Recovery of recombinant beta-glucosidase by expanded bed adsorption from Pichia pastoris high-cell-density culture broth

Methanol limited fed-batch cultivation was applied for production of a plant derived beta-glucosidase by Pichia pastoris. The beta-glucosidase was recovered by expanded bed adsorption chromatography applied to the whole culture broth. The new Streamline Direct HST1 adsorbent was compared with Streamline SP. Higher bead density made it possible to operate at two times higher feedstock concentration and at two times higher flow velocity. The higher binding capacity in the conductivity range 0-48 mS cm(-1) of Streamline Direct HST1 might be caused by the more complex interaction of multi-modal ligand in Streamline Direct HST1 compared to the single sulphonyl group in Streamline SP. Harsher elution condition had to be applied for dissociation of beta-glucosidase from Streamline Direct HST1 due to stronger binding interaction. The 5% dynamic binding capacity was 160 times higher for Streamline Direct HST1 compared to Streamline SP. The yield of beta-glucosidase on Streamline Direct HST1 (74%) was significantly higher than on Streamline SP (48%). Furthermore, beta-glucosidase was purified with a factor of 4.1 and concentrated with a factor of 17 on Streamline Direct HST1 while corresponding parameters were half of these values for Streamline SP. Thus, for all investigated parameters Streamline Direct HST1 was a more suitable adsorbent for recovery of recombinant beta-glucosidase from unclarified P. pastoris high-cell-density cultivation broth.     

Recovery of mouse endostatin produced by Pichia pastoris using expanded bed adsorption

Endostatin, a 20 KDa fragment of collagen XVIII, was shown to have an inhibitory effect on angiogenesis and can potentially be used as a tumor growth suppressor. To obtain the amount needed for testing, the protein was successfully cloned and expressed in Pichia pastoris. At the end of the fermentation process, the concentration of the endostatin in the culture was 50 mg per liter, accompanied by 400 gr per liter (wet weight) of biomass. Before the protein can be captured and purified on a packed bed of heparin-Sepharose, the biomass must be removed. Because of the high biomass concentration, conventional biomass removal techniques like centrifugation or filtration are inefficient and cumbersome. Therefore, the expanded-bed adsorption technique was chosen as an alternative approach. An efficient procedure for the initial recovery and purification of the endostatin was developed. The process utilized a cation- exchanger resin instead of a heparin-based affinity resin, because its dynamic capacity was higher, even though it was affected by the high linear flow on the expanded bed. After adjusting the conductivity, pH and biomass concentration, the complete broth was pumped directly on the expanded-bed matrix (Streamline SP XL). Though the yields of protein are similar, the expanded-bed approach is superior to the packed-bed method for several reasons. The expanded-bed process was shorter (only 8 hours compared to 16 hours for the packed bed), it is cheaper, and the product has higher specific activity (29% compared with 18%). Endostatin produced by the expanded-bed adsorption method showed the expected bioactivity and is currently being tested for its potential as a tumor suppressor.     

Antibody capture from corn endosperm extracts by packed bed and expanded bed adsorption

Topical treatments of chronic infections with monoclonal antibodies will require large quantities of antibodies. Because plants have been proven capable of producing multisubunit antibodies and provide for large-scale production, they are likely hosts to enable such applications. Recovery costs must also be low because of the relatively high dosages required. Hence, we have examined the purification of a human secretory antibody from corn endosperm extracts by processing alternatives of packed bed and expanded bed adsorption (EBA). Because of the limited availability of the transgenic corn host, the system was modeled by adding the antibody to extracts of nontransgenic corn endosperm. Complete clarification of a crude extract followed by packed bed adsorption provided antibody product in 75% yield with 2.3-fold purification (with antibody accounting for 24% of total protein). The small size of the packed bed, cation-exchange resin SP-Sepharose FF and the absence of a dense core (present in EBA resins) allowed for more favorable breakthrough performance compared to EBA resins evaluated. Four adsorbents specifically designed for EBA operation, with different physical properties (size and density), chemical properties (ligand), and base matrices were tested: SP-steel core resin (UpFront Chromatography), Streamline SP and Streamline DEAE (Amersham Biosciences), and CM Hyper-Z (BioSepra/Ciphergen Biosystems). Of these, the small hyperdiffuse-style resin from BioSepra had the most favorable adsorption characteristics. However, it could not be utilized with crude feeds due to severe interactions with corn endosperm solids that led to bed collapse. UpFront SP-steel core resin, because of its relatively smaller size and hence lower internal mass transfer resistance, was superior to the Streamline resins and operated successfully with application of a crude corn extract filtered to remove all solids of >44 microm. However, the EBA performance with this adsorbent provided a yield of only 61% and purification factor of 2.1 (with antibody being 22% of total protein). Process simulation showed that capital costs were roughly equal between packed and expanded bed processes, but the EBA design required four times greater operating expenditures. The use of corn endosperm as the starting tissue proved advantageous as the amount of contaminating protein was reduced approximately 80 times compared to corn germ and approximately 600 times compared to canola. Finally, three different inlet designs (mesh, glass beads, and mechanical mixing) were evaluated on the basis of their ability to produce efficient flow distribution as measured by residence time distribution analysis. All three provided adequate distribution (axial mixing was not as limiting as mass transfer to the adsorption process), while resins with different physical properties did not influence flow distribution efficiency values (i.e., Peclet number and HETP) when operated with the same inlet design.     

Partial purification of nattokinase from Bacillus subtilis by expanded bed adsorption

Nattokinase was purified from unclarified Bacillus subtilisculture filtrate using an expanded bed with a purification factor of 8.2 and at a yield of 95%. The optimal pHs for adsorption and elution were 6.0 and 7.0, respectively. The expanded bed route shortened the process time by 8–10 h and increased the yield by 50% when compared with the conventional method.     

In situ butanol recovery from Clostridium acetobutylicum fermentations by expanded bed adsorption

Although butanol is a promising biofuel, its fermentative production suffers from inhibition caused by end product toxicity. The in situ removal of butanol from cultures via expanded bed adsorption offers an effective strategy for mitigating the effects of product toxicity while eliminating the need to clarify cultures via microfiltration. The hydrophobic polymer resin Dowex Optipore L‐493 was found to be both an effective butanol adsorbent and suitable for use in expanded bed adsorption. Recirculation rates through the adsorption column were strongly correlated with and ultimately controlled rates of butanol uptake from the media which, reaching as high as 41.1 g/L h, easily exceed those of its production in a typical fermentation. Vacuum application with vapor collection was found to be an effective means of adsorbent regeneration, with an average of 81% butanol recovery possible, with butanol concentrations in the cold trap reaching as high as 85.8 g/L. Integration of expanded bed adsorption with a fed‐batch Clostridium acetobutylicum ATCC 824 fermentation and its continuous operation for 38.5 h enabled the net production (i.e., in solution and adsorbed) of butanol and total solvent products at up to 27.2 and 40.7 g/L of culture, respectively, representing 2.2‐ and 2.3‐fold improvements over conventional batch culture. While adsorbent biofouling was found to be minimal, further investigation of biofouling in longer‐term studies will provide useful and further insight regarding the robustness of the process strategy. © 2013 American Institute of Chemical Engineers Biotechnol. Prog., 30:68–78, 2014     

LdARL-1 His-tagged recombinant protein: purification by immobilized metal affinity expanded bed adsorption

Previously we have cloned three ADP-ribosylation factor-like (ARL) genes from the parasitic protozoan Leishmania donovani: LdARL-3A and 3B, LdARL-1. LdARL-3A was previously purified as an active native form, which was able to bind GTP in vitro. In this paper, we have performed the production and the purification of Histidine-tagged (His-tagged) LdARL-1 recombinant protein by immobilized metal affinity chromatography (IMAC) using expanded bed adsorption (EBA) technology. This protein was purified with more than 95% purity and could be successfully used for GTP-binding assay.     

A novel system for continuous protein refolding and on-line capture by expanded bed adsorption

A novel two-step protein refolding strategy has been developed, where continuous renaturation-bydilution is followed by direct capture on an expanded bed adsorption (EBA) column. The performance of the overall process was tested on a N-terminally tagged version of human beta2-microglobulin (HAT-hbeta2m) both at analytical, small, and preparative scale. In a single scalable operation, extracted and denatured inclusion body proteins from Escherichia coli were continuously diluted into refolding buffer, using a short pipe reactor, allowing for a defined retention and refolding time, and then fed directly to an EBA column, where the protein was captured, washed, and finally eluted as soluble folded protein. Not only was the eluted protein in a correctly folded state, the purity of the HAThbeta2m was increased from 34% to 94%, and the product was concentrated sevenfold. The yield of the overall process was 45%, and the product loss was primarily a consequence of the refolding reaction rather than the EBA step. Full biological activity of HAT-hbeta2m was demonstrated after removal of the HAT-tag. In contrast to batch refolding, a continuous refolding strategy allows the conditions to be controlled and maintained throughout the process, irrespective of the batch size; i.e., it is readily scalable. Furthermore, the procedure is fast and tolerant toward aggregate formation, a common complication of in vitro protein refolding. In conclusion, this system represents a novel approach to small and preparative scale protein refolding, which should be applicable to many other proteins.     

Removal of poly-histidine fusion tags from recombinant proteins purified by expanded bed adsorption

Enzymatic methods have been used to cleave the C- or N-terminus polyhistidine tags from histidine tagged proteins following expanded bed purification using immobilized metal affinity chromatography (IMAC). This study assesses the use of Factor Xa and a genetically engineered exopeptidase dipeptidyl aminopeptidase-1 (DAPase-1) for the removal of C-terminus and N-terminus polyhistidine tags, respectively. Model proteins consisting of maltose binding protein (MBP) having a C- or N-terminal polyhistidine tag were used. Digestion of the hexahistidine tag of MBP-His(6) by Factor Xa and HT15-MBP by DAPase-1 was successful. The time taken to complete the conversion of MBP-His(6) to MBP was 16 h, as judged by SDS-PAGE and Western blots against anti-His antibody. When the detagged protein was purified using subtractive IMAC, the yield was moderate at 71% although the overall recovery was high at 95%. Likewise, a yield of 79% and a recovery of 97% was obtained when digestion was performed with using "on-column" tag digestion. On-column tag digestion involves cleavage of histidine tag from polyhistidine tagged proteins that are still bound to the IMAC column. Digestion of an N-terminal polyhistidine tag from HT15-MBP (1 mg/mL) by the DAPase-I system was superior to the results obtained with Factor Xa with a higher yield and recovery of 99% and 95%, respectively. The digestion by DAPase-I system was faster and was complete at 5 h as opposed to 16 h for Factor Xa. The detagged MBP proteins were isolated from the digestion mixtures using a simple subtractive IMAC column procedure with the detagged protein appearing in the flowthrough and washing fractions while residual dipeptides and DAPase-I (which was engineered to exhibit a poly-His tail) were adsorbed to the column. FPLC analysis using a MonoS cation exchanger was performed to understand and monitor the progress and time course of DAPase-I digestion of HT15-MBP to MBP. Optimization of process variables such as temperature, protein concentration, and enzyme activity was developed for the DAPase-I digesting system on HT15-MBP to MBP. In short, this study proved that the use of either Factor Xa or DAPase-I for the digestion of polyhistidine tags is simple and efficient and can be carried out under mild reaction conditions.     

Refolding of protein inclusion bodies directly from E. coli homogenate using expanded bed adsorption chromatography

To avoid the intrinsic problem of aggregation associated with the traditional solution-phase refolding process, we proposed a solid-phase refolding method integrated with the expanded bed adsorption chromatography. The model protein was a fusion protein of recombinant human growth hormone and a glutathione S-transferase fragment. It was demonstrated that the inclusion body proteins in the cell homogenate could be directly refolded with higher yield. To verify the applicability of this method, we have tested with success three types of the starting materials, i.e., rhGH monomer, inclusion bodies containing the fusion protein, and the E. coli cell homogenate. This direct refolding process could reduce the number of the renaturation steps required and allow the refolding at a higher concentration, approximately 2 mg fusion protein per ml resin. This revised version was published online in July 2006 with corrections to the Cover Date.     

Purification of recombinant nucleocapsid protein of Newcastle disease virus from unclarified feedstock using expanded bed adsorption chromatography

In the present work, a single-step purification of recombinant nucleocapsid protein (NP) of the Newcastle disease virus (NDV) directly from unclarified feedstock using an expanded bed adsorption chromatography (EBAC) was developed. Streamline 25 column (ID = 25 mm) was used as a contactor and Streamline chelating adsorbent immobilized with Ni2+ ion was used as affinity adsorbent. The dynamic binding capacity of Ni2+ -loaded Streamline chelating adsorbent for the NP protein in unclarified feedstock was found to be 2.94 mg ml(-1) adsorbent at a superficial velocity of 200 cm h(-1). The direct purification of NP protein from unclarified feedstock using expanded bed adsorption has resulted in a 31% adsorption and 9.6% recovery of NP protein. The purity of the NP protein recovered was about 70% and the volume of processing fluid was reduced by a factor of 10. The results of the present study show that the IMA-EBAC developed could be used to combine the clarification, concentration and initial purification steps into a single-step operation.     

Separation of nattokinase fromBacillus subtilis fermentation broth by expanded bed adsorption with mixed-mode adsorbent

Mixed-mode hydrophobic/ionic matrices exhibit a salt-tolerant property for adsorbing target protein from high-ionic strength feedstock, which allows the application of undiluted feedstockvia an expanded bed process. In the present work, a new type of mixed-mode adsorbent designed for expanded bed adsorption, Fastline PRO^®, was challenged for the capture of nattokinase from the high ionic fermentation broth ofBacillus subtilis. Two important factors, pH and ion concentration, were investigated with regard to the performance of nattokinase adsorption. Under initial fermentation broth conditions (pH 6.6 and conductivity of 10 mS/cm) the adsorption capacity of nattokinase with Fastline PRO was high, with a maximum capacity of 5,350 U/mL adsorbent. The elution behaviors were investigated using packed bed adsorption experiments, which demonstrated that the effective desorption of nattokinase could be achieved by effecting a pH of 9.5. The biomass pulse response experiments were carried out in order to evaluate the biomass/adsorbent interactions betweenBacillus subtilis cells and Fastline PRO, and to demonstrate a stable expanded bed in the feedstock containingBacillus subtilis cells. Finally, an EBA process, utilizing mixed-mode Fastline PRO adsorbent, was optimized to capture nattokinase directly from the fermentation broth. The purification factor reached 12.3, thereby demonstrating the advantages of the mixed-mode EBA in enzyme separation.     

Capture of human Fab fragments by expanded bed adsorption with a mixed mode adsorbent

A novel group of mixed mode adsorbents has been developed for purification of monoclonal and polyclonal antibodies from a broad range of raw materials such as hybridoma cell culture, ascites fluid, animal sera, milk, whey and egg yolk. The aim of this study was to determine whether such mixed mode adsorbents were also useful for the recovery of recombinant proteins from microbial feedstocks. This paper describes the performance of one of these adsorbents for expanded bed capture of a human Fab fragment from recombinant E. Coli cell extracts.It is concluded that the mixed mode adsorbent binds the Fab fragment efficiently from crude extracts without any requirement for preconditioning the extract by for example de-salting or dilution. The capacity of the mixed mode adsorbent is approx. 12 mg Fab/ml matrix.The novel mixed mode adsorbent can be useful during production of highly purified Fab fragments as the first step in a purification scheme. In this respect the mixed mode adsorbent is advantageous over alternative commercially available ion-exchange materials which require pre-conditioning of cell extract for Fab' capture. Together with the concentration and clarification effect a significant enrichment of the Fab fragment is obtained in one single high yield operation.     

Direct coupling of expanded bed adsorption with a downstream purification step

In the course of developing a cost-effective, scaleable process for the purification of a recombinant protein from Chinese hamster ovary (CHO) suspension cell culture, we investigated direct capture of this molecule using expanded bed adsorption (EBA). EBA combines clarification, purification, and concentration of the product into a single step. The unclarified bioreactor material was directly applied to a STREAMLINE 25 column containing an affinity STREAMLINE adsorbent. This work focused on simplifying the EBA operations and minimizing the overall processing time by running the EBA column unidirectionally, eluting in the expanded bed mode, and coupling the EBA column directly with ion exchange or hydrophobic interaction chromatography. Unidirectional EBA was clearly a simpler unit operation and did not require the use of specialized equipment. The increase in the elution pool volume was insignificant, especially when the EBA column was eluted directly onto the downstream column. Scale-down was simple and could be automated. Coupling of unidirectional EBA with a downstream purification step reduced processing time, equipment requirements and cost.     

Single-step recovery of ephedrine hydrochloride from raw materials using expanded bed adsorption

Expanded bed adsorption, using a cation resin 001 x 7 Styrene-DVB, was used to recover and purify ephedrine hydrochloride from a powdered herb. The axial liquid-phase dispersion coefficient was about 10(-5) m(2) s(-1) and the recovery yield and purification reached 86% and 22, respectively. Compared with using conventional extraction with dimethylbenzene, this method is safer and also more efficient.     

Large-scale recovery of C-phycocyanin from Spirulina platensis using expanded bed adsorption chromatography

C-phycocyanin was purified on a large scale by a combination of expanded bed adsorption, anion-exchange chromatography and hydroxyapatite chromatography from inferior Spirulina platensis that cannot be used for human consumption. First, phycobiliproteins were extracted by a simple, scaleable method and then were recovered by Phenyl-Sepharose chromatography in an expanded bed column. The purity (the A(620)/A(280) ratio) of C-phycocyanin isolated with STREAMLINE column was up to 2.87, and the yield was as high as 31 mg/g of dried S. platensis. After the first step, we used conventional anion-exchange chromatography for the purification steps, with a yield of 7.7 mg/g of dried S. platensis at a purity greater than 3.2 and with an A(620)/A(650) index higher than 5.0. The fractions from anion-exchange chromatography with a level of purity that did not conform to the above standard were subjected to hydroxyapatite chromatography, with a C-PC yield of 4.45 mg/g of dried S. platensis with a purity greater than 3.2. The protein from both purification methods showed one absolute absorption peak at 620 nm and a fluorescence maximum at 650 nm, which is consistent with the typical spectrum of C-phycocyanin. SDS-PAGE gave two bands corresponding to 21 and 18 kDa. In-gel digestion and LC-ESI-MS showed that the protein is C-phycocyanin.     

Expanded bed adsorption for recovery of patatin from crude potato juice

An expanded bed adsorption process was used to isolate patatin possessing esterase activity, from a crude juice of potato tubers. Patatin is the major storage protein of potato tubers and is released in ample amounts in the processing effluent during starch milling. We employed mixed mode affinity resins, where the binding depends primarily on the pH, and is almost independent of the ionic strength. From a library of mixed mode chemistries involving both charged and hydrophobic functions, we screened for ligands with binding specificity for patatin. The dynamic binding capacity of two high density (1.45–1.5 g ml^-1) patatin-binding agarose-glass resins in response to change of linear velocity (85–230 cm h^-1) was tested in packed (25 ml) and expanded (250 ml) column modes. The column operation included a loading step at low expansion; H/H_o~1.2. Adsorption from crude juice at pH 7.5, retained patatins up to a breakthrough level of 50%. The eluate fraction at pH 3.5, now effectively stripped from the pigments, provided a 2.5-fold enzyme enrichment and produced 4 g protein per cycle. Column productivity was 122 kAU L^-1 h^-1. The study, using potato juice as model feedstock, demonstrated the feasibility of expanded bed-recovery of potentially valuable proteins from plant biomass.This revised version was published online in October 2005 with corrections to the Cover Date.     

Isolation of a recombinant formate dehydrogenase by pseudo-affinity expanded bed adsorption.

Formate dehydrogenase (FDH) is an enzyme of industrial interest, which is recombinantly expressed as an intracellular protein in Escherichia coli. In order to establish an efficient and reliable purification protocol, an expanded bed adsorption (EBA) process was developed, starting from the crude bacterial homogenate. EBA process design was performed with the goal of finding operating conditions which, on one hand, allow efficient adsorption of the target protein and which, on the other hand, support the formation of a perfectly classified fluidised bed (expanded bed) in the crude feed solution. A pseudo-affinity ligand (Procion Red HE3B) was used to bind the FDH with high selectivity and reasonable capacity (maximum equilibrium capacity of 30 U/ml). Additionally, a simplified modelling approach, involving small packed beds for generation of process parameters, was employed for defining the operating conditions during sample application. In combination with extended elution studies, a process was set up, which could be scaled up to 7.5 l of adsorbent volume yielding a total amount of 100,000 U of 94% pure FDH per run. On this scale, 19 l of a benzonase-treated E. coli homogenate of 15% wet-weight (pH 7.5, 9 mS/cm conductivity) were loaded to the pseudo-affinity adsorbent (0.25 m sed. bed height, 5 x 10(-4) m/s fluid velocity). After a series of two wash steps, a particle-free eluate pool was obtained with 85% yield of FDH. This excellently demonstrates the suitability of expanded bed adsorption for efficient isolation of proteins by combining solid-liquid separation with adsorptive purification in a single unit operation.     

Pilot scale recovery of monoclonal antibodies by expanded bed ion exchange adsorption

The aim of the investigations was to estimate the scale up properties of an efficient chromatographic first capture step for the recovery of murine IgG₁ from undiluted and unclarified hybridoma cell culture broth using an ion exchange matrix in expanded bed mode. The tested new sulfopropyl-based ion exchange matrix (Streamline^TM SP XL, Amersham Pharmacia Biotech) stands out due to its enhanced capacity compared to its precursor (Streamline^TM SP). Defining the working pH in preliminary electrophoretic analyses (titration curve, SDS-PAGE) and small-scaled chromatographic binding studies showed, that the optimal value for the IgG purification was pH 4.6, where a co-chromatography of the medium supplement albumin (500 mg l^-1, pI = 4.8) could not be avoided. Further scouting experiments dealt with the dynamic capacity of the matrix, which was evaluated by frontal adsorption analysis. In packed bed mode no break-through of the target protein was achieved even after 6.5 mg IgG per ml matrix were applied. These results could not be reproduced in expanded bed mode with cell-free supernatant, where the dynamic capacity was found to be only 1.5 mg IgG/ml SP XL. Processing cell-containing broth resulted in an additional decrease of the value down to 0.5 mg ml^-1, presumably caused by the remarkable biomass adsorption to the matrix. The search for the reasons led to the examination of the hydrodynamic conditions. Buffer experiments with a tracer substance (acetone) pointed out, that the flow in expanded bed was significantly more influenced by back-mixing effects and channel formations than in packed bed. These effects could be compensated with an enhanced viscosity of the liquid phase, which was achieved by the addition of glucose. As a result of the improved hydrodynamic conditions in the expanded bed, the dynamic capacity could be increased from 0.5 to more than 4.5 mg IgG/ml matrix for the processing of cell culture broth with 400 mM glucose. Finally, the scale up from a Streamline^TM 25 to a Streamline^TM 200 column was performed under conditions, which proved to be optimal: 100 L of unclarified hybridoma broth were concentrated with a binding rate of 95% in less than 3.5 hours. Loading the column no break-through of the target protein was achieved. However, the eluate still contained debris and cells, which points out the major disadvantage of the method: the biomass attachment to the matrix.     

Purification by expanded bed adsorption and characterization of an alpha-amylases FORILASE NTL from A. niger

In this work the purification and biochemistry characterization of alpha-amylases from Aspergillus niger (FORILASE NTL) were studied. The effects of expansion degree of resin bed on enzyme purification by expanded bed adsorption (EBA) have also been studied. Residence time distributions (RTD) studies were done to achieve the optimal conditions of the amylases recovery on ion-exchange resin, and glucose solution was used as a new tracer. Results showed that height equivalent of the theoretical plates (HETP), axial dispersion and the Prandt number increased with bed height, bed voidage and linear velocity. The adsorption capacity of alpha-amylases, on the resin, increased with bed height and the best condition was at four-expansion degree. alpha-Amylase characterization showed that this enzyme has high affinity with soluble starch, good hydrolysis potential and molecular weight of 116 kDa.     

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.