Synthesis and evaluation of polymeric continuous bed (monolithic) reversed-phase gradient stationary phases for capillary liquid chromatography and capillary electrochromatography

There is a demand of novel high resolution separation media for separation of complex mixtures, particularly biological samples. One of the most flexible techniques for development of new separation media currently is synthesis of the continuous bed (monolithic) stationary phases. In this study the capillary format gradient stationary phases were formed using continuous bed (monolith) polymerization in situ. Different reversed-phase stationary phase gradients were tailored and their resolution using capillary liquid chromatography and capillary electrochromatography at isocratic mobile phase conditions was evaluated. It is demonstrated, that efficiency and resolution of the gradient stationary phases can be substantially increased comparing to the common (isotropic) stationary phases. The proposed formation approach of the gradient stationary phase is reproducible and compatible with the capillary format or microchip format separations. It can be easily automated for the separation optimizations or mass production of the capillary columns or chips.     

Synthesis and evaluation of polymeric continuous bed (monolithic) reversed-phase gradient stationary phases for capillary liquid chromatography and capillary electrochromatography

There is a demand of novel high resolution separation media for separation of complex mixtures, particularly biological samples. One of the most flexible techniques for development of new separation media currently is synthesis of the continuous bed (monolithic) stationary phases. In this study the capillary format gradient stationary phases were formed using continuous bed (monolith) polymerization in situ. Different reversed-phase stationary phase gradients were tailored and their resolution using capillary liquid chromatography and capillary electrochromatography at isocratic mobile phase conditions was evaluated. It is demonstrated, that efficiency and resolution of the gradient stationary phases can be substantially increased comparing to the common (isotropic) stationary phases. The proposed formation approach of the gradient stationary phase is reproducible and compatible with the capillary format or microchip format separations. It can be easily automated for the separation optimizations or mass production of the capillary columns or chips.     

Chromatography of human prothrombin from Nitschmann fraction III on Q Sepharose Fast Flow using axial and radial flow column

An axial column (Hitrap Q 5 ml, 2.5 2 1.6 cm) and a radial flow column (3.5 2 5 cm) packed with Q Sepharose Fast Flow media had been evaluated for the separation of human prothrombin. Nitschmann fraction III dissolved in buffered saline (0.10 M sodium chloride buffered with 0.06 M Tris/HCl to pH 7.5) was the starting material. Effects of sample flow rate of the two columns were screened. Under radial flow conditions using the radial column, sample flow rate up to 15 ml/min (i.e. 18 bed volumes/h) was achieved and the operating pressure was below 0.2 MPa eventhough the elution velocity was 30 ml/min. Breakthrough capacity was determined by analyzing the total protein and prothrombin activity of the target protein-containing fraction under subsaturating conditions and both columns had almost the same breakthrough capacity per ml media, indicating that the sample loading was independent of radial column geometry. It was concluded that the radial column is an attractive alternate to traditional axial packed bed column, exhibiting very good potential for use in the separation of human prothrombin.     

Fibrous stationary phase in capillary electrochromatography

Capillary electrochromatography (CEC) using fibrous cellulose acetate (CA) stationary phase was investigated. The advantage of this fiber-packed column is relatively easy preparation process compared with other conventional CEC columns, such as particle-packed and wall-coated capillaries. CA fibers are manually packed into a capillary with two guide liners and fixed with a frit at the column inlet. The separation characteristics of this column were investigated using n-alkyl p-hydroxybenzoates (parabens) as the sample probe. It has been demonstrated that the use of a short column length and a specially designed tee-connector as the injection device should make the separation performance and efficiency much higher on the fiber-packed columns. Sufficient separation between methyl and n-butylparabens is obtained on the 5-cm-packed column and linear relationships between the injection time and the peak area are observed. Bubble formation is not encountered during the analysis.     

Modified CelliGen-packed bed bioreactors for hybridoma cell cultures

This study describes two packed bed bioreactor configurations which were used to culture a mouse-mouse hybridoma cell line (ATCC HB-57) which produces an IgG₁ monoclonal antibody. The first configuration consists of a packed column which is continuously perfused by recirculating oxygenated media through the column. In the second configuration, the packed bed is contained within a stationary basket which is suspended in the vessel of a CelliGen^™ bioreactor. In this configuration, recirculation of the oxygenated media is provided by the CelliGen Cell Lift impeller. Both configurations are packed with disk carriers made from a non-woven polyester fabric. During the steady-state phase of continuous operation, a cell density of 10⁸ cells per cm³ of bed volume was obtained in both bioreactor configurations. The high levels of productivity (0.5 gram MAb per 1 of packed bed per day) obtained in these systems demonstrates that the culture conditions achieved in these packed bed bioreactors are excellent for the continuous propagation of hybridomas using media which contains low levels (1 %) of serum as well as serum-free media. These packed bed bioreactors allow good control of pH, dissolved oxygen and temperature. The media flows evenly over the cells and produces very low shear forces. These systems are easy to set up and operate for prolonged periods of time. The potential for scale-up using Fibra-cel carriers is enhanced due to the low pressure drop and low mass transfer resistance, which creates high void fraction approaching 90% in the packed bed.     

Separation of plasmid DNA from protein and bacterial lipopolysaccharides using displacement chromatography

The preparation of plasmid DNA at large scale constitutes a pressing problem in bioseparation. This paper describes a first investigation of displacement chromatography as a means to separate plasmid DNA (4.7 kb) from E. coli lipopolysaccharides and protein (holo transferrin), respectively. Displacement chromatography has advantages in this regard, since the substance mixture is resolved into rectangular zones of the individual components rather than into peaks. Thus a higher total concentration can be maintained in the pooled product fractions. Hydroxyapatite (type I and II) and anion exchange stationary phases were included in the experiments. In addition to a conventional anion exchange column packed with porous particles, the recently introduced continuous bed UNOTM anion exchange column was investigated. No DNA purification was possible with either hydroxyapatite material. Conventional particle based columns in general were not suited to the separation of any two substances varying considerably in molecular mass, e.g. plasmid DNA and standard protein. Presumably, the direct competition for the binding sites, which is essential in displacement chromatography, was restricted by the size dependency of the accessible stationary phase surface area in this case. Better results were obtained with the continuous bed column, in which the adsorptive surface coincides with the walls of the flow through pores. As a result the accessible surface does not vary as much with the size of the interacting molecules as for the conventional stationary phase materials. Sharper transitions were also observed between substance zones recovered from the UNOTM column. The steric mass action model was used to aid method development in case of the anion exchange approach. While further research in obviously necessary, displacement chromatography on continuous bed columns has been shown to be capable of separating plasmid DNA from typical impurities. This revised version was published online in July 2006 with corrections to the Cover Date.     

Gas concentration and temperature gradients in a packed bed solid-state fermentor

In solid-state fermentation (SSF), interaction of heat and mass transfer with biochemical reaction (growth associated enzyme production) affects the bioreactor performance. This interaction was earlier observed to cause temperature and gaseous concentration gradients which reduced the effective bed height of the bioreactor. Since forced aeration is known to alleviate this problem, a packed column bioreactor with forced aeration was employed in the present study. Using wheat bran and Aspergillus niger CFTRI 1105, experiments were conducted for the production of the enzyme amyloglucosidase at various air flow rates. Temperatures and gas concentrations were recorded and enzyme activities estimated at different bed heights during the course of SSF. Gas concentration and temperature gradients decreased with increasing air flow rate. The packed column allowed the use of larger bed heights and yielded higher enzyme activities (6,260 Units/gDMB) than trays (345 Units/gDMB). Enzyme activity was affected more by temperature than concentration gradients, and increased with air flow rates.     

Mathematical Modeling of Size Exclusion Chromatography

A mathematical model of the size exclusion chromatography (SEC) process in chromatographic columns has been developed. It considers the following three mass transfer processes in the SEC column: axial dispersion in the bulk‐fluid phase, interfacial film mass‐transfer between the stationary and mobile phases, and diffusion of solutes within the macro pores of the packing particles. Differential equations of the process model were solved by the finite difference method. Characteristics of the column and the packing particles (bed void volume fraction, particle porosity, accessible particle porosity) were obtained experimentally, as well as retention times of different molecules with known molecular weights. Experiments were performed with two different columns containing two different packing materials, Superdex 75 HR 10/30 and BioSep SEC S2000, respectively. The model has been validated by comparing theoretical and experimental retention times for the different columns.     

Monitoring of temperature effects on animal cell metabolism in a packed bed process

Animal cell (Chinese Hamster Ovary) concentration was determined on-line in a packed bed process using dielectric spectroscopy. This enabled the evaluation of the effect of temperature on specific metabolic rates during 3 months of continuous culture. The effect of low cultivation temperature on cell growth and metabolism was monitored, and the data were used for process development. At 37 degrees C cells grew exponentially with a specific growth rate of 0.038 d-1 and specific glucose uptake and lactate production rates increased continually. Reduction of the temperature to 33.5 degrees C resulted in a lowering of these metabolic rates while having no effect on cell proliferation. Subsequent reduction of the temperature to 32 degrees C resulted in stabilization of the cell concentration at a high density (3.6 x 10(7) cell per mL of packed bed). In addition, the specific production rate of the protein of interest increased by a factor of 6 compared to the value at 37 degrees C. During the stationary phase at 32 degrees C, all other specific metabolic rates could be controlled to low and constant levels.     

Modeling of scale-down effects on the hydrodynamics of expanded bed adsorption columns

Expanded-bed adsorption (EBA) is a technique for primary recovery of proteins starting from unclarified broths. This process combines centrifugation, concentration, filtration, and initial capturing of the proteins in a single step. An expanded bed (EB) is comparable to a packed bed in terms of separation performance but its hydrodynamics are that of a fluidized bed. Downstream process development involving EBA is normally carried out in small columns to minimize time and costs. Our purpose here is to characterize the hydrodynamics of expanded beds of different diameters, to develop scaling parameters that can be reliably used to predict separation efficiency of larger EBA columns. A hydrodynamic model has been developed which takes into account the radial liquid velocity profile in the column. The scale-down effect can be characterized in terms of apparent axial dispersion, D(axl,app), and plate number, N(EB), adapted for expanded bed. The model is in good agreement with experimental results obtained from 1- and 5-cm column diameters with buffer solutions of different viscosities. The model and the experiments show an increase of apparent axial dispersion with an increase in column diameter. Furthermore, the apparent axial dispersion is affected by an increase in liquid velocity and viscosity. Supported by visual observations and predictions from the model, it was concluded that operating conditions (liquid viscosity and superficial velocity) resulting in a bed-void fraction between 0.7 and 0.75 would provide the optimal separation efficiency in terms of N(EB).     

The influence of process parameters in production of lipopeptide iturin A using aerated packed bed bioreactors in solid-state fermentation

The strain Bacillus iso 1 co-produces the lipopeptide iturin A and biopolymer poly-γ-glutamic acid (γ-PGA) in solid-state fermentation of substrate consisting of soybean meal, wheat bran with rice husks as an inert support. The effects of pressure drop, oxygen consumption, medium permeability and temperature profile were studied in an aerated packed bed bioreactor to produce iturin A, diameter of which was 50 mm and bed height 300 mm. The highest concentrations of iturin A and γ-PGA were 5.58 and 3.58 g/kg-dry substrate, respectively, at 0.4 L/min after 96 h of fermentation. The low oxygen uptake rates, being 23.34 and 22.56 mg O₂/kg-dry solid substrate for each air flow rate tested generated 5.75 W/kg-dry substrate that increased the fermentation temperature at 3.7 °C. The highest pressure drop was 561 Pa/m at 0.8 L/min in 24 h. This is the highest concentration of iturin A produced to date in an aerated packed bed bioreactor in solid-state fermentation. The results can be useful to design strategies to scale-up process of iturin A in aerated packed bed bioreactors. Low concentration of γ-PGA affected seriously pressure drop, decreasing the viability of the process due to generation of huge pressure gradients with volumetric air flow rates. Also, the low oxygenation favored the iturin A production due to the reduction of free void by γ-PGA production, and finally, the low oxygen consumption generated low metabolic heat. The results show that it must control the pressure gradients to scale-up the process of iturin A production.     

Purification of histidine-tagged nucleocapsid protein of Nipah virus using immobilized metal affinity chromatography

Nucleocapsid (N) protein of Nipah virus (NiV) is a potential serological marker used in the diagnosis of NiV infections. In this study, a rapid and efficient purification system, HisTrap? 6 Fast Flow packed bed column was applied to purify recombinant histidine-tagged N protein of NiV from clarified feedstock. The optimizations of binding and elution conditions of N protein of NiV onto and from Nickel Sepharose? 6 Fast Flow were investigated. The optimal binding was achieved at pH 7.5, superficial velocity of 1.25 cm/min. The bound N protein was successfully recovered by a stepwise elution with different concentration of imidazole (50, 150, 300 and 500 mM). The N protein of NiV was captured and eluted from an inlet N protein concentration of 0.4 mg/ml in a scale-up immobilized metal affinity chromatography (IMAC) packed bed column of Nickel Sepharose? 6 Fast Flow with the optimized condition obtained from the method scouting. The purification of histidine-tagged N protein using IMAC packed bed column has resulted a 68.3% yield and a purification factor of 7.94.     

Modeling of immobilized cell columns for bioconversion and wastewater treatment

Immobilized cells are widely used in bioconversions to produce biological products as well as in wastewater treatment such as solvent removal from wastewater streams. In this work, a rate model is proposed to simulate this kind of process in an axial-flow fixed-bed column packed with porous particles containing immobilized cells. The transient model considered various mass transfer mechanisms including axial dispersion, interfacial film mass transfer, and intraparticle diffusion. Cell death in the immobilized cell system was also considered. Effects of various parameters such as kinetic constants and mass transfer parameters were studied. Operational situations such as feed fluctuation flow rate increase and two columns in series were also investigated. The model can be used to study the behavior and characteristics of immobilized cell columns in order to perform scale-up predictions of effluent profiles and for the purpose of process optimization.     

Factors affecting dispersion in expanded bed chromatography

Factors affecting the dispersion of solutes in expanded bed chromatography were experimentally investigated to characterize the behavior in small columns. Pulse response curves were measured with a vitamin B¹² tracer, and HETP (height equivalent to a theoretical plate) values were calculated from peak variance and retention time. Approximately 15 min were required to attain a stable steady state expanded bed height with constant HETP values. HETP values ranged from 0.8 to 1.6 cm and did not change appreciably with the degree of expansion (1.5–3.5 fold), column diameter (1.6 and 2.6 cm), column temperature (293–308 K) or settled bed height (ca. 4–11 cm). A very small column (1.6 cm diam. and 4.2 cm-settled bed height) was successfully expanded and axial mixing measured could be useful for conducting scale down experiments.     

Pressure-flow relationships for packed beds of compressible chromatography media at laboratory and production scale

Pressure drop across chromatography beds employing soft or semirigid media can be a significant problem in the operation of large-scale preparative chromatography columns. The shape or aspect ratio (length/diameter) of a packed bed has a significant effect on column pressure drop due to wall effects, which can result in unexpectedly high pressures in manufacturing. Two types of agarose-based media were packed in chromatography columns at various column aspect ratios, during which pressure drop, bed height, and flow rate were carefully monitored. Compression of the packed beds with increasing flow velocities was observed. An empirical model was developed to correlate pressure drop with the aspect ratio of the packed beds and the superficial velocity. Modeling employed the Blake-Kozeny equation in which empirical relationships were used to predict bed porosity as a function of aspect ratio and flow velocity. Model predictions were in good agreement with observed pressure drops of industrial scale chromatography columns. A protocol was developed to predict compression in industrial chromatography applications by a few laboratory experiments. The protocol is shown to be useful in the development of chromatographic methods and sizing of preparative columns.     

Preparation and characterization of a new open‐tubular capillary column for enantioseparation by capillary electrochromatography

In order to use the enantioseparation capability of cationic cyclodextrin and to combine the advantages of capillary electrochromatography (CEC) with open‐tubular (OT) column, in this study, a new OT‐CEC, coated with cationic cyclodextrin (1‐allylimidazolium‐β‐cyclodextrin [AI‐β‐CD]) as chiral stationary phase (CSP), was prepared and applied for enantioseparation. Synthesized AI‐β‐CD was characterized by infrared (IR) spectrometry and mass spectrometry (MS). The preparation conditions for the AI‐β‐CD‐coated column were optimized with the orthogonal experiment design L₉(3⁴). The column prepared was characterized by scanning electron microscopy (SEM) and elemental analysis (EA). The results showed that the thickness of stationary phase in the inner surface of the AI‐β‐CD‐coated columns was about 0.2 to 0.5 μm. The AI‐β‐CD content in stationary phase based on the EA was approximately 2.77 mmol·m^?2. The AI‐β‐CD‐coated columns could separate all 14 chiral compounds (histidine, lysine, arginine, glutamate, aspartic acid, cysteine, serine, valine, isoleucine, phenylalanine, salbutamol, atenolol, ibuprofen, and napropamide) successfully in the study and exhibit excellent reproducibility and stability. We propose that the column, coated with AI‐β‐CD, has a great potential for enantioseparation in OT‐CEC.     

The effect of column verticality on separation efficiency in expanded bed adsorption

The effect of column verticality on liquid dispersion and separation efficiency in expanded bed adsorption columns was investigated using 1 and 5 cm diameter columns. Column misalignment of only 0.15° resulted in the reduction of the Bodenstein number from 140 to 50 for the 1 cm dia. column and from 75 to 45 for the 5 cm dia. column. This degree of misalignment was not detectable by visual assessment of adsorbent particle movement within the column. Depending on the relative importance of transport limitations, kinetic limitations and dispersion to any specific separation, this increase in dispersion with column alignment can significantly affect separation efficiency. Pure protein breakthrough profiles resulting from the application of bovine serum albumin onto STREAMLINE Q XL demonstrated that, at 10% breakthrough, 7.8% more protein could be applied to a vertical 1 cm dia. column compared to the same column misaligned by 0.15°. When an unclarified yeast homogenate was applied to a 1 cm dia. vertical column packed with STREAMLINE DEAE, 10% breakthrough of glucose-6-phosphate dehydrogenase (G6PDH) corresponded to a load 55% greater compared to the same column aligned 0.185° off-vertical. The G6PDH breakthrough curves for vertical and 0.15° off-vertical runs performed using a 5 cm column were essentially indistinguishable.     

A rapid enantioseparation system of capillary electrochromatography modified by electrostatic adsorption with transfersomes

Transfersomes were a special kind of nanomaterials with higher deformability and flexibility. A rapid method for coated-column preparation using anionic transfersomes as a coating material by electrostatic adsorption was developed. With carboxymethyl-β-cyclodextrin added in running buffer as the chiral selector, the capillary electrochromatography enantioseparation system based on the transfersomes-coated column modified by electrostatic adsorption was established for the first time. Propranolol and metoprolol acted as model drugs to evaluate the enantioseparation performance, these two basic drugs achieved baseline separation with satisfactory resolution and selection factor in this transfersomes-electrochromatography system but only partial separation in bare column system. In order to get the optimal separation condition, concentration of chiral selector, buffer pH, and applied voltage were systematically investigated. A rapid and efficient enantioseparation electrochromatography system was established and showed that transfersomes as the stationary phase could efficiently improve chiral separation effect.     

Validation of a model describing two-dimensional heat transfer during solid-state fermentation in packed bed bioreactors

A two-dimensional heat transfer model was validated against two experimental studies from the literature which describe the growth of Aspergillus niger during solid-state fermentation in packed bed bioreactors. With the same set of model parameters, the two-dimensional model was able to describe both radial temperature gradients, which dominated in one of the studies, and axial temperature gradients, which dominated in the other study. The sensitivity of the model predictions to the characteristics of the substrate and the microbe were explored. The temperatures reached in the column are most sensitive to parameters which affect the peak heat load, including the substrate packing density, the maximum specific growth rate, and the maximum biomass concentration. Even though the bed is assumed to be aerated with saturated air, the increase in temperature with bed height increases the water-carrying capacity of the air and therefore enables evaporation to contribute significantly to cooling. The model suggests that evaporation can remove as much as 78% of the heat from the bed during times of peak heat generation. Our model provides a tool which can guide the design and operation of packed bed bioreactors. However, further improvements are necessary to do this effectively, the most important of which is the incorporation of a water balance.     

Continuous adsorption and recovery of Cr(VI) in different types of reactors

This study reports the results of experiments on continuous adsorption and desorption of Cr(VI) ions by a chemically modified and polysulfone-immobilized biomass of the fungus Rhizopus nigricans. A fixed quantity of polymer-entrapped biomass beads corresponding to 2 g of dry biomass powder was employed in packed bed, fluidized bed, and stirred tank reactor for monitoring the continuous removal and recovery of Cr(VI) ions from aqueous solution and synthetic chrome plating effluent. Parameters such as flow rate (5, 10 and 15 mL/min), inlet concentration of Cr(VI) ions (50, 100, 150 and 250 mg/L) and the depth of biosorbent packing (22.8, 11.2 and 4.9 cm) were evaluated for the packed bed reactor. The breakthrough time and the adsorption rates in the packed bed column were found to decrease with increasing flow rate and higher Cr inlet concentrations and to increase with higher depths of sorbent packing. To have a comparative analysis of Cr adsorption efficiency in different types of reactors, the fluidized bed reactor and stirred tank reactor were operated using the same quantities of biosorbent material. For the fluidized bed reactor, Cr(VI) solution of 100 mg/L was pumped at 5 mL/min and fluidized by compressed air at a flow rate of 0.5 kg/cm.(2) The stirred tank reactor had a working volume of 200 mL capacity and the inlet/outlet flow rate was 5 mL/min. The maximum removal efficiency (mg Cr/g biomass) was obtained for the stirred tank reactor (159.26), followed by the fluidized reactor (153.04) and packed bed reactor (123.33). In comparison to the adsorption rate from pure chromate solution, approximately 16% reduction was monitored for synthetic chrome plating effluent in the packed bed. Continuous desorption of bound Cr ions from the reactors was effective with 0.01 N Na(2)CO(3) and nearly 80-94% recoveries have been obtained for all the reactors.