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 Bovine Lactoferrin from Sweet Whey

The development of a downstream process for the isolation of bovine lactoferrin (bLF) from sweet whey is presented. Whey is a by‐product from the cheese manufacturing process that is often used to produce whey protein concentrate powders for food applications. Besides the major whey proteins such as lactalbumin or BSA, minor whey proteins are present such as lactoperoxidase and bLF. In addition to the well‐known biological functions as an antimicrobial and antiviral agent, bLF shows immunomodulatory functions in the host defence system. For the isolation of bLF, a two‐step downstream process was developed based on membrane systems. This paper discusses the application of several membrane types for a crossflow filtration of sweet whey to remove insoluble particles and lipids from the whey with the aim of obtaining a permeate which can be directly used for downstreaming the minor component via ion exchange membrane adsorber systems. The application of such a membrane adsorber is demonstrated.     

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.     

Integration of a perfusion reactor and continuous precipitation in an entirely membrane‐based process for antibody capture

Continuous precipitation coupled with continuous tangential flow filtration is a cost-effective alternative for the capture of recombinant antibodies from crude cell culture supernatant. The removal of surge tanks between unit operations, by the adoption of tubular reactors, maintains a continuous harvest and mass flow of product with the advantage of a narrow residence time distribution (RTD). We developed a continuous process implementing two orthogonal precipitation methods, CaCl₂ precipitation for removal of host-cell DNA and polyethylene glycol (PEG) for capturing the recombinant antibody, with no influence on the glycosylation profile. Our lab-scale prototype consisting of two tubular reactors and two stages of tangential flow microfiltration was continuously operated for up to 8 days in a truly continuous fashion and without any product flow interruption, both as a stand-alone capture and as an integrated perfusion-capture. Furthermore, we explored the use of a negatively charged membrane adsorber for flow-through anion exchange as first polishing step. We obtained a product recovery of approximately 80% and constant product quality, with more than two logarithmic reduction values (LRVs) for both host-cell proteins and host-cell DNA by the combination of the precipitation-based capture and the first polishing step.     

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.     

Centrifugal precipitation chromatography: principle, apparatus, and optimization of key parameters for protein fractionation by ammonium sulfate precipitation

A novel chromatographic system introduced here internally generates a concentration gradient of ammonium sulfate (AS) through a long separation channel under a centrifugal force field. Protein samples are exposed to a gradually increasing AS concentration and precipitated along the channel. Then, chromatographic elution is initiated by gradually decreasing the AS concentration in the gradient which causes the proteins to repeat dissolution and precipitation through the channel. Consequently, they are eluted out in the order of their solubility in the AS solution. The separation column consists of a pair of disks equipped with mutually mirror-imaged spiral grooves. A dialysis membrane is sandwiched between the disks to form two identical channels partitioned by the membrane. The disk assembly is mounted on the sealless continuous-flow centrifuge. When a concentrated AS solution is eluted through one channel and water through the other channel in an opposite direction, an exponential AS gradient is formed through the water channel. A series of basic experiments was performed to study the rates of AS transfer and osmosis through the membrane, and the operational parameters including elution time, revolution speed, inclination of gradient, and sample size were optimized using stable protein samples. Preliminary applications were successful in purification of monoclonal antibody from cell culture supernatant and an affinity separation of recombinant ketosteroid isomerase from a crude Escherichia coli lysate.     

A rapid method for the purification of β-lactamase from Bacillus cereus by affinity chromatography

A procedure for the purification of β-lactamase from Bacillus cereus in a single chromatographic step is described. The enzyme is isolated from the crude culture supernatant by affinity chromatography. An inhibitor, methicillin, was immobilised by covalent attachment to the insoluble column gel, Sepharose. The enzyme was adsorbed to the column ligand from the crude supernatant and was subsequently released by increasing the ionic strength of the eluting buffer. In this way the enzyme was selectively isolated from other proteins in the crude supernatant. About 98% of the original β-lactamase activity was recovered in the purified enzyme fraction.     

Primary structure of human class II histocompatibility antigens (HLA-D). I. Isolation, purification and characterization of the HLA-D alpha/beta chain complex from a homozygous lymphoblastoid B cell line, H2LCL (HLA-A3,3;B7,7;Dw2, 2;DR2,2;MT1,1;DC1,1;MB1,1

The complex of alpha and beta chains of HLA-D membrane antigens has been isolated from a lymphoblastoid homozygous B cell line, H2LCL (HLA-A3,3; B7,7; Dw2,2; DR2,2; MT1,1; DC1,1; MB1,1), by an exclusively chemical two-step procedure and characterized by electrophoresis as well as isoelectric focusing in polyacrylamide gel. Cells were gained using long term cultivation in large scale, the crude membrane by differential centrifugation. The proteins of the crude membrane were then solubilized in NP-40, pH 5.0. The first purification step for HLA-D antigens consisted in an ion-exchange chromatography on carboxymethyl cellulose using the solubilization buffer. By this procedure the complex of proteins with relative molecular masses of Mr approximately 34 000 and Mr approximately 29 000 was in a high percentage not bound to the carboxymethyl cellulose. The bound fraction contained the HLA-A, -B and -C antigens and a component with Mr approximately 31 000 corresponding to the well known Ii-fraction. The bound proteins could be recovered from the column by a sodium chloride gradient. The proteins not bound to the carboxymethyl cellulose were precipitated with acetone, dissolved, dialysed against SDS buffer, pH 7.2 and then submitted to the second purification step, the Sephacryl S-300 chromatography. By this procedure the corresponding complex could be further separated from higher and lower molecular proteins. The complex was used as the starting material for the separation of alpha and beta chains. Amino-acid sequences established of the isolated chains have already been communicated.     

Quantitation of soluble aggregates in recombinant monoclonal antibody cell culture by pH-gradient protein A chromatography

Monoclonal antibodies (mAbs) produced from mammalian cell culture may contain significant amounts of dimers and higher order aggregates. Quantitation of soluble aggregates in the cell culture is time-consuming and labor-intensive, usually involving a purification step to remove the impurities that interfere with the subsequent size exclusion chromatography (SEC) analysis. We have developed a novel pH-gradient protein A chromatography for rapid, non-size based separation of the aggregates in mAb cell culture samples. Our results demonstrate that this method has excellent correlation with SEC and can be applied to both human immunoglobulin gamma 1 (IgG1) and IgG2 antibodies. This approach can be useful in the quantitation of soluble aggregates in crude cell culture samples.     

High-resolution Native-PAGE for membrane proteins capable of fluorescence detection and hydrodynamic state evaluation

An improved native polyacrylamide gel electrophoresis (PAGE) method capable of evaluating the hydrodynamic states of membrane proteins and allowing in-gel fluorescence detection was established. In this method, bis(alkyl) sulfosuccinate is used to provide negative charges for detergent-solubilized membrane proteins to facilitate proper electrophoretic migration without disturbing their native hydrodynamic states. The method achieved high-resolution electrophoretic separation, in good agreement with the elution profiles obtained by size exclusion chromatography. The applicability of in-gel fluorescence detection for tagged green fluorescent protein (GFP) facilitates the analysis of samples without any purification. This method might serve as a general analytical technique for assessing the folding, oligomerization, and protein complex formation of membrane proteins.     

Simultaneous ultrafiltration and affinity sorptive separation of proteins in a hollow fiber membrane module

A protein separation scheme combining affinity or ion exchange sorption with hollow fiber cross-flow filtration is described. Sorptive gel particles were loaded into the shell side of a hollow fiber membrane module. In the adsorption step, crude protein mixtures were passed through the lumen and permeating proteins passed through the membrane to bind on the gel particles in the shell. During elution, a buffer of adequate ionic strength to desorb the bound proteins was passed through the lumen and permeated through the shell. The eluant was then collected at the outlet to the shell of the hollow fiber module. The concept is illustrated by two examples: the purification of butyrylcholinesterase (EC 3.1.1.7) from raw horse serum using the affinity gel procainamide-Sepharose as the packing and the separation of carboxylesterase (EC 3.1.1.1) from beef liver homogenate using DEAE-Sephadex as the packing. The technique has the advantage of high volumetric throughputs typical of hollow fiber membrane modules as well as the high capacity characteristic of chromatographic packings. In addition, cross-flow filtration of particulates, agglomerates, and debris in passing protein from lumen to shell side can help eliminate the need for extensive pretreatment.     

A large-scale purification of paclitaxel from cell cultures of Taxus chinensis

A large-scale purification method was developed for producing paclitaxel, to guarantee high purity and yield from plant cell cultures. The complete method for mass production was a simple and efficient procedure, for the isolation and purification of paclitaxel from the biomass of Taxus chinensis, consisting of solvent extraction, synthetic adsorbent treatment, and two steps of precipitation, followed by two steps of high performance liquid chromatography (HPLC). The organic solvent extraction of biomass obtained crude extract containing paclitaxel. The use of synthetic adsorbent treatment and precipitation in the prepurification process allows for rapid and efficient separation of paclitaxel from interfering compounds and dramatically increases the yield and purity of crude paclitaxel for HPLC purification steps compared to alternative processes. This prepurification process serves to minimise solvent usage, size, and complexity of the HPLC operations for paclitaxel purification. The paclitaxel of over 99.5% purity can be simply obtained with high yield from crude paclitaxel by HPLC using reverse-phase separation on C18 as the first step and normal-phase separation on silica as the second step.     

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.     

Two step capture and purification of IgG2 using multicolumn countercurrent solvent gradient purification (MCSGP)

A two‐step chromatography process for monoclonal antibody (mAb) purification from clarified cell culture supernatant (cCCS) was developed using cation exchange Multicolumn Countercurrent Solvent Gradient Purification (MCSGP) as a capture step. After an initial characterization of the cell culture supernatant the capture step was designed from a batch gradient elution chromatogram. A variety of chromatographic materials was screened for polishing of the MCSGP‐captured material in batch mode. Using multi‐modal anion exchange in bind‐elute mode, mAb was produced consistently within the purity specification. The benchmark was a state‐of‐the‐art 3‐step chromatographic process based on protein A, anion and cation exchange stationary phases. The performance of the developed 2‐step process was compared to this process in terms of purity, yield, productivity and buffer consumption. Finally, the potential of the MCSGP process was investigated by comparing its performance to that of a classical batch process that used the same stationary phase. Biotechnol. Bioeng. 2010;107: 974–984. © 2010 Wiley Periodicals, Inc.     

Isolation of an integral membrane glycoprotein by chloroform-methanol extraction and C3-reversed-phase high-performance liquid chromatography

Methodology is presented for the isolation of integral membrane proteins and applied to the purification of the major myelin glycoprotein, P0. This isolation scheme depends on the detergent solubilization of an isoosmotically extracted membrane fraction from sciatic nerve endoneurium, followed by the removal of lipids and detergent by chloroform/methanol extraction. The resulting membrane proteins are readily dissolved in acetic acid/water (1/1) and directly analyzed by reversed-phase high-performance liquid chromatography. The hydrophobic nature of the intrinsic membrane protein mixture results in strong binding to a C8 stationary phase, leading to poor resolution and yields. These problems can be eliminated by employing a C3 alkylsilane column, thereby allowing separation of the protein components and the isolation of P0. The purified P0 has an amino-terminal sequence that matches that predicted from nucleotide sequencing, and the glycoprotein contains the expected amount of sialic acid. This latter finding indicates that the isolation procedure is not detrimental to the complex-type oligosaccharide structure of P0 and should make the methodology readily applicable to the purification of other integral membrane proteins and glycoproteins.     

Purification of a membrane glycoprotein with an inositol-containing phospholipid anchor from Dictyostelium discoideum.

Large-scale purification of a Dictyostelium discoideum cell surface glycoprotein, which is anchored in the membrane via a glycosylphosphatidylinositol (GPI) moiety, is described. The purification protocol involved four steps: separation of crude cell membranes by low-speed centrifugation, delipidization of these membranes using acetone, extraction of the membrane proteins using the detergent Octyl beta-D-thioglucopyranoside (OTP), and purification of a specific membrane protein by monoclonal antibody immunoaffinity chromatography. The protein purified, PsA (prespore-specific antigen), is a developmentally regulated membrane glycoprotein found on a subset of cells from the cellular slime mould, D. discoideum. The protocol provides an efficient, economical, and technically simple way to purify GPI proteins in sufficient quantities for structural and functional studies. PsA was recovered at a yield of about 60%; with a purity of 97%, the extraction of 1 x 10(10) cells (1.1 g dry weight) yielded about 0.5 mg PsA glycoprotein. Techniques are described for growing kilogram quantities of D. discoideum cells in stainless steel trays at little cost. D. discoideum has considerable potential as a novel expression system for the production of foreign membrane-associated proteins. The purification strategy provides a means of purifying other GPI proteins, including those produced by protein engineering techniques.     

Antibody purification from CHO cell supernatant using new multimodal membranes

This contribution describes strategies to purify monoclonal antibodies from Chinese hamster ovary (CHO) cell culture supernatant using newly designed multimodal membranes (MMMs). The MMMs were used for the capture step purification of human IgG₁ following a size‐exclusion desalting column to remove chaotropic salts that interfere with IgG binding. The MMM column attained higher dynamic binding capacity than a Protein A resin column at an equivalent residence time of 1 min. The two‐step MMM chromatography process achieved high selectivity for capturing hIgG₁ from the CHO cell culture supernatant, though the desalting step resulted in product dilution. Product purity and host cell protein (HCP) level in the elution pool were analyzed and compared to results from a commercial Protein A column. The product purity was >98% and HCP levels were <20 ppm for both purification methods. In addition, hIgG₁ could be eluted from the MMM chromatography column at neutral pH, which is important for limiting the formation of aggregates; although slow elution dilutes the product. Overall, this paper shows that MMMs are highly effective for capture step purification of proteins and should be considered when Protein A cannot be used, e.g., for pH sensitive mAbs or proteins lacking an Fc binding domain. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:658–665, 2017     

Isolation and characterization of the proteolytic enzyme component from commercially available crude trypsins

A purification procedure for the isolation of a mixture of the major proteolytic pancreatic enzymes (trypsin, chymotrypsin, and elastase) from commercial crude trypsins is described. These enzymes are apparently the enzymes responsible for tissue dispersal in numerous cell culture systems. Materials toxic to cell cultures, present in certain crude trypsin samples, are removed during a purification involving centrifugation, dialysis, treatment with a cellulose ion-exchange resin, removal of salts, and lyophilization. While the fundamental use of this proteolytic mixture would be to prepare primary cell culture, the broad peptide bond specifleity of this mixture would suggest application in cases where a general protease, free of other enzymatic activities, is required.     

Ion exchange purification of G6PDH from unclarified yeast cell homogenates using expanded bed adsorption

The use of expanded beds of STREAMLINE ion exchange adsorbents for the direct extraction of an intracellular enzyme glucose-6-phosphate dehydrogenase (G6PDH) from unclarified yeast cell homogenates has been investigated. It has been demonstrated that such crude feedstocks can be applied to the bed without prior clarification steps. The purification of G6PDH from an unclarified yeast homogenate was chosen as a model system containing the typical features of a direct extraction technique. Optimal conditions for the purification were determined in small scale, packed bed experiments conducted with clarified homogenates. Results from these experiments were used to develop a preparative scale separation of G6PDH in a STREAMLINE 50 EBA apparatus. The use of an on-line rotameter for measuring and controlling the height of the expanded bed when operated in highly turbid feedstocks was demonstrated. STREAMLINE DEAE has been shown to be successful in achieving isolation of G6PDH from an unclarified homogenate with a purification factor of 12 and yield of 98% in a single step process. This ion exchange adsorbent is readily cleaned using simple cleaning-in-place procedures without affecting either adsorption or the bed expansion properties of the adsorbent after many cycles of operation. The ability of combining clarification, capture, and purification in a single step will greatly simplify downstream processing flowsheets and reduce the costs of protein purification. (c) 1996 John Wiley & Sons, Inc.     

Resolution of Rhodocyclus gelatinosus photoreceptor unit components by temperature-induced phase separation in the presence of decyltetraoxyethylene

A simple method for dissociating photoreceptor units from Rhodocyclus gelatinosus is described. Incubation of a chromatophore extract (Agalidis, I., Rivas, E. and Reiss-Husson, F. (1990) Photosynth. Res. 23, 249-255) at 4 degrees C with decyltetraoxyethylene and octyl-beta-D-thioglucopyranoside, followed by temperature-induced phase separation at 20 degrees C, led to the formation of three phases: a pellet composed of pure B875 antenna; an oily layer containing cytochrome c and other proteins; a detergent-poor supernatant containing crude reaction centers. This method provided a first step towards further purification of reaction centers and B875 antenna, respectively.