Suspended bed chromatography, a new approach in downstream processing

A new technique in downstream processing, suspended bed chromatography has been developed. This hybrid technique exploiting the benefits of batch adsorption and the process advantages of an enclosed column system can be carried out using established contactors and adsorbents. A 44 cm I.D. IsoPak column and the anion-exchange cellulose Express-Ion Exchanger Q were used in the purification of ovalbumin from hen-egg white. After suspension of 16.25 kg Express-Ion Q in 500 l of feedstock containing 5 g protein/l, adsorption was effected by recirculation of the suspension using the IsoPak slurry preparation station. Protein-loaded adsorbent was collected in the IsoPak column unit, where it was washed and protein desorbed using gradient elution at a flow-rate of 300 cm/h. The entire process was complete in under 3 h. With the introduction of pump-packed column systems and the availability of mechanically strong adsorbents suitable for column separations, suspended bed chromatography offers a new approach to downstream processing and provides a less challenging alternative to batch separations.     

Adsorption Strategy of Plasmid DNA Nanoparticulate: Preparative Purification by a Simple Custom Expanded Bed Column

This paper summarizes the critical examination of the hydrodynamic performance of the NBG expanded bed contactor operated with streamline-DEAE adsorbent under various operating conditions for expanded bed adsorption of plasmid DNA nanoparticles from alkaline lysate. The purification process is not RNase-free. In this study, a rapid and efficient scaleable purification protocol obtaining, plasmid DNA nanoparticles (average size of 40 nm) with a high purity level for use as therapeutic agent in customized NBG expanded bed columns was developed. This technique allows efficient levels of binding to the column media and vector purification without centrifugation or filtration steps. Residence time distribution (RTD) studies were exploited to achieve the optimal condition of plasmid DNA nanoparticle (pDNA) recovery upon anion exchange adsorbent in this contactor. In addition, the purification experiments were carried out in the expanded bed columns with settle bed height of 6.0 ± 0.2 cm. NaCl gradient elution enabled the isolation of supercoiled plasmid from low-Mr RNA, cDNA and plasmid variants. Subsequently dynamic binding capacity of the adsorbent was calculated while these values decreased with increase in flow velocity. Moreover, the effect of pH upon the performance of this recovery process and the feedstock volume upon the expanded bed anion exchange purification was investigated. The results demonstrated that separation of low-Mr RNA from plasmid DNA isoforms in the range of pH between 5.5 and 7.5 is achievable in this column. The yield of recovery of pDNA in optimal condition was higher than 88.51% which was a superior result in one-pass frontal chromatography. The generic application of simple customized NBG expanded bed column and its potential for the purification and recovery of plasmid DNA as a nanoparticulate bioproduct is strongly discussed.     

Adsorptive separations for the recovery and purification of biobutanol

A?conceptual adsorption process for the recovery and purification of biobutanol is proposed. Different porous materials are tested on their ability to perform the adsorptive separations relevant to the process. The metal-organic framework ZIF-8, silicalite zeolite and active carbon were compared with respect to their adsorption capacity of 1-butanol dissolved in water, as obtained in static and dynamic conditions by respectively batch and breakthrough measurements at room temperature. Batch experimentation showed that other compounds present in a real ABE fermentation have no significant effect on the adsorption of 1-butanol on ZIF-8. The breakthrough separation of 1-butanol from an aqueous ABE mixture was performed with a ZIF-8 packed column. The desorption of 1-butanol from a saturated ZIF-8 packed column by a stepwise increase of the temperature to 423?K in combination with a purge of a nitrogen gas (60?ml/min) shows that 1-butanol desorbs at low temperature from ZIF-8. Adsorption isotherms of ethanol, 1-butanol and water in liquid phase on the zeolite SAPO-34 were determined by batch adsorption at 298?K. Also the separation of an ethanol/1-butanol mixture and the removal of ethanol from 1-butanol could be achieved with a SAPO-34 packed column. From this experimental work, two materials—ZIF-8 and SAPO-34—thus emerged as suitable adsorbents for the recovery and purification of biobutanol by adsorption.     

Recovery of actinorhodin from fermentation broth

In the present work, a new method of purification for actinorhodin was developed using an expanded bed chromatography technique in which antibiotic capture, feedstock clarification, centrifugation, dialysis and concentration are done in one step. The cation-exchanger (P-11) resulted in 26% adsorption and 2% recovery whereas the anion-exchanger (DE-52) resulted in 99% adsorption and 56% recovery of adsorbed antibiotic using methanol buffer and 2 M NH4Cl as eluting agent. Streamline DEAE anion-exchanger, which is especially designed for EBA applications, yields 82% adsorption and 50% elution of actinorhodin fed into the chromatography column directly from the fermentation broth. Isocratic elution resulted in extremely efficient yield compared to linear gradient elution, i.e. 13.5-fold more recovery in the column with an aspect ratio (L:D) of 4. Expansion by 150% of settled bed resulted in the best recovery of actinorhodin among 100 and 200% expansions. A comparison of breakthrough profiles in packed and expanded bed adsorption showed that the performance of the expanded bed is better (by 33%) at allowing more volume of the fermentation broth to pass through the chromatography column.     

Expanded-bed chromatography in primary protein purification

Chromatography in stable expanded beds enables proteins to be recovered directly from cultivations of microorganisms or cells and preparations of disrupted cells, without the need for prior removal of suspended solids. The general performance of an expanded bed is comparable to a packed bed owing to reduced mixing of the adsorbent particles in the column. However, optimal operating conditions are more restricted than in a packed bed due to the dependence of bed expansion on the size and density of the adsorbent particles as well as the viscosity and density of the feedstock. The feedstock composition may become the most limiting restriction owing to interactions of adsorbent particles with cell surfaces, DNA and other substances, leading to their aggregation and consequently to bed instabilities and channeling. Despite these difficulties, expanded-bed chromatography has found widespread applications in the large scale purification of proteins from mammalian cell and microbial feedstocks in industrial bioprocessing. The basics and implementation of expanded-bed chromatography, its advantages as well as problems encountered in the use of this technique for the direct extraction of proteins from unclarified feedstocks are addressed.     

Modelling Affinity Chromatography

Abstract

Affinity chromatography plays a significant role in the separation and purification of biologically active macromolecules in laboratory and large-scale applications. There is a need for models which could be used to predict accurately the dynamic behavior of affinity chromatography separations, in order to permit the design, optimization, control, and process scale-up of affinity chromatography systems. Furthermore, the construction and use of such models will contribute to a better fundamental understanding of the physicochemical and biospecific mechanisms involved in affinity chromatography processes. The parameters of the models should be obtainable by using information from a small number of experiments.

This work reviews the modeling of affinity chromatography, and presents general models that could be used to describe the dynamic behavior of the adsorption, wash, and elution stages of affinity chromatography systems. Certain model structures, modeling approaches and operational strategies for systems having porous or nonporous adsorbent particles are also suggested, and experiments are proposed whose data are necessary for parameter estimation and model discrimination studies in affinity chromatography.

Particular emphasis is given to :he modeling of the intrinsic mechanisms of intraparticle diffusion, adsorption, and desorption, because the intrinsic mechanisms are normally independent of the mode of operation (i.e., batch, fixed bed, fluidized bed, continuous countercurrent, or others).     

Macroporous copolymer matrix. IV. Expanded bed adsorption application

Macroporous crosslinked hydroxyethyl methacrylate-ethylene dimethacrylate copolymeric beads (HEG beads) were synthesized by suspension polymerization in the presence of a pore generating agent. These beads were coupled to alpha-cyclodextrin through a urethane spacer. These modified copolymer beads (affinity-HEG beads) so prepared were evaluated for their suitability in expanded bed chromatography. The optimum thickness of the distributor plate for stable expanded bed for use in expanded bed adsorption (EBA) was established. The affinity-HEG beads are comparable in density to Streamline diethyl amino ethane (DEAE) and exhibit better mechanical stability at higher superficial velocity under fluidization. The affinity-BEG beads were used as affinity chromatography matrices for the purification of cyclodextrin glycosyltransferase. Feeding of 5-fold diluted fermented broth to the column containing affinity-HEG beads of settled bed height 7.5 cm (I.D. 26 mm and length 42 cm) at double bed expansion resulted in a sharp breakthrough curve of alpha-cyclodextrin glycosyltransferase (CGTase). The adsorbed enzyme was eluted from the bed in 50 mM Tris-HCl buffer containing 10 mM CaCl2 at 25 degrees C in packed bed configuration.     

Purification of L-Lysine in Simulated Moving Bed and Fixed-Bed Chromatography

 L-Lysine was produced by a microbial process utilizing a Corynebacterium glutamicum (ATCC 21799) strain. L-Lysine was purified from the cultivated medium by fixed-bed and simulated moving bed （SMB） chromatography. The separation conditions including pH, eluent concentration and Lys+ and Lys2+ adsorption isotherms were studied in batch adsorption. The column capacity, eluent flow rate and eluent concentration have been studied in fixed-bed chromatography. Maximum purification rate of lysine was obtained as 0.066 g/(g·h) (per gram resin and per hour) at an eluent flow rate of 10 mL/min in fixed-bed chromatography. The results obtained from SMB were 0.11 g/(g·h) for L-lysine purification rate and 96% for L-lysine recovery.     

Use of expanded bed adsorption to purify flavonoids from Ginkgo biloba L.

Three techniques (liquid–liquid extraction, packed bed adsorption and expanded bed adsorption) have been compared for the purification of flavonoids from the leaves of Ginkgo biloba L. A crude Ginkgo extract was obtained by refluxing with ethanol for 3 h. The yield of flavonoids achieved by this crude extraction was about 19% (w/w) and the purity of flavonoids in the concentrated extract was between 1.9 and 2.3% (w/w). The crude extract was then dissolved in deionized water and centrifuged where necessary to prepare clarified feedstock for further purification. For the method using liquid–liquid extraction with ethyl acetate, the purity, concentration ratio and yield of flavonoids were 25.4–31.0%, 16–18 and >98%, respectively. For the method using packed bed adsorption, Amberlite XAD7HP was selected as the adsorbent and clarified extract was used as the feedstock. The dynamic adsorption breakthrough curves and elution profiles were measured. For a feedstock containing flavonoids at a concentration of 0.25 mg/mL, the appropriate loading volume to reach a 5% breakthrough point during the adsorption stage was estimated to be 550–600 mL for a packed bed of volume 53 mL and a flow rate of 183 cm/h. The results from the elution stage indicated that the majority of impurities were eluted by ethanol concentrations of 40% (v/v) or below and efficient separation of flavonoids from the impurities could be achieved by elution of the flavonoids with 50–80% ethanol reaching an average purity of ∼25%. The recovery yield of flavonoids using the packed bed purification method was about 60% of the flavonoids present in the clarified feedstock (corresponding to around 30% for the total flavonoids in the unclarified crude extract). For the method using expanded bed adsorption also conducted with Amberlite XAD7HP as the adsorbent, the optimal operation conditions scouted during the packed bed experiments were used but unclarified crude extract could be loaded directly into the column. For an expanded bed with a settled bed height of 30 cm, the loss of flavonoids in the column flow-through was about 30%. The two-step elution protocol again proved to be effective in separating the adsorbed impurities and flavonoids. More than 96% of the bound impurities were completely removed by 40% ethanol in the first elution stage and less than 4% remained in the final product eluted by 90% ethanol in the second elution stage. Also, ∼74% of the adsorbed flavonoids on column (corresponding to 51% of the total flavonoids in the unclarified feedstock) were recovered in the product. In addition to higher recovery yield, the average process time to obtain the same amount of product was decreased in the expanded bed adsorption (EBA) process. The results suggest that the adoption of EBA procedures can greatly simplify the process flow sheet and in addition reduce the cost and time to purify flavonoids from Ginkgo biloba. These results clearly demonstrate the potential for the use of EBA to purify pharmaceuticals from plant sources.     

Efficiency of preparative and process column distribution systems

An analytical method for computing the residence time distribution of the liquid distribution system in chromatography columns is described. The impact of the distributor design on the separation efficiency is predicted as a function of media properties and packed bed dimensions. The efficiency loss due to the distributor when increasing column diameter during scale-up is quantified. It is shown that this loss can be compensated by modulating the local bed height via a moderate inclination of the bed support. It is concluded that the selection of an appropriate distributor design concept with optimised dimensions enables a scale-up of chromatographic separations without any significant loss of chromatographic efficiency due to the distribution system.     

丹参酚酸B生产中去除胶体类杂质的工艺方法

胶体类杂质的去除是丹参酚酸B(salvianolic acid B, SB)纯化工艺的难点之一。实验中基于前沿色谱与置换色谱相结合的原则,改良常规大孔吸附树脂柱的操作方法,将树脂按一定的比例装入大小两支柱。小柱与大柱串联,上样至胶体类杂质在小柱上达到吸附饱和,用50%甲醇单独洗脱大柱上的SB部分,利用树脂吸附色谱法实现了SB与胶体类杂质的分离。结果表明,经过去胶体类杂质处理后,SB的加权平均纯度由59.6%提高到64.5%,收率由69.75%提高到80.0%,并且SB的洗脱条件降低。本工艺方法适合于规模化工业生产。     

Direct enzyme adsorption from an unclarified microbial feedstock using suspended bed chromatography

Suspended bed chromatography (SBC) is a new hybrid technique concomitantly benefiting from batch adsorption, the process advantages of an enclosed system, and its compatibility with established commercial chromatographic contactors and adsorbents. SBC was evaluated in the anion-exchange capture and chromatographic fractionation of native glyceraldehyde-3-phosphate dehydrogenase (G3PDH) from the complex mixture of molecular and particulate moieties that constitute wet-milled bakers' yeast. Method scouting established operating conditions exploiting Whatman Express-Ion Exchanger Q at pH 7.5 and a disrupted biomass concentration equivalent to 3.5% (wet mass/v original intact cells). Partially purified G3PDH was recovered directly from the yeast disruptate in a scaled-down process developed at 1/756 process scale. This was used to establish operating parameters to facilitate process scale-up to exploit a 44 cm I.D. Millipore IsoPak column, 18 kg (swollen mass) of Express-Ion Q anion-exchange cellulose and 275 1 of 3.5% (wet w/v) bakers' yeast disruptate. The generic utility of SBC was demonstrated for direct product adsorption from feedstocks characterised by a modest content of bioparticulates (equivalent to < 4% (wet w/v) disrupted cells). Analyses illustrated an enrichment of G3PDH in respect of enzyme concentration and significant reduction in product turbidity and Pico-Green reactivity (correlated with double stranded (ds) DNA content). The application niche for this new approach to primary protein recovery is discussed with particular reference to the downstream processing of coarsely clarified whole broths, cell disruptates and biological extracts.     

Adsorption in columns packed with porous adsorbent particles having partially fractal structures

A mathematical model is constructed and solved that could describe the dynamic behavior of the adsorption of a solute of interest in single and stratified columns packed with partially fractal porous adsorbent particles. The results show that a stratified column bed whose length is the same as that of a single column bed, provides larger breakthrough times and a higher dynamic utilization of the adsorptive capacity of the particles than those obtained from the single column bed, and the superior performance of the stratified bed becomes especially more important when the superficial velocity of the flowing fluid stream in the column is increased to accommodate increases in the system throughput. This occurs because the stratified column bed provides larger average external and intraparticle mass transfer and adsorption rates per unit length of packed column. It is also shown that increases in the total number of recursions of the fractal and the ratio of the radii between larger and smaller microspheres that make up the partially fractal particles, increase the intraparticle mass transfer and adsorption rates and lead to larger breakthrough times and dynamic utilization of the adsorptive capacity of the particles. The results of this work indicate that highly efficient adsorption separations could be realized through the use of a stratified column comprised from a practically reasonable number of sections packed with partially fractal porous adsorbent particles having reasonably large (i) total number of recursions of the fractal and (ii) ratio of the radii between larger and smaller microspheres from which the partially fractal particles are made from. It is important to mention here that the physical concepts and modeling approaches presented in this work could be, after a few modifications of the model, applied in studying the dynamic behavior of chemical catalysis and biocatalysis in reactor beds packed with partially fractal porous catalyst particles.     

Isolation and preparative purification of microcystin variants

Preparative reversed-phase liquid chromatography was successfully used to purify two microcystins (microcystin LR and microcystin LA) from a cyanobacterial process waste. The separation protocol involved extraction of lyophilized cells by methanol, isolation and concentration by solid-phase extraction, and purification by reversed-phase HPLC. Milligram-level loading of microcystins was obtained on a solid-phase extraction cartridge packed with 0.5 g of C18 stationary phase. The separations were first carried out on an analytical column and then scaled-up to a preparative column. The microcystins were quantified by HPLC and enzyme-linked immunosorbent assay. A method to remove microcystins rapidly and economically from the cyanobacterial process waste is also described.     

Preparative liquid chromatography

The status of the theory and the main methods of implementation of preparative liquid chromatography are reviewed. On the theory front, the focus has recently shifted. The theory of non-linear, non-ideal chromatography has given rise to numerous models whose advantages, disadvantages and ranges of application are now well understood. Interest now resides in investigating the equilibrium thermodynamics of complex new systems, in the study of the kinetics of mass transfers in conventional chromatographic systems, and in the application of the various models of chromatography to optimize the experimental conditions. Progress in computer technology allows the use of sophisticated models, provided their parameters can be measured. This allows the detailed investigation of separations for which the mass transfer kinetics is slow such as chiral separations, the purification of basic compounds, and the extraction of recombinant proteins. On the applied front, in addition to numerous incremental improvements in reliability and economic performance, a few essential new features should be noted, i.e. the availability of instruments for simulated moving bed separations at the scale needed for preparative chiral separations, the use of expanded beds for the extraction of recombinant proteins from fermentation broths, and the attention given to improvements in the performance of packed beds. A survey of the literature dealing with practical applications and recent meetings shows that preparative chromatography is becoming a well established separation and purification method in the pharmaceutical industry.     

Expanded Bed Adsorption Chromatography for Recovery of Phycocyanins from the Microalga Spirulina Platensis

We carried out the purification of C-phycocyanin and allophycocyanin from Spirulina platensis taking advantage of the adsorption properties of the expanded beds. Initially, phycobiliproteins were released from the microalga cells by osmotic shock. Next, phycocyanins were recovered by applying the centrifuged cell suspension directly to the anion exchanger Streamline-DEAE using expanded bed columns, equilibrated with 50 mM sodium phosphate buffer, pH 7.0. After adsorption, washing was carried out in the expanded-bed mode. Having removed unbound proteins and cellular debris, the bed was allowed to sediment and phycocyanins rich solution was eluted with a downward flow of 500 mM sodium phosphate buffer, pH 7.0. Finally, we utilized conventional gel filtration and ion exchange chromatography methods for separation and purification of C-phycocyanin and allophycocyanin. The purification steps were monitored using sodium dodecyl sulfate-polyacrylamide gel electrophoresis, and the purity of recovered phycocyanins was confirmed by absorption and emission spectroscopy. The main advantage of this new method is the high yield achieved in the steps of product extraction and adsorption by expanded bed adsorption, so reducing both processing times and costs.     

Capillary electrochromatography using polyelectrolyte multilayer coatings

This review covers recent progress in polyelectrolyte multilayer (PEM) coatings applied to analytical separations using open-tubular capillary electrochromatography (OT-CEC). The simple preparation procedure involved in the PEM approach has provided some attractive features over other modes of capillary electrophoresis-based separations including packed column capillary electrochromatography (PC-CEC) and micellar electrokinetic chromatography (MEKC). PEM coatings have been used to alleviate the adsorption of basic analytes, to improve separations, and to improve the stability of the electroosmotic flow. Fundamental aspects of PEM coatings on surfaces and analytical separation platforms are briefly outlined in this review. In addition, applications of PEM coatings to fused-silica capillaries or microchip separation devices for the separation of small achiral or chiral analytes, as well as large biomolecules, are discussed.     

Analysis of aminofluorescein-fatty acid derivatives by capillary electrophoresis with laser-induced fluorescence detection at the attomole level: application to mycobacterial fatty acids

In the present work, a new method of purification for antithrombin was developed using an expanded bed chromatography technique. Milk fat was removed by centrifugation and caseins were precipitated selectively by addition of zinc chloride. Crude skim milk was then directly fed to an expanded bed column containing the ion-exchange matrix. The use of a cation-exchanger (P-11) resulted in 100% adsorption and 13% recovery whereas the use of an anion-exchanger (DE-52) resulted in 100% adsorption and 84% recovery and up to five-fold purification of antithrombin. The buffer, 25 mM Tris-HCl pH 8.0; the eluting agent, 2 M (NH4)2SO4; and 100% expansion of settled bed were determined to be the optimum conditions for the purification of antithrombin by ion-exchange expanded bed chromatography. A comparison of column diameters revealed that the elution yields increase by two-fold while the column diameter increases from 1 to 2.5 cm. However, antithrombin III was concentrated to a higher degree by using the column with an internal diameter of 1 cm.     

多柱色谱技术进展

在色谱分析过程中，利用串联、并联或串并联结合的方式将多根色谱柱组合起来，可以实现高通量和高分辨的分离效果。相比于传统单柱色谱技术，多柱技术很好地满足了批量样品分析和复杂生物样品分离分析的需求，因此引起了广泛关注。该文对多柱技术在多维分离、芯片色谱、毛细管电泳、固定相筛选以及串联色谱等领域的应用进行了综述，并对其发展前景进行了展望。     

磁场辅助毛细管电色谱

磁场辅助毛细管电色谱是液相色谱研究领域中出现的新技术．它利用外加磁场的引力将置于毛细管内的具有磁响应性的硅胶微球或四氧化三铁微球固定在管内任意位置．磁场固定微球聚集体既可用作填充柱,直接用于电色谱分离;也可用作柱筛,用于填装由商品色谱填料组成的色谱柱．这一技术的优势在于制备简便易行,柱管可以再生使用,适合于微流控芯片上柱筛或柱床的制作．本文简要评述磁场辅助毛细管电色谱的进展,包括磁性色谱填料的制备,磁场固定柱床电色谱,磁性柱筛电色谱及毛细管柱内柱结构参数的测定等方面．