Evaluation of dynamic control of continuous capture with periodic counter-current chromatography under feedstock variations

Multi-column periodic counter-current chromatography is a promising technology for continuous antibody capture. However, dynamic changes due to disturbances and drifts pose some potential risks for continuous processes during long-term operation. In this study, a model-based approach was used to describe the changes in breakthrough curves with feedstock variations in target proteins and impurities. The performances of continuous capture of three-column periodic counter-current chromatography under ΔUV dynamic control were systematically evaluated with modeling to assess the risks under different feedstock variations. As the concentration of target protein decreased rapidly, the protein might not breakthrough from the first column, resulting in the failure of ΔUV control. Small reductions in the concentrations of target proteins or impurities would cause protein losses, which could be predicted by the modeling. The combination of target protein and impurity variations showed complicated effects on the process performance of continuous capture. A contour map was proposed to describe the comprehensive impacts under different situations, and nonoperation areas could be identified due to control failure or protein loss. With the model-based approach, after the model parameters are estimated from the breakthrough curves, it can rapidly predict the process stability under dynamic control and assess the risks under feedstock variations or UV signal drifts. In conclusion, the model-based approach is a powerful tool for continuous process evaluation under dynamic changes and would be useful for establishing a new real-time dynamic control strategy.

Model-assisted process development, characterization and design of continuous chromatography for antibody separation

Continuous manufacturing in monoclonal antibody production has generated increased interest due to its consistent quality, high productivity, high equipment utilization, and low cost. One of the major challenges in realizing continuous biological manufacturing lies in implementing continuous chromatography. Given the complex operation mode and various operation parameters, it is challenging to develop a continuous process. Due to the process parameters being mainly determined by the breakthrough curves and elution behaviors, chromatographic modeling has gradually been used to assist in process development and characterization. Model-assisted approaches could realize multi-parameter interaction investigation and multi-objective optimization by integrating continuous process models. These approaches could reduce time and resource consumption while achieving a comprehensive and systematic understanding of the process. This paper reviews the application of modeling tools in continuous chromatography process development, characterization and design. Model-assisted process development approaches for continuous capture and polishing steps are introduced and summarized. The challenges and potential of model-assisted process characterization are discussed, emphasizing the need for further research on the design space determination strategy and parameter robustness analysis method. Additionally, some model applications for process design were highlighted to promote the establishment of the process optimization and process simulation platform.

Improved process design for monoclonal antibody charge variants separation with multicolumn counter-current solvent gradient purification

The multicolumn counter-current solvent gradient purification (MCSGP) method has proven effective in addressing the issue of elution profile overlap for difficult-to-separate proteins, leading to improved purity and recovery. However, during the MCSGP process, the flow rate and proportion of loaded proteins undergo changes, causing a significant discrepancy between the elution profiles of batch process design and the actual MCSGP process. This mismatch negatively impacts the purity and recovery of the target protein. To address this challenge, an improved process design (reDesign) was proposed with the first-run MCSGP to mimic the actual continuous process and obtain elution profiles that closely resemble the real ones. The reDesign was demonstrated with both a model protein mixture and a sample of monoclonal antibody (mAb) with charge variants. For model protein mixture, the reDesign-based MCSGP process (reMCSGP) showed a remarkable improvement in recovery, increasing from 83.6% to 97.8% while maintaining a purity of more than 95%. For mAb sample, the recovery of reMCSGP improved significantly to 93.9%, surpassing the performance of normal MCSGP processes at a given purity level of more than 84%. In general, the new process design strategy developed in this work could generate a more representative elution profile that closely mirrors actual conditions in continuous processes, which enhances the separation performance of MCSGP.

Role of the gradient slope during the product internal recycling for the multicolumn countercurrent solvent gradient purification of PEGylated proteins

Protein PEGylation, i.e. functionalization with poly(ethylene glycol) chains, has been demonstrated an efficient way to improve the therapeutic index of these biopharmaceuticals. We demonstrated that Multicolumn Countercurrent Solvent Gradient Purification (MCSGP) is an efficient process for the separation of PEGylated proteins (Kim et al., Ind. and Eng. Chem. Res. 2021, 60, 29, 10764-10776), thanks to the internal recycling of product-containing side fractions. This recycling phase plays a critical role in the economy of MCSGP as it avoids wasting valuable product, but at the same time impacts its productivity extending the overall process duration. In this study, our aim is to elucidate the role of the gradient slope within this recycling stage on the yield and productivity of MCSGP for two case-studies: PEGylated lysozyme and an industrially relevant PEGylated protein. While all the examples of MCSGP in the literature refer to a single gradient slope in the elution phase, for the first time we systematically investigate three different gradient configurations: i) a single gradient slope throughout the entire elution, ii) recycling with an increased gradient slope, to shed light on the competition between volume of the recycled fraction and required inline dilution and iii) an isocratic elution during the recycling phase. The dual gradient elution proved to be a valuable solution for boosting the recovery of high-value products, with the potential for alleviating the pressure on the upstream processing.

Obtaining acidic and basic charge variants using a twin-column continuous chromatography system

For recombinantly produced monoclonal antibody (mAb), charge variants including acidic and basic species are common heterogeneities. For characterization purpose, sufficient amount of acidic and basic species with high purity is needed. In this work, we developed an approach that allows for continuous separating and collecting of acidic and basic charge variants. First, with batch-mode cation exchange (CEX) chromatography, the load density and linear salt gradient elution conditions under which good separation of both charge variants can be achieved were determined. Next, a stepwise elution protocol was developed based on the linear gradient elution. Finally, acidic and basic charge variants were persistently produced under stepwise elution using a customized twin-column continuous chromatography system. This approach allows acidic and basic charge variants with high purity (i.e., >90%) to be efficiently generated in sufficient amount, which greatly facilitates the necessary characterization of these mAb variants.

Continuous Countercurrent Chromatography in Protein Purification

Continuous countercurrent chromatography can be applied for both capture and polishing steps in the downstream processing of biopharmaceuticals. This chapter explains the concept of countercurrent operation, focusing on twin-column processes and how it can be used to alleviate the trade-offs of traditional batch chromatography with respect to resin utilization/productivity and yield/purity. CaptureSMB and MCSGP, the main twin-column continuous countercurrent chromatography processes, are explained, and the metrics by which they are compared to single-column chromatography are identified. Practical hints for process design and application examples are provided. Finally, regulatory aspects, scale-up, and UV-based process control are covered.

Design and economic investigation of a Multicolumn Countercurrent Solvent Gradient Purification unit for the separation of an industrially relevant PEGylated protein

Conjugation of biopharmaceuticals to polyethylene glycol chains, known as PEGylation, is nowadays an efficient and widely exploited strategy to improve critical properties of the active molecule, including stability, biodistribution profile, and reduced clearance. A crucial step in the manufacturing of PEGylated drugs is the purification. The reference process in industrial settings is single-column chromatography, which can meet the stringent purity requisites only at the expenses of poor product recoveries. A valuable solution to this trade-off is the Multicolumn Countercurrent Solvent Gradient Purification (MCSGP), which allows the internal and automated recycling of product-containing side fractions that are typically discarded in the batch processes. In this study, an ad hoc design procedure was applied to the single-column batch purification of an industrially relevant PEGylated protein, with the aim of defining optimal collection window, elution duration and elution buffer ionic strength to be then transferred to the MCSGP. This significantly alleviates the design of the continuous operation, subjected to manifold process parameters. The MCSGP designed by directly transferring the optimal parameters allowed to improve the yield and productivity by 8.2% and 17.8%, respectively, when compared to the corresponding optimized batch process, ensuring a purity specification of 98.0%. Once the efficacy of MCSGP was demonstrated, a detailed analysis of its cost of goods was performed and compared to the case of single-column purification. To the best of our knowledge, this is the first example of a detailed economic investigation of the MCSGP across different manufacturing scenarios and process cadences of industrial relevance, which demonstrated not only the viability of this continuous technology but also its flexibility.

Integrated continuous biomanufacturing on pilot scale for acid-sensitive monoclonal antibodies

In this study, we demonstrated the first, to our knowledge, integrated continuous bioprocess (ICB) designed for the production of acid-sensitive monoclonal antibodies, prone to aggregate at low pH, on pilot scale. A high cell density perfusion culture, stably maintained at 100 x 10⁶ cells/mL, was integrated with the downstream process, consisting of a capture step with the recently developed Protein A ligand, Z_Ca ; a solvent/detergent-based virus inactivation; and two ion exchange chromatography steps. The use of a mild pH in the downstream process makes this ICB suitable for the purification of acid-sensitive monoclonal antibodies. Integration and automation of the downstream process were achieved using the Orbit software, and the same equipment and control system were used in initial small-scale trials and the pilot-scale downstream process. High recovery yields of around 90% and a productivity close to 1 g purified antibody/L/day were achieved, with a stable glycosylation pattern and efficient removal of impurities, such as host cell proteins and DNA. Finally, negligible levels of antibody aggregates were detected owing to the mild conditions used throughout the process. The present work paves the way for future industrial-scale integrated continuous biomanufacturing of all types of antibodies, regardless of acid stability. This article is protected by copyright. All rights reserved.

Multi-wavelength UV-based PAT tool for measuring protein concentration

Process chromatography is commonly used for purification of therapeutic proteins. Most chromatography skids that are used in such operations utilize single ultraviolet (UV) absorbance for monitoring and quantification of protein content. While the signal from such UV measurement is linear with respect to protein concentration at low values of protein concentrations, as the concentration increases across an eluting product peak, it goes manifold over the linear range, resulting in saturation of the UV signal and as a result incomplete quantification of the protein concentration. This can hamper our ability to decide on where to pool the process chromatography peak. It is evident that a simple, fast, and cost-effective methodology for on-line estimation of protein concentration is the need of the hour. In this paper, a multi-wavelength UV-based approach has been proposed for dilution-free on-line concentration estimation in the range of 0.8-100 g/L. Stable absorbance regions are picked up in the proposed approach from the multi-wavelength UV spectra, thereby offering a solution to the problem of saturation and non-linearity of the UV signal that is otherwise observed at higher concentrations. Further, using chemometrics tools such as principal component analysis (PCA) and partial least squares (PLS), the model has been validated for rapid quantification of protein concentration from the spectra. The predictions from the model were comparable to values measured using an existing UV-based offline method with an R² of>98%. The proposed process analytical technology (PAT) tool was successfully tested online and exhibited<8% variability and could effectively be used from capture to formulation to enable dilution-free online concentration measurement of IgG. The proposed tool is a simple, low-cost alternative to other methods and could enable integrated/continuous operations throughout the downstream train.

Continuous purification of influenza A virus particles using pseudo-affinity membrane chromatography

Robust and flexible continuous unit operations that enable the establishment of intensified bioprocesses is one of the most relevant trends in manufacturing of biopharmaceuticals, including virus-based products. Sulfated cellulose membrane adsorbers (SCMA) are one of the most promising matrices for chromatographic purification of virus particles, like influenza viruses. Here, a three 'column' periodical counter current set-up was used to continuously purify influenza A/PR/8/34 virus particles using SCMA in bind-elute mode. It was possible to recover 67.4% of the HA-activity and to remove 67.4% and 99.8% of the total protein and DNA, respectively. The performance of the continuous process operated over a total of 10 loops, was slightly inferior to was obtained in a comparable batch process. Nevertheless, it was possible to increase the effective usage of binding capacity to 80%, resulting on a productivity of 22.8 kHAU ml_memb^-1 min^-1. As a proof-of-principle, SCMA were successfully used as matrix for purification of cell-derived influenza virus particles, in continuous mode.

A regressive approach to the design of continuous capture process with multi-column chromatography for monoclonal antibodies

Although empirical methods have been introduced in the process development of continuous chromatography, the common approach to optimize a multi-column continuous capture chromatography (periodic counter-current chromatography, PCCC) process heavily relies on numerical model simulations and the number of experiments. In addition, different multi-column settings in PCCC add more design variables in process development. In this study, we have developed a rational method for designing PCCC processes based on iterative calculations by mechanistic model-based simulations. Breakthrough curves of a monoclonal antibody were measured at different residence times for three protein A resins of different particle sizes and capacities to obtain the parameters needed for the simulation. Numerical calculations were performed for the protein sample concentration in the range of 1.5 to 4 g/L. Regression curves were developed to describe the relative process performances compared with batch operation, including the resin capacity utilization and the buffer consumption. Another linear correlation was established between breakthrough cut-off (BT%) and a modified group composed of residence time, mass transfer coefficient, and particle size. By normalizing BT% with binding capacity and switching time, the linear regression curves were established for the three protein A resins, which are useful for the design and optimization of PCCC to reduce the process development time.

Comparison of Protein A affinity resins for twin-column continuous capture processes: Process performance and resin characteristics

Continuous chromatography is a promising technology for downstream processing of biopharmaceuticals. The operation of continuous processes is significantly different to batch-mode chromatography and needs comprehensive evaluation. In this work, the performances of four Protein A affinity resins were studied systematically for twin-column continuous capture processes. A model-based approach was used to evaluate the process performance (productivity and capacity utilization) under varying operation conditions, and the objective was to reveal the crucial resin properties for continuous capture. The trade-off between productivity and capacity utilization was found, and it is necessary to select appropriate resins for different feedstock and operation conditions. The capacity utilization heavily depends on mass transfer, and steep breakthrough curves are favorable for high capacity utilization. The productivity is determined by both equilibrium binding capacity and mass transfer, and the balance of feed amount and feed time is critical. Moreover, the influence of binding capacity and mass transfer on process productivity and parameter sensitivity with two important resin properties (equilibrium binding capacity q_max and effective pore diffusion coefficient D_e) were assessed by the model, and suitable resin parameter ranges for twin-column continuous capture were determined. The model-based approach is an effective and useful tool to evaluate the complex performance of different resins and guide the design of next-generation resins for continuous processes.

Improving mAb capture productivity on batch and continuous downstream processing using nanofiber PrismA adsorbents

Improving productivity and decreasing costs for biotherapeutic agents has been a focal driving force in the manufacturing of biologics. Advances in upstream processes have been continuously outpacing the ability for downstream operations to purify biologics, especially monoclonal antibodies. Continuous chromatography has several benefits for biologic purification including automated control, decreased labor, improved productivity, and more consistent product attributes. The goal of this study was to improve productivity and decrease costs associated with batch-mode and continuous purification processes. Productivities using cellulose nanofibers with a protein A ligand offer greater than 30-fold higher productivities than their resin-based equivalents using periodic countercurrent technology with multiple column chromatography. The smaller columns needed for convective mass transfer, faster processing times, and decreased costs allow for a more efficient mAb capture step. Additionally, high throughput purification (grams of mAbs/day) can be achieved from the scale-down model developed using periodic countercurrent technology. These advancements will help drive the evolution of downstream operations to manage the higher workloads due to increased upstream titers in a cost-effective manner.

Model-assisted approaches for continuous chromatography: Current situation and challenges

Continuous bioprocessing is a promising trend in biopharmaceutical production, and multi-column continuous chromatography shows advantages of high productivity, high resin capacity utilization, small footprint, low buffer consumption and less waste. Due to the complexity and dynamic nature of continuous processing, traditional experiment-based approaches are often time-consuming and inefficient. In this review, model-assisted approaches were focused and their applications in continuous chromatography process development, validation and control were discussed. Chromatographic models are useful in describing particular process performances of continuous capture and polishing with multi-column chromatography. Model-assisted tools showed powerful ability in evaluating multiple operating parameters and identifying optimal points over the entire design space. The residence time distribution models, model-assisted process analytical technologies and model-predictive control strategies were also developed to reveal the propagation of disturbances, enhance real time monitor and achieve adaptive control to match the transient disturbances and deviations of continuous processes. Moreover, artificial neural networks and machine learning concepts were integrated into modeling approaches to improve data treatment. In general, further development in research and applications of model-assisted approaches for continuous chromatography are needed urgently to support the continuous manufacturing.

Modern trends in downstream processing of biotherapeutics through continuous chromatography: The potential of Multicolumn Countercurrent Solvent Gradient Purification

Single-column (batch) preparative chromatography is the technique of choice for purification of biotherapeutics but it is often characterized by an intrinsic limitation in terms of yield-purity trade-off, especially for separations containing a larger number of product-related impurities. This drawback can be alleviated by employing multicolumn continuous chromatography. Among the different methods working in continuous mode, in this paper we will focus in particular on Multicolumn Countercurrent Solvent Gradient Purification (MCSGP) which has been specifically designed for challenging separations of target biomolecules from their product-related impurities. The improvements come from the automatic internal recycling of the impure fractions inside the chromatographic system, which results in an increased yield without compromising the purity of the pool. In this article, steps of the manufacturing process of biopharmaceuticals will be described, as well as the advantages of continuous chromatography over batch processes, by particularly focusing on MCSGP.

From batch to continuous chromatographic purification of a therapeutic peptide through multicolumn countercurrent solvent gradient purification

A twin-column Multicolumn Countercurrent Solvent Gradient Purification (MCSGP) process has been developed for the purification of a therapeutic peptide, glucagon, from a crude synthetic mixture. This semi-continuous process uses two identical columns operating either in interconnected or in batch mode, thus enabling the internal recycle of the portions of the eluting stream which do not comply with purity specifications. Because of this feature, which actually results in the simulated countercurrent movement of the stationary phase with respect to the mobile one, the yield-purity trade-off typical of traditional batch preparative chromatography can be alleviated. Moreover, the purification process can be completely automatized. Aim of this work is to present a simple procedure for the development of the MCSGP process based on a single batch experiment, in the case of a therapeutic peptide of industrial relevance. This allowed to recover roughly 90% of the injected glucagon in a purified pool with a purity of about 90%. A comparison between the performance of the MCSGP process and the classical single column batch process indicates that percentage increase in the recovery of target product is +23% when transferring the method from batch conditions to MCSGP, with an unchanged purity of around 89%. This improvement comes at the expenses of a reduction of about 38% in productivity.

Viral clearance capacity by continuous Protein A chromatography step using Sequential MultiColumn Chromatography

In response to the strong demand of biological protein therapeutics, such as monoclonal antibodies (MAbs), continuous downstream process was developed to deliver these molecules while maintaining desired product consistency and quality attributes, and providing manufacturing efficiency and flexibility. Viral safety is a critical quality attribute for biopharmaceuticals, such as MAbs. Evaluation of the viral clearance by the downstream process is a key component of risk mitigation. Protein A chromatography is typically used as an initial capture step for MAbs and efficient for the removal of process-related impurities like Host Cell Proteins (HCP). This step can also contribute to the clearance of potential viral contaminants. Murine Minute Virus (MMV)-spiking experiments were performed at small scale to investigate the impact on the viral clearance efficiency of the way the Protein A chromatography step is carried out, whether in batch or multicolumn mode. Protein A chromatography step using Novasep Sequential MultiColumn Chromatography (SMCC) technology demonstrated no statistical difference in the viral reduction with reduction factor (RF) of 3.7 log₁₀ (vs. RF of 3.8 log₁₀ for batch). The experiments showed also similar viral distribution over the purification cycles and columns. Data confirmed that the viral clearance capacity by the continuous Protein A chromatography step using SMCC technology is maintained and efficient.

Design space and robustness analysis of batch and counter-current frontal chromatography processes for the removal of antibody aggregates

Increasing molecular diversity and market competition requires biopharmaceutical manufacturers to intensify their processes. In this respect, frontal chromatography on cation exchange resins has shown its potential to effectively remove aggregates. However, yield losses during the wash step need to be accepted in order to ensure robust product quality. In this work, we present a novel counter-current frontal chromatography process called Flow2, which uses inline dilution during an interconnected wash phase to allow high monomer recovery without contaminating the product pool with impurities. Its model-based design spaces under purity and yield constraints are compared with those corresponding to traditional batch processes in terms of size and process attributes yield and productivity. The Flow2 process shows the largest extent of feasible operating points independent of feed conditions. Thereby, it allows the implementation of higher ionic strength wash, thus widening the range of operating conditions resulting in yields above 95% compared to batch processes. Productivities of batch and counter-current processes are the same at short regeneration times and equal residence time. However, long regeneration times, while influencing the size of the Flow2 design space, are not detrimental for its productivity resulting in twice as high values as obtained for the batch process. Furthermore, process robustness is evaluated by the ability of the process to maintain the required product quality when subjected to process parameter perturbations. It is found that the Flow2 process is able to retain a larger design space associated also with higher yields showing its ability to improve process attributes without sacrificing robustness at the same time.

Integrated system for temperature-controlled fast protein liquid chromatography. III. Continuous downstream processing of monoclonal antibodies

Three different applications of travelling heating zone reactor (THZR) chromatography for the downstream processing of monoclonal antibodies (mAbs) are described. mAb containing feedstocks were applied to a fixed bed of the thermoresponsive rProtein A matrix, Byzen Pro™, contained in a bespoke column (held at 15 °C) fitted with a travelling heating (42 °C) device encircling a narrow section of the column. For the demonstration of continuous concentration, uninterrupted loading of 1.0 g/L mAb in a pH 8 binding buffer was synchronized with 5 repeated movements of the heating zone along the column's full length at a velocity of 0.1 mm/s. Elution of mAbs was induced solely by the travelling heating zone's action, each full movement generating a sharp concentrated elution peak accompanied by a small transient mAb concentration-dependent dip in conductivity. Quasi-steady-state operation occurred from the third elution onwards, delivering a mean mAb concentration of 4.9 g/L and process yield >93%. Quasi-continuous separation of the target mAb (1.41 g/L) from bovine serum albumin, BSA (1.0 g/L), was achieved by cyclically alternating the feeding of the mAb + BSA feedstock, with that of the binding buffer alone; supply of the latter was timed to coincide with movement of the heating zone. Accurate coordination of the heating zone's travel and switching from feed to buffer permitted quasi-steady-state collection (elutions 3-6) of sharp peaks of mAb in high purity (98.7%) and yield (88.7%) in 4.5-fold concentrated form, with BSA exiting in the flow through fractions between successive mAb elution peaks. Fully automated THZR-mediated quasi-continuous buffer exchange of 1.34 g/L mAb from a phosphate buffer pH 8 into a HEPES buffer pH 8 of slightly lower conductivity was performed over a 19 h period by carefully timed switching from one feed solution to the other and back again, whilst synchronising movement of the heating zone with feeding of the exchange buffer. Quasi-steady-state operation (elutions 2-9) resulted in an average eluted mAb yield of 94.5% and concentration of 4.8 g/L. Triggering movement of the heating zone slightly ahead of the switch from mAb feed to exchange buffer permitted the positioning of mAb elution peaks in 9 mL volume segments with the lowest recorded conductivity. Measurements of buffer exchange performance conducted with two 'protein-free' systems demonstrated that compared to tangential flow filtration in diafiltration mode, which represents the 'state-of-the-art' technology for buffer exchange, the THZR chromatography based approach affords a >60% saving in minimum volume of exchange buffer required to remove 99.9% of the original buffer. Combined far and near UV circular dichroism, intrinsic fluorescence and thermal melting experiments showed that, unlike conventional Protein A/G affinity chromatography, the conditions for THZR Protein A chromatography respect maintenance of a favourable structural profile for mAbs.

Continuous Chromatography Purification of Virus-Based Biopharmaceuticals: A Shortcut Design Method

Novel biopharmaceutical products, such as vaccines and viral vectors, play a significant role in the development of innovative therapeutic, prophylactic, and clinical applications. However, several challenges are posed when manufacturing these products. The diversity of cell lines and the different physical and chemical properties of these biologicals require the use of different production and processing technologies. Alternative purification strategies that can improve the purification yield, such as continuous chromatography, are regarded nowadays as enabling technologies to overcome some of the bottlenecks in biomanufacturing. This chapter offers a shortcut approach to implement a semi-continuous chromatography purification of hepatitis C virus-like particles produced in insect cells with recombinant baculovirus. Although the purification is based on ion exchange chromatography, the present methodology can be extended to other types of chromatography.

Operating mode and parameter selection in liquid-liquid chromatography

The presence of a liquid stationary phase in liquid-liquid chromatography (LLC) allows for high versatility of operation as well as adaptability to different sample types and separation tasks. LLC, also known as countercurrent chromatography (CCC) or centrifugal partition chromatography (CPC), offers the user a variety of operating modes, many of which have no direct equivalent in conventional preparative liquid-solid chromatography. These operating modes have the potential to greatly improve LLC separation performance compared to the standard "classical" isocratic batch injection mode, and they often require minimal to no addition of equipment to the standard set-up. However, reports of the use of alternative LLC operating modes make up only a fraction of the literature. This is likely due, at least in part, to the lack of clear guidelines and methods for operating mode and parameter selection, leaving alternative process options to be avoided and underutilized. This review seeks to remedy this by providing a thorough overview of the available LLC operating modes, identifying the key characteristics, advantages and disadvantages, and areas of application of each. Additionally, the equations and short-cut models aiding in operating mode and parameter selection are presented and critiqued, and their notation is unified for clarity. By rendering LLC and its alternative operating modes more accessible to current and prospective users, it is hoped to help expand the application of this technology and support the achievement of its full potential.

Continuous Manufacturing of Recombinant Therapeutic Proteins: Upstream and Downstream Technologies

Continuous biomanufacturing of recombinant therapeutic proteins offers several potential advantages over conventional batch processing, including reduced cost of goods, more flexible and responsive manufacturing facilities, and improved and consistent product quality. Although continuous approaches to various upstream and downstream unit operations have been considered and studied for decades, in recent years interest and application have accelerated. Researchers have achieved increasingly higher levels of process intensification, and have also begun to integrate different continuous unit operations into larger, holistically continuous processes. This review first discusses approaches for continuous cell culture, with a focus on perfusion-enabling cell separation technologies including gravitational, centrifugal, and acoustic settling, as well as filtration-based techniques. We follow with a review of various continuous downstream unit operations, covering categories such as clarification, chromatography, formulation, and viral inactivation and filtration. The review ends by summarizing case studies of integrated and continuous processing as reported in the literature.

Continuous purification of Candida antarctica lipase B using 3-membrane adsorber periodic counter-current chromatography

Batch chromatography has several disadvantages, such as insufficient utilization of the capacity of the resin, high buffer consumption and discontinuity. Considering the high costs for downstream processing, a continuously working chromatographic system with three membrane adsorber units was designed, tested and put into operation. The basic principle of the setup is periodic counter-current chromatography (PCCC). The PCCC system was used for capturing and purifying Candida antarctica lipase B (CalB) directly from cell lysate in one single unit operation. The best purification result was achieved by means of anion-exchange chromatography. The dynamic binding capacity with Sartobind® Q 75 amounted to 4.2 mg (56 g/cm2). After transferring the method to the 3MA-PCCC, 0.22 g CalB (73 U/mg) were obtained from 0.9 L E. coli lysate within 6 h and a recovery of 80%. Compared to the batch process, the productivity could be increased by 36% and the buffer consumption could be reduced by about 20%. Although the purification of CalB from lysate by means of anion-exchange chromatography was not selective and quantitative using the 3MA-PCCC device, it could be shown that the concept of the system was successfully implemented and led to a significant improvement of CalB purification.

Continuous and Integrated Expression and Purification of Recombinant Antibodies

This chapter introduces the necessary concepts to design continuous expression and purification processes for monoclonal antibodies. The operation of a perfusion bioreactor is discussed containing the preparation procedures, the seeding train and the preparation and control of a long-term production run. The downstream processes exploit the benefits of countercurrent chromatography. Their design from batch experiments is presented. The CaptureSMB process is introduced for continuous capturing while for polishing applications the design of the two-column MCSGP process is described. The chapter also puts these processes together in the context of their integration to an end-to-end production process.

a conventional batch process

The protein A capture step is the main cost-driver in downstream processing, with high attrition costs especially when using protein A resin not until end of resin lifetime. Here we describe a feasibility study, transferring a batch downstream process to a hybrid process, aimed at replacing batch protein A capture chromatography with a continuous capture step, while leaving the polishing steps unchanged to minimize required process adaptations compared to a batch process. 35g of antibody were purified using the hybrid approach, resulting in comparable product quality and step yield compared to the batch process. Productivity for the protein A step could be increased up to 420%, reducing buffer amounts by 30-40% and showing robustness for at least 48h continuous run time. Additionally, to enable its potential application in a clinical trial manufacturing environment cost of goods were compared for the protein A step between hybrid process and batch process, showing a 300% cost reduction, depending on processed volumes and batch cycles.

Continuous countercurrent tangential chromatography for mixed mode post-capture operations in monoclonal antibody purification

Continuous Countercurrent Tangential Chromatography (CCTC) has been shown to demonstrate significant advantages over column chromatography including higher productivity, lower operational pressure, disposable flow path, and lower resin use. Previous applications of CCTC have been limited to initial capture of monoclonal antibodies (mAb) from clarified cell culture harvest. In this present article, a CCTC system was designed and tested for a post-capture antibody purification step. Mixed mode cation exchange-hydrophobic interaction chromatography resins with two different particle sizes were used to reduce host cell protein (HCP), leached protein A, DNA, and aggregates from a mAb stream after a protein A operation. Product output from CCTC was obtained at a steady-state concentration in sharp contrast to the periodic output of product in multi-column systems. The results show up to 101g of mAb/L of resin/hr productivity, which is 10× higher than in a batch column. A 5% yield increase (95% with CCTC vs. 90% in batch column) resulted from optimizing elution pH within a narrow operational window (pH 4-4.5). Contaminant removal was found to be similar to conventional column performance. Data obtained with the smaller particle size resin showed faster binding kinetics leading to reduced CCTC system volume and increased productivity. Buffer and water usage were modeled to show potential for utilization of in-line mixing and buffer tank volume reduction. The experimental results were used to perform a scale up exercise that predicts a compact CCTC flow path for 500 and 2000L batches using commercially available membranes. These results demonstrate the potential of using CCTC for post-capture operations as an alternative to packed bed chromatography, and provide a framework for the design and development of an integrated continuous bioprocessing platform based on CCTC technology.

Continuous counter-current chromatography for capture and polishing steps in biopharmaceutical production

The economic advantages of continuous processing of biopharmaceuticals, which include smaller equipment and faster, efficient processes, have increased interest in this technology over the past decade. Continuous processes can also improve quality assurance and enable greater controllability, consistent with the quality initiatives of the FDA. Here, we discuss different continuous multi-column chromatography processes. Differences in the capture and polishing steps result in two different types of continuous processes that employ counter-current column movement. Continuous-capture processes are associated with increased productivity per cycle and decreased buffer consumption, whereas the typical purity-yield trade-off of classical batch chromatography can be surmounted by continuous processes for polishing applications. In the context of continuous manufacturing, different but complementary chromatographic columns or devices are typically combined to improve overall process performance and avoid unnecessary product storage. In the following, these various processes, their performances compared with batch processing and resulting product quality are discussed based on a review of the literature. Based on various examples of applications, primarily monoclonal antibody production processes, conclusions are drawn about the future of these continuous-manufacturing technologies.