Development of a polishing step using a hydrophobic interaction membrane adsorber with a PER.C6®‐derived recombinant antibody

Membrane chromatography has already proven to be a powerful alternative to polishing columns in flow‐through mode for contaminant removal. As flow‐through utilization has expanded, membrane chromatography applications have included the capturing of large molecules, including proteins such as IgGs. Such bind‐and‐elute applications imply the demand for high binding capacity and larger membrane surface areas as compared to flow‐through applications. Given these considerations, a new Sartobind Phenyl? membrane adsorber was developed for large‐scale purification of biomolecules based on hydrophobic interaction chromatography (HIC) principles. The new hydrophobic membrane adsorber combines the advantages of membrane chromatography—virtually no diffusion limitation and shorter processing time—with high binding capacity for proteins comparable to that of conventional HIC resins as well as excellent resolution. Results from these studies confirmed the capability of HIC membrane adsorber to purify therapeutic proteins with high dynamic binding capacities in the range of 20 mg‐MAb/cm³‐membrane and excellent impurity reduction. In addition the HIC phenyl membrane adsorber can operate at five‐ to ten‐fold lower residence time when compared to column chromatography. A bind/elute purification step using the HIC membrane adsorber was developed for a recombinant monoclonal antibody produced using the PER.C6® cell line. Loading and elution conditions were optimized using statistical design of experiments. Scale‐up is further discussed, and the performance of the membrane adsorber is compared to a traditional HIC resin used in column chromatography. Biotechnol. Bioeng. 2010; 105: 296–305. © 2009 Wiley Periodicals, Inc.     

Considerations on the flow configuration of membrane chromatography devices for the purification of human basic fibroblast growth factor from crude lysates

Membrane chromatography possesses numerous advantages such as operation at high flow rates, low back pressure, ease of handling and scale up, which make the membrane adsorber process a viable alternative to conventional packed column chromatography. A purification process for the isolation of human recombinant basic fibroblast growth factor (FGF‐2) based on membrane chromatography was investigated using devices with different flow configurations. In the first process, the FGF‐2 capture step was performed with an axial flow device, while the alternative method achieved direct capture of FGF‐2 from unclarified cell lysate with a tangential flow device. In both processes, FGF‐2 purities exceeded 82% and the purified cytokine displayed high biological activity. Binding capacity (BC) from fermentation broth of the axial flow device was 28 mg/mL. This was 50% higher than the BC obtained with the tangential flow device under particle‐free supernatant conditions (18 mg/mL) and 150% higher compared to the BC achieved with unclarified cell lysate (11 mg/mL). While membrane chromatography in tangential flow mode omits clarification and thus reduces the number of stages in the downstream process, it displays lower peak resolution and leads to a lower overall process yield.     

Fast and efficient protein purification using membrane adsorber systems

The purification of proteins from complex cell culture samples is an essential step in proteomic research. Traditional chromatographic methods often require several steps resulting in time consuming and costly procedures. In contrast, protein purification via membrane adsorbers offers the advantage of fast and gentle but still effective isolation. In this work, we present a new method for purification of proteins from crude cell extracts via membrane adsorber based devices. This isolation procedure utilises the membranes favourable pore structure allowing high flow rates without causing high back pressure. Therefore, shear stress to fragile structures is avoided. In addition, mass transfer takes place through convection rather than diffusion, thus allowing very rapid separation processes. Based on this membrane adsorber technology the separation of two model proteins, human serum albumin (HSA) and immungluboline G (IgG) is shown. The isolation of human growth hormone (hGH) from chinese hamster ovary (CHO) cell culture supernatant was performed using a cation exchange membrane. The isolation of the enzyme penicillin acylase from the crude Escherichia coli supernatant was achieved using an anion exchange spin column within one step at a considerable purity. In summary, the membrane adsorber devices have proven to be suitable tools for the purification of proteins from different complex cell culture samples.     

Innovative modular membrane adsorber system for high-throughput downstream screening for protein purification

To develop the most efficient strategy for the purification of proteins, two types of adsorber membrane devices with different functionalities were designed and tested: 8-strips and single spin columns. The most suitable type of membrane adsorber and the optimal chromatographic loading/elution conditions for several target proteins from different biological matrices could be determined simultaneously in microliter scale. Ion exchange (IEX), metal chelate (MC), and Concanavalin A (Con A) modified membrane types were tested in the devices. Bovine serum albumin (BSA) and lysozyme were used as model proteins for investigations of the binding capacity and protein recovery percentage of the 8-strip anion exchange and the cation exchange membrane. The isolation of His(6)-tagged proteins, Bgl-His and GFP-His from fermentation broth and lysate, respectively, was performed using an 8-strip metal chelate affinity membrane loaded with different metal ions. Separation behavior of a ternary protein mixture (BSA, lysozyme, and Bgl-His) was studied in 8-strips IEX and metal chelate membrane chromatography. The Con A affinity devices were developed on the basis of metal chelate membrane spin columns loaded with Cu(2+) ions and investigated using glucose oxidase (GOD) as model protein. In summary, the advantages of the membrane adsorber technology, such as fast processing and easy scale-up, were utilized. The devices made it possible to load the membrane directly with preclarified fermentation broth or cell lysate and separate the protein of interest often in a single step.     

Downstream processing of high chain length polysialic acid using membrane adsorbers and clay minerals for application in tissue engineering

Polysialic acid (polySia) is a carbohydrate polymer of varying chain length. It is a promising scaffold material for tissue engineering. In this work, high chain length polySia was produced by an Escherichia coli K1 strain in a 10‐L bioreactor in batch and fed‐batch mode, respectively. A new downstream process for polySia is presented, based on membrane adsorber technology and use of inorganic anion exchanger. These methods enable the replacement of precipitation steps, such as acetone, cetavlon, and ethanol precipitation of the already established purification process. The purification process was simplified, while process efficiency and product qualities were improved. The overall yield of polySia from a 10‐L batch cultivation process was 61% and for 10‐L fed‐batch cultivation process the yield was 40% with an overall purity of 98%. The endotoxin content was determined to be negligible (14 EU mg^?1). The main advantage of this new downstream process is that polySia with high chain length of more than 130 degree of polymerization can be obtained. In fed‐batch cultivation, chain lengths up to 160 degree of polymerization were obtained.     

Bioactive components of ovine and caprine cheese whey

Cheese whey, also known as sweet whey, is a by-product of cheese-making that contains many valuable constituents. Among them, whey proteins stand out for their high nutritional value in terms of biological value and composition in essential amino acids. In recent years, the increasing demand for caprine and ovine cheeses has produced important amounts of whey from these species, boosting research on the biological activities of its constituent proteins. Different bioactivities have been associated to these proteins, among them antihypertensive, antimicrobial, opioid, antioxidant and immunomodulant activity being the most studied. Although biological activities are present in the intact proteins, in many cases whey proteins act as precursors of bioactive peptides that are released from the hydrolysis of these proteins with different enzymes. This review presents an overview of the different biological activities described for caprine and ovine cheese whey proteins as well as for other whey components such as lactose, oligosaccharides or minerals.     

Synthesis of membrane proteins in eukaryotic cell‐free systems

Cell‐free protein synthesis (CFPS) is a valuable method for the fast expression of difficult‐to‐express proteins as well as posttranslationally modified proteins. Since cell‐free systems circumvent possible cytotoxic effects caused by protein overexpression in living cells, they significantly enlarge the scale and variety of proteins that can be characterized. We demonstrate the high potential of eukaryotic CFPS to express various types of membrane proteins covering a broad range of structurally and functionally diverse proteins. Our eukaryotic cell‐free translation systems are capable to provide high molecular weight membrane proteins, fluorescent‐labeled membrane proteins, as well as posttranslationally modified proteins for further downstream analysis.     

A nonchromatographic process for purification of secretory immunoglobulins from caprine whey

Secretory immunoglobulins are an important antibody class being primarily responsible for immunoprotection of mucosal surfaces. A simple, non‐chromatographic purification process for secretory immunoglobulins from caprine whey was developed. In the first process step whey was concentrated 30–40‐fold on a 500 kDa membrane, thereby increasing the purity from 3% to 15%. The second step consisted of a fractionated PEG precipitation, in which high molecular weight impurities were removed first and in the second stage the secretory immunoglobulins were precipitated, leaving a majority of the low molecular weight proteins in solution. The re‐dissolved secretory immunoglobulin fraction had a purity of 43% which could then be increased to 72% by diafiltration at a volume exchange factor of 10. Further increase of purity was only possible at the expense of very high buffer consumption. If diafiltration was performed directly after ultrafiltration, followed by precipitation, the yield was higher but purity was only 54%. Overall, filtration performance was characterized by high concentration polarization, therefore process conditions were set to low trans‐membrane pressure and moderate protein concentration. As such purity and to a lesser extent throughput were the major objectives rather than yield, since whey, as a by‐product of the dairy industry, is a cheap raw material of almost unlimited supply. Ultra‐/diafiltration performance was described well by correlations using dimensionless numbers. Compared with a theoretical model (Graetz/Leveque solution) the flux was slightly overestimated. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:642–653, 2017     

Purification of kappa-casien glycomacropeptide from sweet whey with undetectable level of phenylalanine

Glycomacropeptide (GMP) found in sweet whey is a biologically active compound released from kappa-casein by the action of chymosin during cheese making. This study was undertaken to purify GMP from sweet whey as a research chemical on a laboratory scale. Glycomacropeptide was isolated from proteins and other non-GMP compounds by deproteinization with trichloroacetic acid and gel chromatography on Sephacryl S-200. The purified GMP accounted for 0.12% of dry sweet whey powder and contained 107.0, 50.9, 61.2 and 4.3 microg, respectively, of sialic acid, galactose, galactosamine and phosphorus per mg dry weight. The GMP was of high purity, with its amino acid composition showing undetectable levels of phenylalanine, tyrosine and arginine, the amino acids that do not occur in bovine GMP. On gel electrophoresis, the GMP showed a single broad band with an average mobility faster than that of carbonic anhydrase (molecular weight = 31 kDa). The purified GMP may be used as a standard glycopeptide in chromatography and electrophoresis and may also be used to test various known or unknown properties and biological activities of this compound.     

Isolation of a protein from the plasma membrane of adrenal medulla which binds to secretory vesicles.

Solubilized proteins of the plasma membrane of bovine adrenal medulla were fractionated on the basis of their affinity for secretory vesicles. The isolation procedure included preparation of a highly purified fraction of plasma membranes, its solubilization in detergent, and application to a column prepared from glutaraldehyde-fixed chromaffin granules. Using this technique, one major polypeptide (80% of the material bound) was isolated. This protein has been shown to originate from the plasma membrane and has no affinity for fixed bovine adrenal medullary mitochondria or lysosomes. It is eluted most effectively by low pH (3.0) and can be rebound and re-eluted from fixed secretory granules. In sodium dodecyl sulfate and beta-mercaptoethanol it has an apparent molecular weight of 51,000. In addition, two minor components, comprising about 20% of the material bound were detected having apparent molecular weights in sodium dodecyl sulfate of 14,000 and 62,000. It is suggested that such a molecule could function as a plasma membrane-located receptor for chromaffin granules during the secretory process.     

Fermentation of sweet whey by ethanologenic Escherichia coli

Whey, an abundant byproduct of the dairy industry, contains large amounts of protein and lactose which could be used for fuel ethanol production. We have investigated a new organism as a candidate for such fermentations: recombinant Escherichia coli containing the genes encoding the ethanol pathway from Zymomonas mobilis. The highest level of ethanol achieved, 68 g/L, was produced after 108 hours in Luria broth containing 140 g lactose/L. Fermentations of lower lactose concentrations were completed more rapidly with approximately 88% of theoretical yields. Reconstituted sweet whey (60 g lactose/L)was fermented more slowly than lactose in Luria broth requiring 144 hours to produce 26 g ethanol/L. Supplementing sweet whey with a trace metal mix and ammonium sulfate reduced the required fermentation time to 72 hours and increased final ethanol concentration (28 g ethanol/L). By adding proteinases during fermentation, the requirement for ammonia was completely eliminated, and the rate of fermentation further improved (30 g ethanol/L after 48 hours). This latter incresed in rate of ethanol production and ethanol yield are presumed to result from incorporation of amino acids released by hydrolysis of whey proteins. The fermentation of sweet whey by ethanologenic E. coil reduced the nonvolatile residue by approximately 70%. This should reduce biological oxygen demand and reduce the cost of waste treatment. Whey supplemented with trace metals and small amounts of proteinase may represent an economically attractive feedstock for the production of ethanol and other useful chemicals.     

SNARE protein analog‐mediated membrane fusion

Fusion of lipid membranes to form a single bilayer is an essential process for life and provides important biological functions including neurotransmitter release. Membrane fusion proteins facilitate approximation of interacting membranes to overcome the energy barrier. In case of synaptic transmission, proteins involved are known as soluble N‐ethylmaleimide‐sensitive‐factor attachment receptor (SNARE) proteins. The SNAREs from synaptic vesicles interact with the SNAREs from the target membrane to form a coiled‐coil bundle of four helices, thus pulling the membranes tightly together and initiating fusion. However, it remains unclear how these proteins function at molecular level. Natural systems are often too complex to obtain unambiguous results. Simple model systems mimicking natural proteins in synthetic lipid bilayers are powerful tools for obtaining insights into this essential biological process. An important advantage of such systems is their well‐defined composition, which can be systematically varied in order to fully understand events at molecular level. In this review, selected model systems are presented based upon specific interactions between recognition units embedded in separate lipid bilayers mimicking native SNARE protein‐mediated membrane fusion. Copyright © 2015 European Peptide Society and John Wiley & Sons, Ltd.     

Isolation and Characterization Of Chimeric Human Fc-expressing Proteins Using Protein A Membrane Adsorbers And A Streamlined Workflow

Laboratory scale to industrial scale purification of biomolecules from cell culture supernatants and lysed cell solutions can be accomplished using affinity chromatography. While affinity chromatography using porous protein A agarose beads packed in columns is arguably the most common method of laboratory scale isolation of antibodies and recombinant proteins expressing Fc fragments of IgG, it can be a time consuming and expensive process. Time and financial constraints are especially daunting in small basic science labs that must recover hundreds of micrograms to milligram quantities of protein from dilute solutions, yet lack access to high pressure liquid delivery systems and/or personnel with expertise in bioseparations. Moreover, product quantification and characterization may also excessively lengthen processing time over several workdays and inflate expenses (consumables, wages, etc.). Therefore, a fast, inexpensive, yet effective protocol is needed for laboratory scale isolation and characterization of antibodies and other proteins possessing an Fc fragment. To this end, we have devised a protocol that can be completed by limited-experience technical staff in less than 9 hr (roughly one workday) and as quickly as 4 hr, as opposed to traditional methods that demand 20+ work hours. Most required equipment is readily available in standard biomedical science, biochemistry, and (bio)chemical engineering labs, and all reagents are commercially available. To demonstrate this protocol, representative results are presented in which chimeric murine galectin-1 fused to human Fc (Gal-1hFc) from cell culture supernatant was isolated using a protein A membrane adsorber. Purified Gal-1hFc was quantified using an expedited Western blotting analysis procedure and characterized using flow cytometry. The streamlined workflow can be modified for other Fc-expressing proteins, such as antibodies, and/or altered to incorporate alternative quantification and characterization methods.     

Microbial production of single-cell protein from deproteinized whey concentrates

Deproteinized sweet and sour cheese whey concentrates were investigated for their suitability as substrates for the production of single-cell protein with Kluyveromyces marxianus CBS 6556 up to a 100-l scale. An important factor for gaining high cell concentrations was the use of the Crabtree-negative strain K. marxianus CBS 6556. Supplements such as trace elements, ammonium and calcium were required for the complete conversion of sweet whey concentrates into biomass, whereas sour whey concentrates had to be supplemented with ammonium, trace elements and vitamins. After improvement, biomass dry concentrations of up to 50 g l⁻¹ could be reached with Yx/s values of 0.52 for sweet whey and of up to 65 g l⁻¹ with Yx/s values of 0.48 for sour whey concentrates. The chemical oxygen demand of the whey concentrates were reduced by 80%. The cells were used for the analysis of amino acid and ash composition, showing a distinct increase of eight out of ten essential amino acids compared to sweet and sour whey protein and exceeding the World Health Organisation guidelines for valine, leucine, isoleucine, threonine, phenylalanine and tyrosine.     

Mechanisms of phase behaviour and protein partitioning in detergent/polymer aqueous two-phase systems for purification of integral membrane proteins

Detergent/polymer aqueous two-phase systems are studied as a fast, mild and efficient general separation method for isolation of labile integral membrane proteins. Mechanisms for phase behaviour and protein partitioning of both membrane-bound and hydrophilic proteins have been examined in a large number of detergent/polymer aqueous two-phase systems. Non-ionic detergents such as the Triton series (polyoxyethylene alkyl phenols), alkyl polyoxyethylene ethers (C(m)EO(n)), Tween series (polyoxyethylene sorbitol esters) and alkylglucosides form aqueous two-phase systems in mixtures with hydrophilic polymers, such as PEG or dextran, at low and moderate temperatures. Phase diagrams for these mixtures are shown and phase behaviour is discussed from a thermodynamic model. Membrane proteins, such as bacteriorhodopsin and cholesterol oxidase, were partitioned strongly to the micelle phase, while hydrophilic proteins, BSA and lysozyme, were partitioned to the polymer phase. The partitioning of membrane protein is mainly determined by non-specific hydrophobic interactions between detergent and membrane protein. An increased partitioning of membrane proteins to the micelle phase was found with an increased detergent concentration difference between the phases, lower polymer molecular weight and increased micelle size. Partitioning of hydrophilic proteins is mainly related to excluded volume effects, i.e. increased phase component size made the hydrophilic proteins partition more to the opposite phase. Addition of ionic detergent to the system changed the partitioning of membrane proteins slightly, but had a strong effect on hydrophilic proteins, and can be used for enhanced separation between hydrophilic proteins and membrane protein.     

Downstream processing of lactoperoxidase from milk whey by involving liquid emulsion membrane

The current work deals with downstream processing of lactoperoxidase using liquid emulsion membrane from the bovine milk whey, which is a by-product from dairy industry. It is an alternate separation technique that can be used for the selective extraction of lactoperoxidase. The extraction of lactoperoxidase in liquid emulsion membrane takes place due to the electrostatic interaction between the enzyme and polar head group of reverse micellar surfactant. The optimum conditions resulted in 2.86 factor purity and activity recovery of 75.21%. Downstream processing involving liquid emulsion membrane is a potential technique for the extraction of lactoperoxidase from bovine whey.     

Bacteriostatic effect of orally administered bovine lactoferrin on proliferation of Clostridium species in the gut of mice fed bovine milk.

When milk-fed mice were orally inoculated with Clostridium ramosum C1, this strain proliferated in the gut and became the dominant component of the fecal microflora. In this experimental model, bovine lactoferrin (bLF) administered with milk suppressed the proliferation of this strain in vivo and decreased the numbers of C. ramosum and other bacteria in the feces. This bacteriostatic effect of bLF was dependent on the concentration of bLF, the duration of feeding, and the administered dose of C. ramosum C1. Compared with bovine serum albumin, ovalbumin, bovine whey protein isolate, or bovine casein, only bLF showed this specific activity. A similar effect of bLF was observed after oral inoculation with C. ramosum JCM 1298, C. paraputrificum VPI 6372, or C. perfringens ATCC 13124. A hydrolysate prepared by digestion of bLF with porcine pepsin showed the same inhibitory effect on proliferation of C. ramosum in vivo as occurred with undigested bLF. These results indicate that ingested bLF can exert a bacteriostatic effect against clostridia in the gut even after it has been digested to some extent.     

A new large‐scale manufacturing platform for complex biopharmaceuticals

Complex biopharmaceuticals, such as recombinant blood coagulation factors, are addressing critical medical needs and represent a growing multibillion‐dollar market. For commercial manufacturing of such, sometimes inherently unstable, molecules it is important to minimize product residence time in non‐ideal milieu in order to obtain acceptable yields and consistently high product quality. Continuous perfusion cell culture allows minimization of residence time in the bioreactor, but also brings unique challenges in product recovery, which requires innovative solutions. In order to maximize yield, process efficiency, facility and equipment utilization, we have developed, scaled‐up and successfully implemented a new integrated manufacturing platform in commercial scale. This platform consists of a (semi‐)continuous cell separation process based on a disposable flow path and integrated with the upstream perfusion operation, followed by membrane chromatography on large‐scale adsorber capsules in rapid cycling mode. Implementation of the platform at commercial scale for a new product candidate led to a yield improvement of 40% compared to the conventional process technology, while product quality has been shown to be more consistently high. Over 1,000,000 L of cell culture harvest have been processed with 100% success rate to date, demonstrating the robustness of the new platform process in GMP manufacturing. While membrane chromatography is well established for polishing in flow‐through mode, this is its first commercial‐scale application for bind/elute chromatography in the biopharmaceutical industry and demonstrates its potential in particular for manufacturing of potent, low‐dose biopharmaceuticals. Biotechnol. Bioeng. 2012; 109: 3049–3058. © 2012 Wiley Periodicals, Inc.     

Demonstration of a strategy for product purification by high-gradient magnetic fishing: recovery of superoxide dismutase from unconditioned whey

A systematic approach for the design of a bioproduct recovery process employing magnetic supports and the technique of high-gradient magnetic fishing (HGMF) is described. The approach is illustrated for the separation of superoxide dismutase (SOD), an antioxidant protein present in low concentrations (ca. 0.15-0.6 mg L(-1)) in whey. The first part of the process design consisted of ligand screening in which metal chelate supports charged with copper(II) ions were found to be the most suitable. The second stage involved systematic and sequential optimization of conditions for the following steps: product adsorption, support washing, and product elution. Next, the capacity of a novel high-gradient magnetic separator (designed for biotechnological applications) for trapping and holding magnetic supports was determined. Finally, all of the above elements were assembled to deliver a HGMF process for the isolation of SOD from crude sweet whey, which consisted of (i) binding SOD using Cu2+ -charged magnetic metal chelator particles in a batch reactor with whey; (ii) recovery of the "SOD-loaded" supports by high-gradient magnetic separation (HGMS); (iii) washing out loosely bound and entrained proteins and solids; (iv) elution of the target protein; and (v) recovery of the eluted supports from the HGMF rig. Efficient recovery of SOD was demonstrated at approximately 50-fold increased scale (cf magnetic rack studies) in three separate HGMF experiments, and in the best of these (run 3) an SOD yield of >85% and purification factor of approximately 21 were obtained.