Dye–ligand expanded bed adsorption of G6PDH from highly dense unclarified yeast extract

The application of dye–ligand expanded bed chromatography adsorption (EBA) of glucose-6-phosphate dehydrogenase (G6PDH) from unclarified yeast extract was undertaken by using a commercially available expanded bed column (20 mm i.d.) and UpFront adsorbent (ρ = 1.5 g/mL) from UpFront Chromatography. The influence of biomass concentration on the adsorption capacity was explored by employing yeast extracts containing various biomass concentrations (5–30%, w/v). It was demonstrated that the biomass concentration had little effect on G6PDH adsorption performance. Feedstock containing 15% (w/v) biomass gave a relatively high recovery yield (>90%) of G6PDH compared to feedstock containing 30% (w/v) biomass, which gave a recovery of 75% G6PDH. Nevertheless, the enzyme specific activity of 7 U mg⁻¹ with a purification factor of 6 was achieved in the feedstock containing biomass concentration of 30% (w/v). The generic applicability of dye–ligand as an affinity tool in expanded bed chromatography is discussed.     

The influence of bakers’ yeast cells on protein adsorption performance in dye-ligand expanded bed chromatography

The influence of whole yeast cells (0–15% w/v) on the protein adsorption performance in dye-ligand chromatography was explored. The adsorption of a model protein, bovine serum albumin (BSA), was selected to demonstrate this approach. The UpFront adsorbent (ρ=1.5 g/cm³) derivatised with Cibacron Blue 3GA and a commercially available expanded bed column (20 mm i.d.) from UpFront Chromatography, Denmark, were employed in the batch binding and expanded bed operation. The BSA binding capacity was demonstrated to not be adversely affected by the presence of yeast cells. The dynamic binding capacity of BSA at aC/C ₀=0..1 biomass concentration of 5, 10, 15% w/v were 9, 8, and 7.5 mg/mL of settled adsorbent, respectively.     

Thermophilic high-rate anaerobic treatment of wastewater containing long-chain fatty acids: effect of washed out biomass recirculation

Biomass washed out from an expanded granular sludge bed (EGSB) reactor treating oleate (82%, w/w) was inves-tigated. This biomass had a 50% higher activity compared to granules present in the EGSB reactor. Recirculationof washed out biomass into reactor remarkably improved the treatment performance. The highest methane conversion rate from oleate, 300 mg CH₄-COD/g VSS.d, was achieved at a concentration of 4 g oleate-COD/l and a volumetric loading rate of 8 g COD/l.d. This revised version was published online in November 2006 with corrections to the Cover Date.     

Partial purification properties of human epidermal growth factor from recombinant Escherichia coli by expanded bed adsorption

Human epidermal growth factor is a polypeptide hormone having many diverse biological functions. This paper first presents the recovery results of human epidermal growth factor (hEGF) immediately from the fermentation broth of recombinant Escherichia coli by using an expanded bed system (a couple of STREAMLINE25 and ÄKTA explorer 100). The influences of operational conditions such as linear flow rate, gradient length of NaCl concentration, pH and sample concentration on the purification performances of hEGF in expanded and packed bed modes with STREAMLINE DEAE resin were systematically evaluated. After optimization, the practical recovery procedure in the expanded bed mode was carried out on a scaled-up system under the conditions of linear flow rates of 183 cm/h (upward) and 37 cm/h (downward), sample volume of 300 ml and column bed height of 13.8 cm which yielded a primary product of hEGF from the cell-free supernatant containing hEGF after centrifugation at 4000 rev/min for 15 min. As a result, the hEGF concentration in the product was higher than 20% (w/v), the concentration factor was greater than 4.3 and the total yield was higher than 80%, respectively. At the same time, the results of hEGF recovery by using expanded bed adsorption (EBA), packed bed chromatography (PBC) and salting out were compared. The results show that the procedure of hEGF recovery in expanded bed adsorption has some advantages over the other two procedures, because of its higher concentration factor, recovery yield, productivity, hEGF concentration in the primary product and shorter duration of purification run.     

Operational intensification by direct product sequestration from cell disruptates: application of a pellicular adsorbent in a mechanically integrated disruption-fluidised bed adsorption process

A novel prototype adsorbent, designed for intensified fluidised bed adsorption processes, was assembled by the emulsification coating of 4% (w/v) porous agarose upon a zirconia-silica solid core. The adsorbent, designated ZSA (particle density 1.75 g/ml, maximum pellicle depth 40 microm), was subjected to physical and biochemical comparison with the performance of two commercial adsorbents (Streamline and Macrosorb K4AX). Bed expansion qualities and hydrodynamic characteristics (N, D(axl) and B(o)) of ZSA demonstrated a marked robustness in the face of elevated velocities (up to 550 cm/h) and biomass loading (up to 30% (ww/v)) disrupted yeast cells. Cibracron Blue derivatives of the pellicular prototype (ZSA-CB), evaluated in the batch and fluidised bed recovery of glyceraldehyde 3-phosphate dehydrogenase (G3PDH) from unclarified yeast disruptates, exhibited superior capacities and adsorption/desorption performance to the commercial derivatives. These advanced physical and biochemical properties facilitated a demonstration of the direct, mechanical coupling of bead-milling and fluidised bed adsorption in a fully integrated process for the accelerated recovery of G3PDH from yeast. The generic application of such pellicular adsorbents and integrated processes to the recovery of labile, intracellular products is discussed.     

Preparative regio- and chemoselective functionalization of hydrocarbons catalyzed by cell free preparations of 2-hydroxybiphenyl 3-monooxygenase

Oxygenases are useful catalysts for the selective incorporation of molecular oxygen into hydrocarbons. Here, we report on the application of isolated, cell free 2-hydroxybiphenyl 3-monooxygenase (HbpA) as catalyst for the regio- and chemospecific hydroxylation of 2-hydroxybiphenyl to 2,3-dihydroxybiphenyl. The catalyst was prepared from recombinant Escherichia coli using expanded bed adsorption chromatography and could be stored without significant loss of activity in lyophilized form. The reaction was performed in an aerated and thermostated simple stirred glass vessel in an aqueous (20% v/v)/organic (80% v/v) reaction medium. This allowed in situ product recovery preventing substrate and product inhibition of the catalyst as well as decay of the labile product 2,3-dihydroxybiphenyl. Enzymatic regeneration of reduced nicotinamide cofactors was achieved using the formate/formate dehydrogenase system. We obtained volumetric productivities of up to 0.45 g l⁻¹ h⁻¹. No significant decrease of productivity was observed within 7 h and more. Product purification (purity 92%) was achieved using solid phase extraction with aluminum oxide followed by crystallization as a polishing step (purity>99%).

To our knowledge, these results show for the first time the perspectives of integrated enzyme and cofactor regeneration-based biocatalytic processes in organic/aqueous emulsions, coupled with in situ product recovery.     

The disruption ofSaccharomyces cerevisiae cells and release of glucose 6-phosphate dehydrogenase (G6PDH) in a horizontal dyno bead mill operated in continuous recycling mode

Baker’s yeast was disrupted in a 1.4-L stainless steel horizontal bead mill under a continuous recycle mode using 0.3 mm diameter zirconia beads as abrasive. A single pass in continuous mode bead mill operation liberates half of the maximally released protein. The maximum total protein release can only be achieved after passaging the cells 5 times through the disruption chamber. The degree of cell disruption was increased with the increase in feeding rate, but the total protein release was highest at the middle range of feeding rate (45 L/h). The total protein release was increased with an increase in biomass concentration from 10 to 50% (w/v). However, higher heat dissipation as a result of high viscosity of concentrated biomass led to the denaturation of labile protein such as glucose 6-phosphate dehydrogenase (G6PDH). As a result the highest specific activity of G6PDH was achieved at biomass concentration of 20% (ww/v). Generally, the degree of cell disruption and total protein released were increased with an increase in impeller tip speed, but the specific activity of G6PDH was decreased substantially at higher impeller tip speed (14 m/s). Both the degree of cell disruption and total protein release increased, as the bead loading increased from 75 to 85% (v/v). Hence, in order to obtain a higher yield of labile protein such as G6PDH, the yeast cell should not be disrupted at biomass concentration and impeller tip speed higher than 20% (w/v) and 10 m/s, respectively.     

The influence of bakers’ yeast cells on protein adsorption in anion exchange expanded bed chromatography

Baker’s yeast was disrupted in a 1.4-L stainless steel horizontal bead mill under a continuous recycle mode using 0.3 mm diameter zirconia beads as abrasive. A single pass in continuous mode bead mill operation liberates half of the maximally released protein. The maximum total protein release can only be achieved after passaging the cells 5 times through the disruption chamber. The degree of cell disruption was increased with the increase in feeding rate, but the total protein release was highest at the middle range of feeding rate (45 L/h). The total protein release was increased with an increase in biomass concentration from 10 to 50% (w/v). However, higher heat dissipation as a result of high viscosity of concentrated biomass led to the denaturation of labile protein such as glucose 6-phosphate dehydrogenase (G6PDH). As a result the highest specific activity of G6PDH was achieved at biomass concentration of 20% (ww/v). Generally, the degree of cell disruption and total protein released were increased with an increase in impeller tip speed, but the specific activity of G6PDH was decreased substantially at higher impeller tip speed (14 m/s). Both the degree of cell disruption and total protein release increased, as the bead loading increased from 75 to 85% (v/v). Hence, in order to obtain a higher yield of labile protein such as G6PDH, the yeast cell should not be disrupted at biomass concentration and impeller tip speed higher than 20% (w/v) and 10 m/s, respectively.     

Routine manufacture of recombinant proteins using expanded bed adsorption chromatography

Two different recombinant human proteins were purified directly from Pichia pastoris whole cell fermentation broth, containing 30–44% biomass (wet weight percent), by strong cation exchange expanded bed adsorption chromatography. Expanded bed adsorption chromatography provided clarification, product purification and product concentration in a single unit operation at large scale (2000-l nominal fermentation volume). The efficiency of expanded bed adsorption chromatography resulted in a short process time, high process yield, and limited proteolytic degradation of the target proteins. The separations were operated using a 60-cm (d) column run at 14 l/min. For one protein, expanded bed adsorption chromatography resulted in an average product recovery of 113% (relative to fermentation supernatant) and a purity of 89% (n=10). For the other protein, the average product recovery was 99% (relative to fermentation supernatant) and the purity was 62.1 (n=10). Laboratory experiments showed that biomass reduced product dynamic binding capacity for protein 2.     

Effective recovery of poly‐β‐hydroxybutyrate (PHB) biopolymer from Cupriavidus necator using a novel and environmentally friendly solvent system

This work demonstrates a significant advance in bioprocessing for a high‐melting lipid polymer. A novel and environmental friendly solvent mixture, acetone/ethanol/propylene carbonate (A/E/P, 1:1:1 v/v/v) was identified for extracting poly‐hydroxybutyrate (PHB), a high‐value biopolymer, from Cupriavidus necator. A set of solubility curves of PHB in various solvents was established. PHB recovery of 85% and purity of 92% were obtained from defatted dry biomass (DDB) using A/E/P. This solvent mixture is compatible with water, and from non‐defatted wet biomass, PHB recovery of 83% and purity of 90% were achieved. Water and hexane were evaluated as anti‐solvents to assist PHB precipitation, and hexane improved recovery of PHB from biomass to 92% and the purity to 93%. A scale‐up extraction and separation reactor was designed, built and successfully tested. Properties of PHB recovered were not significantly affected by the extraction solvent and conditions, as shown by average molecular weight (1.4 × 10⁶) and melting point (175.2°C) not being different from PHB extracted using chloroform. Therefore, this biorenewable solvent system was effective and versatile for extracting PHB biopolymers. © 2016 American Institute of Chemical Engineers Biotechnol. Prog., 32:678–685, 2016     

Preliminary studies on continuous recovery and purification of the penicillin acylase under pseudo-affinity conditions using phenyl-Sepharose gel

A continuous system for the recovery and purification of the penicillin acylase from crude extracts by recycling phenyl-Sepharose gel through three agitated vessels with disc filters of stainless steel is presented. The penicillin acylase present in the crude extract was absorbed into the phenyl-Sepharose gel under pseudo-affinity conditions (16% w/v of ammonium sulphate). After gel washing under the same conditions in the second vessel, enzyme desorption was performed using the same salt but at a lower concentration (6% w/v) in the third vessel. The preliminary studies reported here occurred without experimental difficulties, even at a gel concentration as high as 40% (v/v). The recovery of the penicillin acylase was achieved with high yield (74%), but a low purification factor of 2.4 was obtained owing to the use of a crude extract with low specific activity.     

Capture of a recombinant protein from unclarified canola extract using streamline expanded bed anion exchange

The feasibility of applying expanded bed adsorption technology to recombinant protein recovery from extracts of transgenic canola (rapeseed) was assessed. The extraction step results in a suspension of high solids content that is difficult to clarify. The coarse portion of the solids can be removed easily, and our aim was to operate the expanded bed in the presence of the recalcitrant particulates. Recombinant beta-glucuronidase (rGUS) produced in transgenic canola seed was the model system. Diethylaminoethyl (DEAE) and Streamline DEAE resin exhibited similar binding and elution properties for both rGUS and native canola proteins. More than 95% of native canola proteins did not bind to DEAE resins at pH 7.5, whereas the bound proteins were fractionated by two-step salt elution into two groups with the first peak, containing 70% of total bound proteins, at 20 mS/cm, followed by elution of rGUS at 50 mS/cm. The adsorption isotherm was only slightly influenced by the presence of up to 14 mg solids/mL extract; C(m) and K(d) changed by -1% and +39%, respectively. Bed expansion was semiquantitatively predictable from physical properties of the fluid together with Stokes's law and the Richardson-Zaki correlation for both clarified and partially clarified extracts. The presence of 1.4% solids did not change rGUS breakthrough behavior of the expanded bed; however, a small difference between expanded bed and packed bed was observed early in the sample loading stage, during which bed expansion adjusts. Canola solids moved through the column in approximately plug flow with no detriment to bed stability. Seventy-two percent recovery of 34-fold purified rGUS was obtained after initial loading of 1.4% (w/w) solids extract to 25% breakthrough.     

Minimising biomass/adsorbent interactions in expanded bed adsorption processes: a methodological design approach

Expanded bed adsorption (EBA) is an integrated technology for the primary recovery of proteins from crude feedstock. Interactions between solid matter in the feed suspension and fluidised adsorbent particles influence bed stability and therefore have a significant impact on protein adsorption in expanded beds. In order to design efficient and reliable EBA processes a strategy is needed, which allows to find operating conditions, where these adverse events do not take place. In this paper a methodological approach is presented, which allows systematic characterisation and minimisation of cell/adsorbent interactions with as little experimental effort as possible. Adsorption of BSA to the anion exchanger Streamline Q XL from a suspension containing S. cerevisiae cells was chosen as a model system with a strong affinity of the biomass towards the stationary phase. Finite bath biomass adsorption experiments were developed as an initial screening method to estimate a potential interference. The adhesiveness of S. cerevisiae to the anion exchanger could be reduced significantly by increasing the conductivity of the feedstock. A biomass pulse response method was used to find optimal operation conditions showing no cell/adsorbent interactions. A good correlation was found between the finite bath test and the pulse experiment for a variety of suspensions (intact yeast cells, E. coli homogenate and hybridoma cells) and adsorbents (Streamline Q XL, DEAE and SP), which allows to predict cell/adsorbent interactions in expanded beds just from finite bath adsorption tests. Under the optimised operating conditions obtained using the prior methods, the stability of the expanded bed was investigated during fluidisation in biomass containing feedstock (up to 15% yeast on wet weight basis) employing residence time distribution analysis and evaluation by an advanced model. Based on these studies threshold values were defined for the individual experiments, which have to be achieved in order to obtain an efficient EBA process. Breakthrough experiments were conducted to characterise the efficiency of BSA adsorption from S. cerevisiae suspensions in EBA mode under varying operating conditions. This allowed to correlate the stability of the expanded bed with its sorption efficiency and therefore could be used to verify the threshold values defined. The approach presented in this work provides a fast and simple way to minimise cell/adsorbent interactions and to define a window of operation for protein purification using EBA.     

Development of an expanded bed technique for an affinity purification of G6PDH from unclarified yeast cell homogenates

The use of an expanded bed of STREAMLINE Red H-7B for the purification of the intracellular glycolytic enzyme glucose 6-phosphate dehydrogenase (G6PDH) directly from untreated preparations of disrupted yeast cells has been investigated. Small-scale experiments, carried out in packed beds, have shown that the optimal pH for adsorption is 6.0 and have enabled optimization of elution conditions using a series of eluents. The dynamic capacity of the adsorbent for G6PDH was determined in a small expanded bed to be 28 units/mL. These results were used to develop a preparative scale separation of G6PDH in a STREAMLINE 50 expanded bed column. G6PDH was purified directly from an unclarified yeast homogenate in 99% yield with an average purification factor in the eluted fraction of 103. Cleaning-in-place (CIP) procedures using 0.5 M NaOH and 4M urea in 60% (v/v) ethanol have demonstrated that the adsorbent can be regenerated with no loss of adsorption capacity of alteration of bed expansion characteristics after many cycles of operation. (c) 1995 John Wiley & Sons, Inc.     

The influence of biomass on the hydrodynamic behavior and stability of expanded beds

Expanded bed adsorption is an innovative chromatographic technology that allows the introduction of particle-containing feedstock without the risk of blocking the bed. Provided a perfectly classified fluidized bed (termed expanded bed) is formed in the crude feedstock and the biomass is not influencing protein transport towards the adsorbent surface, a sorption performance comparable to packed beds is found. The influence of biomass on the hydrodynamic stability of expanded beds is essential and was investigated systematically in this article. Residence-time distribution analyses were performed using model systems and a yeast suspension under various fluid-phase conditions. It is demonstrated that three factors (biomass/adsorbent interactions, biomass concentration, and flow rate) play an interdependent role disturbing the classified fluidization of an expanded bed. A clear correlation between the degree of aggregative fluidization--obtained by PDE modeling of RTD data--and the expansion behavior of the fluidized bed has been found. Thus, combining three analytical methods, namely cell transmission index analysis, expansion analysis, and RTD analysis provides a solid base for understanding and control of the fluidization behavior and thus further process design during the initial phase of process development.     

Column sorption of Cr(VI) from electroplating effluent using formaldehyde cross-linked Saccharomyces cerevisiae

Pellets of Saccharomyces cerevisiae, cross-linked by 13% (w/v) formaldehyde, were used in fixed-bed columns to remove Cr(VI) from electroplating rinse effluent at varied influent pHs (2.5–7.5). The Cr uptake at 60% saturation of the biomass was 6.3 mg/g at an optimum pH of 2.5. Desorption of the bound metal was partially achieved by washing the column biomass with a combined solution of 1% (w/v) formaldehyde and 1 M HNO3. © Rapid Science Ltd. 1998     

Protein adsorption and hydrodynamic stability of a dense, pellicular adsorbent in high-biomass expanded bed chromatography

A dense, pellicular UpFront adsorbent (ϱ=1.5 g/cm³, UpFront Chromatography, Cophenhagen, Denmark) was characterized in terms of hydrodynamic properties and protein adsorption performance in expanded bed chromatography. Cibacron Blue 3GA was immobilised into the adsorbent and protein adsorption of bovine serum albumin (BSA) was selected to test the setup. The Bodenstein number and axial dispersion coefficient estimated for this dense pellicular adsorbent was 54 and 1.63×10⁻⁵ m²/s, respectively, indicating a stable expanded bed. It could be shown that the BSA protein was captured by the adsorbent in the presence of 30% (w/v) of whole-yeast cells with an estimated dynamic binding capacity (C/C ₀=0.01) of approximately 6.5 mg/mL adsorbent.     

Nitrogen removal in moving bed sequencing batch reactor using polyurethane foam cubes of various sizes as carrier materials

The performance of moving bed sequencing batch reactors (MBSBRs) added with 8 % (v/v) of polyurethane (PU) foam cubes as carrier media in nitrogen removal was investigated in treating low COD/N wastewater. The results indicate that MBSBR with 8-mL cubes achieved the highest total nitrogen (TN) removal efficiency of 37% during the aeration period, followed by 31%, 24% and 19 % for MBSBRs with 27-, 64- and 125-mL cubes, respectively. The increased TN removal in MBSBRs was mainly due to simultaneous nitrification and denitrification (SND) process which was verified by batch studies. The relatively lower TN removal in MBSBR with larger PU foam cubes was attributed to the observation that larger PU foam cubes were not fully attached by biomass. Higher concentrations of 8-mL PU foam cubes in batch reactors yielded higher TN removal.     

Coconut water as a medium additive for the production of docosahexaenoic acid (C22:6 n3) by Schizochytrium mangrovei Sk-02

The effect of coconut water (CW) on biomass and docosahexaenoic acid (DHA, C22:6 n3) formation by Schizochytrium mangrovei Sk-02 was studied in a yeast extract-diluted sea water medium. Optimal CW-level was ca. 33% (v/v), resulting in a biomass level of 28 g/l with a DHA-content of 20% (w/w) or 6 g DHA/l, almost 50% higher than in non-supplemented cultures at the same initial sugar level. Study on the growth-promoting effects of coconut water suggested that it could be (partially) mimicked by addition of trace elements; the fatty acids present in CW did not appear to be incorporated or effect fatty acid formation by the organism. CW-addition was also effective in media with other nitrogen sources such as casitone, peptone and tryptone. Its inclusion (at 50% v/v) increased biomass levels two-to-three-fold with concomitant increases in the DHA-level.     

Purification of filamentous bacteriophage M13 by expanded bed anion exchange chromatography

In this paper, we investigated the development of a simplified and rapid primary capture step for the recovery of M13 bacteriophage from particulate-containing feedstock. M13 bacteriophage, carrying an insert, was propagated and subsequently purified by the application of both conventional multiple steps and expanded bed anion exchange chromatography. In the conventional method, precipitation was conducted with PEG/NaCl, and centrifugation was also performed. In the single step expanded bed anion exchange adsorption, UpFront FastLine 20 (20 mm i.d.) from UpFront Chromatography was used as the contactor, while 54 ml (Ho = 15 cm) of STREAMLINE DEAE (rho = 1.2 g/cm3) from Amersham Pharmacia Biotechnology was used as the anion exchanger. The performance of the two methods were evaluated, analysed, and compared. It was demonstrated that the purification of the M13 bacteriophage, using expanded bed anion exchange adsorption, yielded the higher recovery percentage, at 82.86%. The conventional multiple step method yielded the lower recovery percentage, 36.07%. The generic application of this integrated technique has also been assessed.