Analysis of low molecular weight plasma proteins using ultrafiltration and large gel two‐dimensional electrophoresis

In this study, various solvent systems were applied to obtain a high and consistent recovery rate of low molecular weight plasma proteins (LMPP) from human plasma. A buffer system containing 7 M urea, 2 M thiourea, 25 mM NH₄HCO₃ + 20% ACN (pH 8.2) produced the highest recovery rate of LMPP. To validate the recovery of cut off membrane (COM) obtained using the urea buffer system, 27 different 30 kDa COMs were used to prepare the LMPP sample which were then subjected to 1‐D SDS‐PAGE. Statistical analysis showed that the buffer system with COM produced a consistent the recovery of LMPP. In addition, 2‐DE analysis was also conducted to determine the relative intensity of each protein spot. When molecular weight ranges over 30 kDa and under 30 kDa were evaluated, 953 and 587 protein spots were observed in the gels, respectively, resulting in a total of 1540 protein spots being resolved. Identification of the major proteins were then performed using a nano‐LC/MS system comprised of an HPLC system and an ESI‐quadrupole IT MS equipped with a nano‐ESI source.     

Purification of a recombinant protein expressed in yeast: optimization of analytical and preparative chromatography

The industrial production of recombinant proteins requires control of both fermentation and purification steps. For the serodiagnosis of toxoplasmosis, the main antigen is a membrane protein of 30 kDa (P30). The P30 gene was cloned and expressed in Schizosaccharomyces pombe at 0.7 μg/ml in culture medium. Batch fermentation was optimized by the specific choice of peptones, which enabled optimum growth and protein expression without reducing the efficacy of the purification step. Analytical purification was then carried out using cation-exchange chromatography. For larger volumes, scaling up was performed on expanded mode by using a Streamline system (Pharmacia). This purification step allowed us to obtain a 67.5% recovery with a purification factor greater than 27-fold. Expanded bed adsorption technology is a convenient and effective technique for protein capture directly from feedstock, and the eluted fraction is ready for a second affinity chromatography step. This second step is performed with a yield of 40% and provides a final purification factor of 2000-fold.     

Extraction of protein from distiller’s grain

We have investigated the feasibility of extracting the oil and protein from distiller’s grain (DG) to obtain a higher-valued protein-rich product and a carbohydrate-rich residue better suited for conversion to fermentable sugars. Protein extractions based on aqueous ethanol, alkaline-ethanol, and aqueous enzyme treatments were compared. Three of the methods extracted a significant amount of the protein from dried, defatted DG (DDDG). The enzymatic extraction decreased the crude protein content in the solid phase for both milled and unmilled DDDG from 41% (dry weight) to approximately 10% (dry weight) protein in the residual solid; this corresponded to extraction of 90% of the protein in the original DDDG. The alkaline-ethanol extraction was similarly effective for milled but not unmilled DG. Simple extraction with alcohol was not as effective. Amino acid analysis of each protein extract was consistent with it consisting mainly of zeins. For the protease-assisted extractions, 95% the proteins were in the form of peptides smaller than 10 kDa.     

Integrated bioprocesses

Integrated bioprocesses have been developed to optimise yield and cost-effectiveness of production of low and high molecular weight molecules. Low molecular weight products are removed from the cultivation medium with in situ extraction, in situ adsorption or crystallisation to avoid product inhibition. One-pot processes are being developed to replace two-stage reactions. Recent developments in the integrated purification of high molecular weight products focus mainly on the integration of solid/liquid separation and initial product recovery such as expanded bed adsorption or extraction in aqueous two-phase systems. Additionally, new approaches for a more efficient processing of inclusion bodies have been developed.     

The effects of membrane filters used in biopharmaceutical processes on the concentration and composition of polysorbate 20

Polysorbate 20 (PS‐20) is often included in the formulation for therapeutic proteins to reduce protein aggregation and surface adsorption. During the production process of therapeutic proteins, various membrane filters are used to filter product pools containing PS‐20. The purpose of this study is to quantify the effects of these membrane filtration processes on the concentration and composition of PS‐20. A quantitative understanding of this process provides the knowledge base for better controlling the consistency of formulation excipients in drug products. PS‐20 solutions (without protein) were filtered through either 0.2 µm sterilizing filters or membrane filters with 30 kDa MWCO. The concentration of PS‐20 was measured by a mixed‐mode chromatography method and a nuclear magnetic resonance spectroscopy (NMR) assay. The composition of PS‐20 was characterized by ¹H‐NMR and a reverse‐phase chromatography method. Non‐specific adsorption of PS‐20 on both the sterilizing filter and 30 kDa MWCO membrane filter was quantified. Composition of PS‐20 was altered after 30 kDa MWCO membrane filtration, possibly because the different interactions between heterogeneous PS‐20 components and the 30 kDa MWCO membrane were not uniform. As a result, the retentate after the 30 kDa MWCO membrane filtration step contains no POE sorbitan and increased amount of POE sorbitan di‐esters and tri‐esters. © 2013 American Institute of Chemical Engineers Biotechnol. Prog., 29:1503–1511, 2013     

Purification and characterisation of gelonin from seeds of Gelonium multiflorum

Gelonin, a ribosome-inactivating protein has been isolated from the seeds of Gelonium multifluorum of Euphorbiaceae family by two methods and the results are compared. In method-I conventional aqueous extraction, cation-exchange and gel-filtration chromatography has been used. In method-II S-Sepharose fast flow gel has been used to purify the proteins from the seed extract, followed by ammonium sulfate fractionation, cation-exchange and gel-filtration chromatography. Extensive physico-chemical and immunological characterizations show that molecular weight of gelonin as determined by gel-filtration chromatography and SDS-PAGE is approximately 30 kDa. The non-proteinous material which binds to CMC-gel in association with gelonin in method-I is substantially removed when gelonin is purified by method-II. Cation exchange, G-100 chromatography, RP-HPLC and SDS-PAGE show that method-II yields 50% more purified gelonin when compared to the yield by method-I. The immunoreactivity of gelonin obtained by methods I and II vary from 22-26% and 50-66% respectively and the ribosome-inactivating property vary from 46-56% and 70-87% respectively.     

Characterization of cryogel monoliths for extraction of minor proteins from milk by cation exchange

Extraction and purification of high‐value minor proteins directly from milk without pre‐treatment is a challenge for the dairy industry. Pre‐treatment of milk before extraction of proteins by conventional packed‐bed chromatography is usually necessary to prevent column blockage but it requires several steps that result in significant loss of yield and activity for many minor proteins. In this paper, we demonstrate that it is possible to pass 40–50 column volumes of various milk samples (raw whole milk, homogenized milk, skim milk and acid whey) through a 5 mL cryogel chromatographic column at 550 cm/h without exceeding its pressure limits if the processing temperature is maintained above 35°C. The dynamic binding capacity obtained for the cryogel matrix (2.1 mg/mL) was similar to that of the binding capacity (2.01 mg/mL) at equilibrium with 0.1 mg/mL of lactoferrin in the feed samples. The cryogel column selectively binds lactoferrin and lactoperoxidase with only minor leakage in flowthrough fractions. Lactoferrin was recovered from elution fractions with a yield of over 85% and a purity of more than 90%. These results, together with the ease of manufacture, low cost and versatile surface chemistry of cryogels suggest that they may be a good alternative to packed‐bed chromatography for direct capture of proteins from milk. Biotechnol. Bioeng. 2009;103: 1155–1163. © 2009 Wiley Periodicals, Inc.     

Soy protein recovery in a solvent-free process using continuous liquid-solid circulating fluidized bed ion exchanger

Soy protein concentrates and soy protein isolates act as ingredients in bakery, meat and dairy products, baby formulas, starting materials for spun textured vegetable products, and other nutritional supplements. In this study, the effectiveness of a liquid-solid circulating fluidized bed (LSCFB) ion exchanger is demonstrated for the recovery of soluble soy proteins from full fat and defatted soy flour. Under steady-state operating conditions, about 50% of the proteins could be recovered from the feed streams entering the ion exchanger. The LSCFB was shown to be a promising system for the recovery of soy protein from both defatted and full fat soy flour solutions. As the ion exchange process captures dissolved proteins, the system may offer a less damaging form of processing compared with the acid precipitation process where soy protein aggregates form and functionality is affected. In addition, the LSCFB allows simultaneous adsorption and desorption of the proteins allowing for a continuous operation. No prefiltration of feed containing suspended particles is required as well, because fluidization is used in place of packed bed technology to improve on current ion exchange processes.     

纳米器件对叶蛋白提取的影响

从植物中提取蛋白质包括机械破碎和离心等一系列步骤,蛋白质在提取液中的溶解度直接影响蛋白提取率和产量.结果表明,用纳米器件处理过的提取液能显著提高叶蛋白的提取率,提升幅度为10％-30％.利用正交试验研究不同提取条件下纳米器件对蛋白可溶性的影响,结果显示浸泡时长(纳米器件浸泡在提取液中的时长)是最关键的已测因素.此外,植物样品的破碎程度也是影响叶蛋白提取率的关键因素之一.     

A shortcut method for evaluation of protein deposition onto the membrane surface in crossflow ultrafiltration

In this study, a procedure for quantifying the surface deposition of proteins in crossflow ultrafiltration has been developed. The procedure consists of determining the protein adsorption behavior onto the membrane surface from a few dynamic measurements performed in a nonfiltration and a filtration mode, and evaluating the concentration polarization (CP) layer thickness based on the adsorption data. To predict the interdependence between the protein adsorption and CP, a simplified mathematical model has been formulated. The model was used to assess the protein adsorption and thus yield reduction in the ultrafiltration process at different protein concentration in the solution. As a case study, ultrafiltration of aqueous solutions of BSA and lysozyme (LYZ) was examined on a polyethersulfone membrane with the molecular weight cutoff of 10 or 100 kDa. The protein concentration in the solutions varied within a relatively low concentration range, i.e. below 10 mg mL^?1, characteristic for solvent exchange between sequential operations of protein purification by chromatography and extraction. Both proteins markedly differed in the mechanism of surface deposition; for BSA hydrophobic interactions were suggested to be dominant, whereas in case of LYZ electrostatic interactions contributed the most to the deposition mechanism. The effect of additives of the protein solutions, i.e. inorganic salts, PEG, and urea depended on the adsorption mechanism and was also specific for each protein. Nevertheless, the proposed procedure performed well in the evaluation of surface deposition and yield reduction, regardless of the protein type and its solvent environment.     

Characterization of vitellin,egg-specific protein and 30 kDa protein from Bombyx eggs,and their fates during oogenesis and embryogenesis

Three major yolk proteins, vitellin, egg-specific protein and 30 kDa proteins, were purified from the same extracts of Bombyx mori eggs by high-performance liquid chromatography on a molecular sieving column. Each preparation was judged to be homogeneous by polyacrylamide gel electrophoresis. The subunit structure was estimated to be as follows: vitellin is a tetramer with a molecular mass of 420 kDa, consisting of two heavy subunits (178 kDa) and two light subunits (43 kDa); egg-specific protein is a trimer (225 kDa) of two heavy subunits (72 kDa) and one light subunit (64 kDa); 30 kDa proteins are a mixture of three monomers (1, 2 and 3) consisting of respective subunit molecular masses of 32.0, 31.0 and 29.5 kDa. The three yolk proteins contained the usual amino acids together with various lipids and carbohydrates. Antisera to each protein did not cross-react. The titration of vitellin, egg-specific protein and 30 kDa proteins on rocket immunoelectrophoresis showed a differential accumulation pattern during the course of oogenesis. In newly laid eggs, vitellin, egg-specific protein and 30 kDa proteins accounted for approx. 40%, 25% and 35%, respectively, in weight. The eggs developed in male hosts after implantation of ovary discs were deficient in vitellin but contained egg-specific protein and 30 kDa proteins at comparable levels to the normal female eggs. During embryogenesis, egg-specific protein was rapidly and completely utilized. Approx. 35% vitellin and 50% 30 kDa proteins remained unused and were carried over to the hatched larvae. Such accumulation and utilization of yolk proteins are correlated with the fates of the proteins during oogenesis and embryogenesis of B. mori.     

Reevaluation of the electrophoretic migration behavior of soluble globular proteins in the native and detergent-denatured states in polyacrylamide gels

Although sodium dodecyl sulfate (SDS)-polyacrylamide gel electrophoresis is widely used for estimating molecular masses of proteins, considerable uncertainty still exists both about the structure of SDS-protein complexes and about their mechanism of electrophoretic migration. In this study, soluble globular proteins, with masses of 14-200 kDa, were heat-denatured in the presence of SDS and their relative total molecular volume and net charge were estimated from Ferguson plots of electrophoretic mobility vs acrylamide concentration. Native globular protein served as standards for overall molecular size and effective radii. Results revealed at least two independent electrophoretic migration mechanisms for the SDS-protein complexes: (i) for proteins in the 14-65 kDa range at <15% acrylamide, linear Ferguson plots suggested that they migrated ideally and that their effective radii could be estimated in this manner: (ii) concave plots at higher gel concentrations, and for complexes derived from larger proteins, indicated that migration in these cases could be described by reptation theory. Migration of the large proteins at lower gel concentrations and small proteins at higher gel concentrations was not well described by either theory, representing intermediate behavior not described by these mechanisms. These data support models in which all but the smallest SDS-protein complexes adopt a necklace-like structure in which spherical micelles are distributed along the unfolded polypeptide chain. Possible relations to recent alternative models of gel electrophoresis are also discussed.     

Purification of the two major proteins from whey concentrate using a cation‐exchange selective adsorption process

The packed‐bed adsorption and elution of aqueous solutions of whey concentrate powders were investigated at pH 3.7 using a 5‐mL SP Sepharose FF column to separate and isolate two major proteins namely, α‐lactalbumin (ALA) and β‐lactoglobulin (BLG) from these solutions. ALA displaced and eluted BLG from the column in a pure form. Pure ALA could then be eluted with good recovery. A novel consecutive two‐stage separation process was developed to separate ALA and BLG from whey concentrate mixtures. Almost all of the BLG in the feed was recovered, with 78% being recovered at 95% purity and a further 20% at 86% purity. In addition, 67% of ALA was recovered, 48% at 54% purity and 19% at 60% purity. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2010     

Enzymatic pre‐treatment of microalgae cells for enhanced extraction of proteins

Crude proteins and pigments were extracted from different microalgae strains, both marine and freshwater. The effectiveness of enzymatic pre‐treatment prior to protein extraction was evaluated and compared to conventional techniques, including ultrasonication and high‐pressure water extraction. Enzymatic pre‐treatment was chosen as it could be carried out at mild shear conditions and does not subject the proteins to high temperatures, as with the ultrasonication approach. Using enzymatic pre‐treatment, the extracted proteins yields of all tested microalgae strains were approximately 0.7 mg per mg of dry cell weight. These values were comparable to those achieved using a commercial lytic kit. Ultrasonication was not very effective for proteins extraction from Chlorella sp., and the extracted proteins yields did not exceed 0.4 mg per mg of dry cell weight. For other strains, similar yields were achieved by both treatment methods. The time‐course effect of enzymatic incubation on the proteins extraction efficiency was more evident using laccase compared to lysozyme, which suggested that the former enzyme has a slower rate of cell disruption. The crude extracted proteins were fractionated using an ion exchange resin and were analyzed by the electrophoresis technique. They were further tested for their antioxidant activity, the highest of which was about 60% from Nannochloropsis sp. The total phenolic contents in the selected strains were also determined, with Chlorella sp. showing the highest content reaching 17 mg/g. Lysozyme was also found to enhance the extraction of pigments, with Chlorella sp. showing the highest pigments contents of 16.02, 4.59 and 5.22 mg/g of chlorophyll a, chlorophyll b and total carotenoids, respectively.     

Mismatch DNA recognition protein from an extremely thermophilic bacterium, Thermus thermophilus HB8.

The mutS gene, implicated in DNA mismatch repair, was cloned from an extremely thermophilic bacterium, Thermus thermophilus HB8. Its nucleotide sequence encoded a 819-amino acid protein with a molecular mass of 91.4 kDa. Its predicted amino acid sequence showed 56 and 39% homology with Escherichia coli MutS and human hMsh2 proteins, respectively. The T.thermophilus mutS gene complemented the hypermutability of the E.coli mutS mutant, suggesting that T.thermophilus MutS protein was active in E.coli and could interact with E.coli MutL and/or MutH proteins. The T.thermophilus mutS gene product was overproduced in E.coli and then purified to homogeneity. Its molecular mass was estimated to be 91 kDa by SDS-PAGE but approx. 330 kDa by size-exclusion chromatography, suggesting that T.thermophilus MutS protein was a tetramer in its native state. Circular dichroic measurements indicated that this protein had an alpha-helical content of approx. 50%, and that it was stable between pH 1.5 and 12 at 25 degree C and was stable up to 80 degree C at neutral pH. Thermus thermophilus MutS protein hydrolyzed ATP to ADP and Pi, and its activity was maximal at 80 degrees C. The kinetic parameters of the ATPase activity at 65 degrees C were Km = 130 microM and Kcat = 0.11 s(-1). Thermus thermophilus MutS protein bound specifically with G-T mismatched DNA even at 60 degrees C.     

Scale‐up of hydrophobin‐assisted recombinant protein production in tobacco BY‐2 suspension cells

Plant suspension cell cultures are emerging as an alternative to mammalian cells for production of complex recombinant proteins. Plant cell cultures provide low production cost, intrinsic safety and adherence to current regulations, but low yields and costly purification technology hinder their commercialization. Fungal hydrophobins have been utilized as fusion tags to improve yields and facilitate efficient low‐cost purification by surfactant‐based aqueous two‐phase separation (ATPS) in plant, fungal and insect cells. In this work, we report the utilization of hydrophobin fusion technology in tobacco bright yellow 2 (BY‐2) suspension cell platform and the establishment of pilot‐scale propagation and downstream processing including first‐step purification by ATPS. Green fluorescent protein‐hydrophobin fusion (GFP‐HFBI) induced the formation of protein bodies in tobacco suspension cells, thus encapsulating the fusion protein into discrete compartments. Cultivation of the BY‐2 suspension cells was scaled up in standard stirred tank bioreactors up to 600 L production volume, with no apparent change in growth kinetics. Subsequently, ATPS was applied to selectively capture the GFP‐HFBI product from crude cell lysate, resulting in threefold concentration, good purity and up to 60% recovery. The ATPS was scaled up to 20 L volume, without loss off efficiency. This study provides the first proof of concept for large‐scale hydrophobin‐assisted production of recombinant proteins in tobacco BY‐2 cell suspensions.     

Reverse micelles in protein separation: the use of silica for the back-transfer process

In order to use reverse micellar solutions successfully for the separation of proteins, good methods are needed to recover the biomolecules into an aqueous environment after solubilization into organic micellar media. Usually the recovery is accomplished by equilibrating the protein-loaded reverse micellar solution with a water phase containing an appropriate salt (back-transfer). In this article we describe an alternative "back extraction" procedure which is based on the addition of silica to the protein-containing reverse micellar solution. In this way, the water is stripped from the reverse micellar solution. [i.e., bis(2-ethylhexyl) sodium sulfosuccinate (AOT)/isooctane/water] and the proteins adsorb to the silica particles. The adsorption process is shown to be practically quantitative. The subsequent recovery of the proteins form the silica into an aqueous solution turns out to be most efficient at alkaline pH (pH 8); 60-80 of the total protein (alpha-chymotrypsin or trypsin) could be recovered. The specific enzyme activity at the end of the whole cycle can be as high as 80-100%. The procedure is applied also for the back extraction from micellar solutions in which, instead of AOT, a biocompatible surfactant such as a synthetic short-chain lecithin was used. It is shown that the recovery of a alpha-chymotrypsin and trypsin is also achievable under these conditions in quite good yield and under good maintenance of the enzyme's catalytic activity. (c) 1993 John Wiley & Sons, Inc.     

Surimi wash water treatment for protein recovery: effect of chitosan-alginate complex concentration and treatment time on protein adsorption

Chitosan (Chi), a protein recovery agent for the treatment of aqueous food processing streams, appears to work by mechanical entrapment and electrostatic interaction of chitosan amino groups with anionic groups on proteins. Chitosan effectiveness for recovering soluble proteins from surimi wash water (SWW) is increased by complexation with alginate (Alg) and by adjusting complex concentration and treatment time. Flocculation at 20 degrees C with Chi-Alg at a 0.2 mixing ratio added as 20, 40, 100 and 150 mg/L SWW was aided by 5 min agitation at 130 rpm and then held at the same temperature for 30 min, 1 and 24 h. Turbidity measurements, protein determinations and qualitative FTIR analysis confirmed SWW protein adsorption which depended on Chi-Alg concentration and reaction time while turbidity reduction was affected by concentration only. No differences (p < 0.05) in protein adsorption were found between 1 and 24 h. Using 100 mg Chi-Alg complex/L SWW for 1 h achieved 83% protein adsorption and 97% turbidity reduction.     

Cell‐free production of a therapeutic protein: Expression,purification, and characterization of recombinant streptokinase using a CHO lysate

The use of cell‐free systems to produce recombinant proteins has grown rapidly over the past decade. In particular, cell‐free protein synthesis (CFPS) systems based on mammalian cells provide alternative methods for the production of many proteins, including those that contain disulfide bonds, glycosylation, and complex structures such as monoclonal antibodies. In the present study, we show robust production of turbo green fluorescent protein (tGFP) and streptokinase in a cell‐free system using instrumented mini‐bioreactors for highly reproducible protein production. We achieved recombinant protein production (～600 μg/ml of tGFP and 500 μg/ml streptokinase) in 2.5 hr of expression time, comparable to previously reported yields for cell‐free protein expression. Also, we demonstrate the use of two different affinity tags for product capture and compare those to a tag‐free self‐cleaving intein capture technology. The intein purification method provided a product recovery of 86%, compared with 52% for conventionally tagged proteins, while resulting in a 30% increase in total units of activity of purified recombinant streptokinase compared with conventionally tagged proteins. These promising beneficial features combined with the intein technology makes feasible the development of dose‐level production of therapeutic proteins at the point‐of‐care.     

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.