurrent liquid-solids contact, mass-transfer efficiencies nearly equal to that of packed beds, and the ability of handle suspended cells or cell debris. A variety of commercially available affinity, ion-exchange, and adsorptive supports can be used in the bed for continuous separations; results are presented for the adsorption and recovery of lysozyme from an aqueous mixture of lysozyme and myoglobin using an affinity resin.     

Continuous removal of malathion by immobilised biomass of Bacillus species S14 using a packed bed column reactor

Abstract

Biosorption of malathion from aqueous solution was studied using Bacillus sp. S₁₄ immobilised on calcium alginate (3%) using a packed bed column reactor at a temperature of 25 °C and a pH of 7.0. The experiments were conducted to study the effect of important design parameters such as bed height, flow rate and influent malathion concentration. Maximum removal capacity (57%) was found at 4 mL min^-1 flow rate, 6.0 cm bed height and 25 mg L^-1 influent malathion concentration. The Adam-Bohart model, Wolborska model, Thomas model, Yoon-Nelson model were employed to determine characteristic parameters such as saturation concentration, external mass transfer coefficient, Thomas rate constant, the maximum solid phase concentration of the solute, rate constant, and the time required for 50% adsorbate breakthrough time, which are all useful for process design. Experimental data were well fitted with Adam–Bohart model at the lower region of effluent/influent malathion concentration values but at higher region values data fitted well with the Thomas and Yoon-Nelson models.     

Using a two species competitive binding model to predict expanded bed breakthrough of a recombinant protein expressed in a high cell density fermentation

Expanded Bed experiments were conducted using a mixed mode (MM) resin to capture and purify a recombinant protein produced in yeast fermentation. Expanded bed breakthrough profiles show an overshoot in column effluent concentration of the target protein in the presence of cells and other broth proteins, similar to that seen by other researchers when loading two competing species onto packed beds. In this research, a numerical model assuming negligible axial dispersion is developed and first validated for columns loads that contain only the target protein. This model is solved by finite differences in a unique way that uses an embedded analytical-solution to increase solution speed and stability. To model expanded bed breakthrough of the target protein in the actual cell broth, it was assumed that the other non-product proteins in the broth compete for MM resin binding sites and might be represented as a second “average” species via a traditional two-component competitive Langmuir isotherm. Estimates of the Langmuir constant and broth concentration of this second species were then calculated from batch adsorption data. Using these parameters for the second species, and other batch-derived parameters for the target protein with this resin, this unique numerical modeling approach provided results that compare favorably to experimental breakthrough data at various flow rates. Finally, the model was employed for a parameter sensitivity analysis that shows which process variables are most important in determining breakthrough time and the shape and magnitude of the concentration overshoot.     

Sorption of heavy metals from electroplating effluent using immobilized biomass Trichoderma viride in a continuous packed-bed column

The sorption of heavy metals ions by immobilized Trichoderma viride biomass in a packed-bed column was studied. Fungal biomass T. viride was immobilized to Ca-alginate used for removal of Cr(VI), Ni(II) and Zn(II) ions from synthetic solutions and electroplating effluent. The experiments were conducted to study the effect of important design parameters such as bed height, flow rate and initial concentration of metal ions. The maximum sorption capacity was observed at flow rate 5 ml/min, bed height 20 cm and metal ions concentration 50 mg/L with immobilized biomass. Whereas, breakthrough time and saturation time decreased with increase flow rate and metal ions concentration and an inverse condition was found in bed height. The bed depth service time (BDST) Adams-Bohart model was used to analyze the experimental data. The regeneration efficiency was observed 40.1%, 75% and 53% for Cr(VI), Ni(II) and Zn(II) without any significant alteration in sorption capacity after 5th sorption-desorption cycles.     

Removal of heavy metals using a brewer's yeast strain of Saccharomyces cerevisiae: the flocculation as a separation process

In this work, a brewer's yeast strain was used to remove heavy metals from a synthetic effluent. The solid-liquid separation process was carried out using the flocculation ability of the strain. The yeast strain was able to sediment in the presence of Cu2+, Ni2+, Zn2+, Cd2+ and Cr3+, which evidences that the flocculation can be used as a cheap and natural separation process for an enlarged range of industrial effluents. For a biomass concentration higher than 0.5 g/l, more than 95% of the cells were settled after 5 min; this fact shows that the auto-aggregation of yeast biomass is a rapid and efficient separation process. Cells inactivated at 45 degrees C maintain the sedimentation characteristics, while cells inactivated at 80 degrees C lose partially (40%) the flocculation. The passage of metal-loaded effluent through a series of sequential batches allowed, after the second batch, the reduction of the Ni2+ concentration in solution for values below the legal limit of discharge of wastewater in natural waters (2mg/l); this procedure corresponds to a removal of 91%. A subsequent batch had a marginal effect on Ni2+ removal (96%). Together, the results obtained suggest that the use of brewing flocculent biomass looks a promising alternative in the bioremediation of metal-loaded industrial effluents since the removal of the heavy metals and cell separation are simultaneously achieved.     

Bench-scale and packed bed sorption of methylene blue using treated olive pomace and charcoal

A combination of olive pomace after solvent extraction and charcoal produced from the solid waste of olive oil press industry was used as an adsorbent for the removal of methylene blue (MB) dye from aqueous solutions. Batch tests showed that up to 80% of dye was removed when the dye concentration was 10 mg/ml and the sorbent concentration was 45 mg/ml. An increase in the olive pomace concentration resulted in greater dye removal from aqueous solution, and an increase in MB dye concentration at constant adsorbent concentration increased the dye loading per unit weigh of adsorbent. In the kinetic of the adsorbent process, the adsorption data followed the second-order kinetic model better than first order kinetic model. Charcoal showed higher sorption capacity (uptake) than that of olive pomace. In the fixed bed adsorption experiment, the breakthrough curves showed constant pattern behavior, typical of favorable isotherms. The breakthrough time increased with increasing bed height, decreasing flow rate and decreasing influent concentration and methylene blue dye uptake. The uptake of MB dye was significantly increased when a mixture of olive pomace and charcoal was packed in the column in a multi-layer fashion. Different models were used to describe the behavior of this packed-sorption process.     

Expanded bed adsorption of human serum albumin from very dense Saccharomyces cerevesiae suspensions on fluoride-modified zirconia.

The adsorption of proteins from high cell density yeast suspensions on mixed-mode fluoride-modified zirconia (FmZr) particles (38 to 75 microm, surface area of 29 m(2)/g and density of 2.8 g/cm(3)) was investigated using human serum albumin (HSA) added to Saccharomyces cerevesiae as the model expression host. Because of the high density of the porous zirconia particles, HSA (4 mg/mL) can be adsorbed from a 100 g dry cell weight (DCW)/L yeast suspension in a threefold-expanded bed of FmZr. The expanded bed adsorption of any protein from a suspension containing >50 g DCW/L cells has not been previously reported. The FmZr bed expansion characteristics were well represented by the Richardson-Zaki correlation with a particle terminal velocity of 3.1 mm/s and a bed expansion index of 5.4. Expanded bed hydrodynamics were investigated as a function of bed expansion using residence time distribution studies with sodium nitrite as the tracer. The adsorption of HSA on FmZr exhibited features of multicomponent adsorption due to the presence of dimers. The protein binding capacity at 5% breakthrough decreased from 22 mg HSA/mL settled bed void volume for 20 g DCW/L yeast to 15 mg HSA/mL settled bed void volume for 40 g DCW/L yeast and remained unchanged for the higher yeast concentrations (60 to 100 g DCW/L). However, the batch (or equilibrium) binding capacity decreased monotonically as a function of yeast concentration (20 to 100 g DCW/L) and the binding capacity at 100 g DCW/L yeast was fivefold lower compared with that at 20 g DCW/L yeast. The lower batch binding capacity at high cell concentrations resulted from the adsorption of cells at the surface of the particles restricting access of HSA to the intraparticle surface area. Batch (or equilibrium) and column HSA adsorption results indicated that the adsorption of HSA on FmZr occurred at a time scale that may be much faster than that of yeast cells. The zirconia particles were cleaned of adsorbed HSA and yeast with a total of 1500 to 2000 column volumes (over many cycles) of 0. 25 M NaOH, without any significant effect on the chromatographic performance.     

Fixed-Bed Studies on Removal of Arsenic from Simulated Aqueous Solutions Using Chitosan Nanoparticles

Arsenic is a toxic element and may be found in natural as well as in industrial water; therefore, before using water for drinking purpose, its proper treatment is required. Thus, the aim of this work was to evaluate the potential of chitosan nanoparticles, in a continuous-flow method, for the removal of arsenic (III) and (V) from aqueous solutions. All experiments were conducted in fixed-bed columns. Experiments were carried out as a function of varying liquid flow rate (0.3–1.0 ml/min), initial metal concentration (0.5–1.5 mg/L), and bed height (3–9 cm) of adsorbent. The total adsorbed quantity, equilibrium uptake, and total percentage removal of arsenic ions were determined by evaluating the breakthrough curves obtained at different flow rates, initial concentrations, and bed heights. The results showed that the column performed well at the lowest flow rate. Also, column bed capacity and exhaustion time were found to increase with increasing bed height. When initial metal ion concentration was increased from 0.5 to 1.5 mg/L, the corresponding adsorption bed capacity decreased from 0.076 to 0.028 mg/g. The bed depth service time model (BDST) model was used to analyze the experimental data and the model parameters were evaluated. The calculated values of N _o and K _a were found to be 19.28 × 10^?2 mg/L and 0.662 L/mg·min, respectively. Good agreement was found between the experimental breakthrough curves and the model predictions.     

Plant cell culture using a novel bioreactor: the magnetically stabilized fluidized bed.

A novel bioreactor using magnetically stabilized fluidized bed (MSFB) technology has been developed that has certain advantages for cultivating cells continuously. In this system, the cells are protected from shear and are constrained to move through the fermenter in lock-step fashion by being immobilized in calcium alginate beads. The MSFB permits good mass transfer, minimizes particle collisions, and allows for the production of cells while maintaining a controlled cell residence time. Details of the experimental system are described. In addition, the experimental performance of an MSFB used to grow plant cells in batch mode is compared to the results obtained in shake flask culture.     

Retention and viability characteristics of mammalian cells in an acoustically driven polymer mesh

A processing approach for the collection and retention of mammalian cells within a high porosity polyester mesh having millimeter-sized pores has been studied. Cell retention occurs via energizing the mesh with a low intensity, resonant acoustic field. The resulting acoustic field induces the interaction of cells with elements of the mesh or with each other and effectively prevents the entrainment of cells in the effluent stream. Experiments involving aqueous suspensions of polystyrene particles were used to provide benchmark data on the performance of the acoustic retention cell. Experiments using mouse hybridoma cells showed that retention densities of over 1.5 x 10(8) cell/mL could be obtained. In addition, the acoustic field was shown to produce a negligible effect on cell viability for short-term exposure.     

Fractionation of cell mixtures using acoustic and laminar flow fields

A fractionation method applicable to different populations of cells in a suspension is reported. The separation was accomplished by subjecting the suspension to a resonant ultrasonic field and a laminar flow field propagating in orthogonal directions within a thin, rectangular chamber. Steady, laminar flow transports the cell suspension along the chamber, while the ultrasonic field causes the suspended cells to migrate to the mid-plane of the chamber at rates related to their size and physical properties. A thin flow splitter positioned near the outlet divides the effluent cell suspension into two product streams, thereby allowing cells that respond faster to the acoustic field to be separated from those cells that respond more slowly. Modeling of the trajectories of individual cells through the chamber shows that by altering the strength of the flow relative to that of the acoustic field, the desired fractionation can be controlled. Proof-of-concept experiments were performed using hybridoma cells and Lactobacillus rhamnosus cells. The two populations of cells could be effectively separated using this technique, resulting in hybridoma/Lactobacillus ratios in the left and right product streams, normalized to the feed ratio, of 6.9 +/- 1.8 and 0.39 +/- 0.01 (vol/vol), respectively. The acoustic method is fast, efficient, and could be operated continuously with a high degree of selectivity and yield and with low power consumption. (c) 2004 Wiley Periodicals, Inc.     

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.     

Continuous flow magnetic cell fractionation based on antigen expression level

Cell separation is important in medical and biological research and plays an increasingly important role in clinical therapy and diagnostics, such as rare cancer cell detection in blood. The immunomagnetic labeling of cells with antibodies conjugated to magnetic nanospheres gives rise to a proportional relationship between the number of magnetic nanospheres attached to the cell and the cell surface marker number. This enables the potential fractionation of cell populations by magnetophoretic mobility (MM). We exploit this feature with our apparatus, the Dipole Magnet Flow Fractionator (DMFF), which consists of an isodynamic magnetic field, an orthogonally-oriented thin ribbon of cell suspension in continuous sheath flow, and ten outlet flows. From a sample containing a 1:1 mixture of immunomagnetically labeled (label+) and unlabeled (label-) cells, we achieved an increase in enrichment of the label+ cell fraction with increasing outlet numbers in the direction of the magnetic field gradient (up to 10-fold). The total recovery of the ten outlet fractions was 90.0+/-7.7%. The mean MM of label+ cells increased with increasing outlet number by up to a factor of 2.3. The postulated proportionality between the number of attached magnetic beads and the number of cell surface markers was validated by comparison of MM measured by cell tracking velocimetry (CTV) with cell florescence intensity measured by flow cytometry.     

A breakthrough column study for removal of malachite green using coco-peat

Abstract

A continuous adsorption study in a fixed bed column using coco-peat (CP) as an adsorbent was carried out for the removal of toxic malachite green (MG) from contaminated water. Fixed bed column studies were carried out to check field application viability. Various parameters like particle size, pH, concentration, dose and interference were exercised to optimize dye removal. Data obtained from breakthrough column studies were evaluated using Thomas and BDST model. Thomas rate constants K_t (0.22?ml min^?1 mg^?1) and adsorption capacity q_o (181.04?mg g^?1) were estimated and found to favor efficiency of CP. Thomas model was tested with several parameters like flow rate, concentration, and bed depth. Upon increase in input dye concentration, flow rate and bed height, adsorption coefficients increased. According to BDST model, maximum dye uptake of 468.26?mg/l was obtained with an input dye concentration of 5?mg/l. HYBRID and MPSD error functions were tested and found that Thomas model fits best. Dilute hydrochloric acid was found best for desorption. Real wastewater from textile industry was analyzed and confirmed the prospect of large-scale industrial application. In conclusion, coco-peat can be used as a promising bio-sorbent in column bed for scavenging of MG from contaminated water.