Cell culture processes for monoclonal antibody production

Animal cell culture technology has advanced significantly over the last few decades and is now generally considered a reliable, robust and relatively mature technology. A range of biotherapeutics are currently synthesized using cell culture methods in large scale manufacturing facilities that produce products for both commercial use and clinical studies. The robust implementation of this technology requires optimization of a number of variables, including (1) cell lines capable of synthesizing the required molecules at high productivities that ensure low operating cost; (2) culture media and bioreactor culture conditions that achieve both the requisite productivity and meet product quality specifications; (3) appropriate on-line and off-line sensors capable of providing information that enhances process control; and (4) good understanding of culture performance at different scales to ensure smooth scale-up. Successful implementation also requires appropriate strategies for process development, scale-up and process characterization and validation that enable robust operation and ensure compliance with current regulations. This review provides an overview of the state-of-the art technology in key aspects of cell culture, e.g., generation of highly productive cell lines and optimization of cell culture process conditions. We also summarize the current thinking on appropriate process development strategies and process advances that might affect process development.

Key words: monoclonal antibody, expression systems, cell line engineering, cell culture process development, optimization scale-up and technology transfer, process advances

Introduction

With the increasing number of protein therapeutic candidates, especially monoclonal antibodies (mAbs) entering various stages of development, biopharmaceutical companies are increasingly looking at innovative solutions to deliver this pipeline. For antibody manufacturing process development, maintaining desired quality attributes while reducing time to market, maintaining cost effectiveness, and providing manufacturing flexibility are key issues in today's competitive market, where several companies are often working on therapies for similar targets and clinical indications. Since antibody therapies may require large doses over a long period of time, manufacturing capacity becomes an issue because the drug substance must be produced in large quantities with cost and time efficiency to meet clinical requirements and pave the way toward commercialization. In response to the strong demand, many companies have built large scale manufacturing plants containing multiple 10,000 L or larger cell culture bioreactors.

In terms of manufacturability and scalability, mammalian cells have historically been considered difficult to work with due to factors such as low yield, medium complexity, serum requirement, and shear sensitivity, although the latter has generally been incorrectly overemphasized. After two decades of intensive development work in cell line, media and bioreactor condition optimization, cell specific productivity of over 20 pg/cell/day can be routinely achieved for production cell lines; 1 high titers up to ∼10 g/L and cell densities of over 20 million cells/mL in fed-batch processes have been recently reported by a few companies at major conferences. The enhancement of specific productivity per cell is achieved not only by selection of highly productive clones, but also by optimization of medium composition and bioreactor operation conditions. Today, the combination of high titers and large capacity has gradually shifted the focus of cell culture process development from pursing even higher titers to controlling product quality and process consistency at all development stages and production scales. 3

Cell culture process development starts with cell line generation and selection, followed by process and media optimization in small scale systems, including 96-well plates, shaker flasks, and bench-scale bioreactors, for high throughput screening purposes. Once conditions are defined, the process is often transferred to a pilot scale to test scalability and produce material for preclinical toxicology studies, and then larger scale manufacturing for production of clinical material under current good manufacturing practices (cGMP) regulations. Once development of a commercial cell culture process for production of a biological product is completed at the laboratory and pilot scales, the commercialization process begins with process characterization, scale-up, technology transfer, and validation of the manufacturing process. 2

As cell culture technology is maturing, the biopharmaceutical industry has applied platform processes to satisfy material demand and quality requirements within a short period of time. The cell culture platform often consists of common host cell, expression vector, transfection and selection methods during cell line generation, and standard cell culture media, process control and scale up methodologies during process optimization. This approach not only enables fast process development, but also provides predictable performances in scale up, facility fit and downstream process integration.

Mammalian Expression Systems

Therapeutic antibodies are mainly produced in mammalian host cell lines including NS0 murine myeloma cells, PER.C6® human cells, and Chinese hamster ovary (CHO) cells. 4 – 8 The selection of expression system is determined by its ability to deliver high productivity with acceptable product quality attributes and the preferences of individual companies, which is often influenced by their historical experiences.

Murine NS0 cells are non-immunoglobulin secreting myeloma cells that are cholesterol auxotrophs requiring the presence of cholesterol in culture medium for growth; 9 however, cholesterol-independent NS0 cells also have been established. 10 – 12 NS0 cells lack endogenous glutamine synthetase (GS) enzyme activity making them suitable for use with GS as a selectable marker for recombinant antibody expression. 13 High antibody productivity has been reported from non-GS NS0 cell lines as well. 14 , 15 Mouse-derived cell lines, including NS0, produce N-glycolylneuraminic acid (NGNA; a sialic acid that cannot be synthesized by humans) at appreciable levels. This sialic acid form was initially believed to present a potential immunogenicity concern in humans. It was later shown that CHO cells can express low levels of NGNA and that humans apparently incorporate NGNA into proteins from dietary sources, which tempered immunogenicity concerns. 16 – 18 Murine cells, including NS0, do produce alpha-Gal-alpha(1,3) Gal linkages, which humans have been shown to express antibodies against. Although NS0 cells have been used in industry to produce therapeutic antibodies, these potential immunogenicity aspects have likely limited use of these cells for therapeutic antibody production.

Compared to NS0 and CHO cells, PER.C6® cells embody a relatively new technology. Cells are derived from human embryonic retina cells that have been immortalized by transfecting the E1 genes from adenovirus 5 DNA. 19 Like NS0 and CHO cells, PER.C6® cells can proliferate indefinitely in suspension under serum-free conditions.

CHO cells are the predominant host used to produce therapeutic proteins. About 70% of all recombinant proteins 20 produced today are made in CHO cells, including DUXB11, DG44 and CHOK1 lineages. DUXB11 and DG44 cells do not have dihydrofolate reductase (DHFR) activity, while CHOK1 cells have endogenous DHFR activity.

Cell Line Development

The process for development of a stable cell line starts with expression vector construction and transfection. After being transfected with plasmids bearing the antibody light and heavy chain genes, as well as selectable marker or markers, cells are screened for high productivity following growth recovery, serum-free suspension adaptation and amplification (if necessary) and clone selection. The screening and selection of a highly productive and stable clone from the transfectant population in a limited time frame is a major challenge.

Mammalian expression vectors typically contain one cassette for antibody genes and selectable marker gene(s) for expression in mammalian cells, and a second cassette for the genes enabling plasmid replication in bacteria. To achieve high levels of antibody expression, strong promoter/enhancers such as the cytomegalovirus (CMV) promoter 21 and elongation factor alpha (EF1α) promoter 22 are used to drive antibody heavy chain and light chain expression. Often an intron sequence in the 5′ untranslated region is included after the promoter/enhancer to increase export of transcribed mRNA to the cytoplasm from the nucleus, and one or more 3′ polyadenylation signal sequences are included to maximize mRNA levels. Commonly used polyadenylation signal sequences are the SV40 late or early polyadenylation signal sequences and the bovine growth hormone polyadenylation sequence. In addition to transcription, translation and secretion are also required for antibody production. Typically, a consensus Kozak sequence 23 is created by placing GCC GCC(A/G)CC immediately in front of the first translation initiation codon to enhance translation initiation, while a signal peptide sequence is placed immediately in front of the mature antibody peptide to direct antibody protein secretion. 13

A variety of transfection methods have been developed to stably introduce vector DNA into mammalian cells, including calcium phosphate, electroporation, cationic lipid-based lipofection, and polymer or dendrimer-based methods. 24 All four methods have been used for stable transfection, but electroporation and lipofection are the most common choices. Transfected cells are then selected, relying on different selectable markers that can be categorized into two groups; metabolic selectable markers and antibiotic selectable markers. Some commonly used selectable markers are listed in Table 1 .

Table 1

Selectable markers often used in mammalian expression vectors

CHO stable cell lines have often been selected using metabolic selective markers including methotrexate (MTX) (dihydrofolate reductase gene mediated) and methionine sulphoximine (MSX) (glutamine synthetase gene mediated). 13 Table 2 shows a selected list of approved antibody products produced in CHO cells. It has also been reported that an antibody-producing cell line can be generated using two different selectable markers together. 14 In cases where two selective markers have been used to select stable antibody-producing cell lines, the selective markers are located either in one expression construct also containing genes for heavy chain and light chain, or on two separate plasmids, each containing either the heavy or light chain gene.

Table 2

Selected list of approved antibodies produced in CHO cells

We recently explored the “double selection” approach, which simultaneously transfects two plasmids into CHO cells for stable antibody cell line generation. The unique feature of this approach is that each plasmid contains both the heavy chain and light chain genes, and one selective marker. Cells transfected with two plasmids are selected with two different selective reagents such as MTX and MSX. The productivity of clones generated using this approach was higher than that of clones transfected with either plasmid alone, as shown in our 96-well productivity assay ( Fig. 1 ). To our knowledge, this is the first time that simultaneous transfection with two expression constructs and selection with two different selective markers has been successfully demonstrated as a means to generate highly productive stable CHO cell lines expressing antibody.

96-well Elisa assay of clones from single and double selection. For each case, 72 clones were screened. [Notes: MTX, methotrexate; MSX, methionine sulphoximine].

To generate stable cell lines with adequate productivity for clinical or commercial material production, hundreds to thousands of clones may be screened. The primary screen is usually an ELISA assay with or without cell number normalization, to eliminate non- or low producers. While high producers are scaled up, additional assays are performed to measure cell growth, cell specific productivity, and volumetric productivity (titer) in order to choose the top 12–24 clone candidates, which are typically further analyzed in a fed-batch cell culture scale-down models such as shake flasks or laboratory scale bioreactors. Product quality attributes such as glycosylation profile, charge variants, aggregate levels, protein sequence heterogeneity, as well as cell culture characteristics including growth, specific productivity, volumetric productivity, and clone stability, are assessed to enable selection of the top 4–6 clones for further evaluation in bioreactors, after which the final production clone and backup clone are chosen.

Cell Line Engineering

A significant amount of work has been done to genetically engineer production host cells to improve or modify the product quality or improve the host cell robustness. Glycosylation control has received a lot of attention because glycan structures on antibodies can have substantial effects on clearance rate and bioactivities. 25 Antibodies produced in CHO cells typically have complex biatennary structures with very low or no bisecting-Nacetylglucosamine (bisecting GlcNAc) and high levels of core fucosylation. 26 Overexpression of N-acetylglucosaminyltransferase III has been used to increase the fraction of bisecting GlcNAc that resides on antibodies to improve antibody-dependent cellular cytotoxicity (ADCC). RNAi and gene deletion technologies have also been used to decrease or eliminate the fucose on antibodies to dramatically increase ADCC activity. 27 , 28 In general, glycosylation is difficult to control precisely in mammalian cells as it is dependent on a variety of factors such as clonal variations, media, as well as culture conditions.

Other areas of host cell engineering include approaches to decrease programmed cell death, reduce lactate accumulation, and manipulate cell growth. Overexpression of anti-apoptotic gene or genes and RNAi-technology mediated knock-down expression of apoptotic gene or genes have been used to extend the culture viability that leads to improved productivity. 29 Since CHO cell and other continuously cultured cells have low efficiency in completely oxidizing glucose to CO₂ and H₂O, one by-product of cell culture process is lactate accumulation, which can cause acidification of culture medium and lead to high osmolarity and low viability due to the alkali added to control the medium pH. A significant amount of work 30 – 32 has been performed to reduce lactate accumulation; however, the usefulness of this approach may be very clone dependent. 31

Another area of research has focused on the use of inducible expression systems in mammalian cells. This strategy has the advantage of decoupling cell growth from product formation. Growth arrest in NS0 cultures via the inducible expression of p21 was reported to result in a significant increase in cell specific productivity. 33 Current practice for the selection of high producing clones involves a time-consuming and laborious screening strategy due to the fact that the random integration of the transgene of interest gives rise to very different expression levels due to variation in the chromosomal surroundings or unpredictable cross-interactions of multiple gene copies. 34 Several strategies have been proposed to overcome the positional dependency of random integration. One of the most promising methods is the use of homologous recombination systems for site-specific gene integration such as the Flp/FRT system from S. cerevisiae and the Cre-lox system from the bacteriophage P1 in eukaryotic cells. Coroadinha et al. 35 used the Flp/FRT system to target gene insertion into a high expression chromosomal locus and succeeded in establishing a viral packaging 293 cell line for consistent high-titer virus production. Fukushige and Sauer 36 demonstrated the use of a lox recombination vector to obtain stable transformants with predictable gene expression profiles. The positive selection vector system was designed to directly select Cre-mediated DNA integration at a lox target (using an inactive lox-neo fusion gene) previously placed into the genome of cultured cells. This technique ought to allow the rapid and efficient exchange of a single copy of the transgene of interest with no change in expression levels.

A pre-requisite to the application of this promising technology is the identification of integration sites that lead to high expression; however, it should be possible to investigate the position effects on gene expression using the site-specific DNA integration Flp/FRT and Cre-lox methods. For example, transfection of DHFR deficient CHO cells with a loxP-GFP fusion and DHFR genes and high-throughput screening via FACS was used to identify transcription active sites. 37 Simultaneous transfection with two expression constructs and selection with two different selective markers as a means to generate highly productive stable CHO cell lines also appears promising. Overall, these methods should result in greater efficiencies in cell line screening for high producers and a further reduction in development timelines.

Several alternative expression systems such as Pichia pastoris and Escherichia coli have recently emerged as promising hosts for mAb secretion. 38 Researchers at Glycofi (a subsidiary of Merck & Co., Inc., NJ) have successfully demonstrated the feasibility of glyco-engineered P. pastoris cell lines to produce mAbs with highly specific glycoforms. 39 Several different glycoforms of commercially available Rituximab (Rituxan; Genentech Inc., CA) were generated, and binding to Fc. receptors and ADCC activity were measured. This study demonstrated a 10-fold increase in binding affinity, as well as enhanced ADCC activity with the glycan-engineered proteins compared with Rituximab. Controlling the glycan composition and structure of IgGs thus appears to be a promising method for improving the efficacy of therapeutic mAbs that utilize ADCC for biological activity. Coupled with the use of well-established P. pastoris as a platform, processes that include high cell density cultures, scalability, cost-effectiveness and existing large scale fermentation capacity can allow for high-fidelity production of human glycosylated therapeutic proteins.

E. coli has been most commonly used for production of antibody fragments such as Fabs that are utilized when Fc-mediated effector functions are not required or deleterious. 39 Simmons et al. 40 demonstrated that efficient secretion of heavy and light chains in a favorable ratio resulted in the high-level expression and assembly of full-length IgGs in the E. coli periplasm. The technology described offers a rapid and potentially inexpensive method for the production of full-length aglycosylated therapeutic antibodies that do not have ADCC functionality. Mazor et al. 41 also showed that it was possible to obtain full-length antibodies from combinatorial libraries expressed in E. coli. The full-length secreted heavy and light chains assembled into aglycosylated IgGs that were captured by an Fc-binding protein located on the inner membrane. Flow cytometry was used after permeabilization of the membrane and attachment of the antibody to a fluorescent antigen.

Aspergillus niger has also been used for the production of mAbs or antibody fragments; Ward et al. 42 used N-terminal fusion to glucoamylase for both heavy and light chains to express a full length IgG in this fungus. In addition, the use of cell-free protein synthesis for recombinant protein production is emerging as an important technology. Goerke and Swartz 43 recently demonstrated the utility of the technology using E. coli cell extracts to produce a number of proteins, antibody fragments and vaccine fusion proteins, with correct folding and presence of disulfide bonds.

Platform Process Development

Due to the high degree of uncertainty associated with clinical studies, process development for biopharmaceuticals is often divided into an early and late stage, with each having different emphasis ( Fig. 2 ). The goal of early stage development is to rapidly develop bioprocesses to produce materials for Phase 1 or 2 clinical trials and animal toxicology studies. In order to accelerate filing of an investigational new drug (IND) application for proof-of-concept clinical studies, it is becoming increasingly necessary for companies to deliver their pipelines efficiently by utilizing streamlined cell culture platform processes that include standardized process conditions and procedures. Use of a platform process allows acceleration of early stage cell culture process development activities, e.g., clone selection, process lock and technology transfer to clinical manufacturing. The similarity of molecular characteristics and properties among different mAbs makes the platform approach feasible, although the processes may not be fully optimized for every molecule.

Clinical and process development flowchart. [Notes: POC, proof of concept; IND, investigational new drug application; Tox, Toxicology; BLA, biologics license application; TT, technology transfer; cGMP MFG, current good manufacturing practices compliant manufacturing; PD, process development].

As the product moves into late stage development, i.e., for Phase 3 and commercial production, the processes can be further optimized. Late stage process development is focused on improvements of process yield, robustness, scalability and regulatory compliance. Optimization of the process is an integrated activity involving clone selection, medium development, and bioreactor condition optimization, which is followed by scale-up to an appropriate manufacturing facility. Product quality and comparability needs to be closely monitored when process changes occur during both early and late stage development to ensure patient safety. To gain regulatory approval for commercialization, processes also need to be characterized to evaluate the effects of process parameters on process performance and product quality; the process should also be validated to demonstrate process consistency before commercial cGMP production.

Clone Selection

Selection of the final production clone is generally considered to be one of the most critical decisions in both early and late stage cell culture process development. Since changes in production cell lines during clinical development are considered major process changes, product comparability must be demonstrated if the cell line is changed during late stage development. Changing the cell line after Phase 3 clinical study typically requires additional human clinical studies. It is thus important to select the right clone prior to Phase 3 production of drug substance, and preferably at the Phase 1 stage.

After being transfected, cells are diluted and cultivated in 96-well plates with a basal growth medium and screened for robust cell growth and high productivity. At this stage, in order to predict clone performance in large-scale production bioreactors, an enriched medium that is similar to the final production medium formulation and a similar feeding regime can be tested in shake flasks or in small-scale bioreactors. Several clone attributes should be considered and evaluated for features such as product quality, manufacturability, and volumetric productivity.

Maintaining consistent and comparable product quality is a challenge if changes to cell line, media or other process changes are made as product candidates move forward from small-scale development lab to pilot plant scale, and eventually to commercial scale cGMP manufacturing. 44 – 46 Among these variables, the cell line has the most significant impact on many quality attributes because these attributes are clone dependent. Some common analytical assays and quality assessment criteria employed during clone selection to test mAb molecular properties are summarized in Table 3 .

Table 3

Product quality assessment during clone selection

CE, capillary electrophoresis; IEF, Isoelectric focusing; iCIEF, Imaged capillary isoelectric focusing.

Process yield is another critical criterion used to select the production clone. Since antibody expression rate in mammalian cells is usually non-growth associated, the final titer is equal to specific productivity Qp multiplied by the integral of viable cell density over culture duration, i.e., Titer = Qp• ∫ X dt. To date, typical production cell line specific productivities range from 20 pg/cell/day to 70 pg/cell/day and peak viability cell densities from 5–30 × 10 6 cells/mL in a 10–14 day fed-batch process.

Cell line stability is another factor that should be considered since volumetric and specific productivity decline as cell age increases for some cell lines. Such unstable clones are not suitable for large-scale production since cell age increases with scale as the cell culture process is scaled up through serial culture passages of the seed train and inoculum train. In addition to cell line stability, growth and metabolite characteristics that can affect process robustness and scalability also need to be assessed. Robust cell growth with high viability and low lactate synthesis is usually desirable. High lactate producing clones are not preferred in order to avoid the dramatic osmolality increase that accompanies the addition of base needed to maintain pH.

Screening and selection of highly productive and scalable clones among the transfectant population in a limited time frame is still a major challenge because the product quality, productivity and even cell metabolic profiles are often dependent on cell culture conditions. Using miniaturized high throughput bioreactors with full process parameter controllability to mimic the large-scale bioreactor environment could help to identify the best production clone at a very early stage.

Medium and Feeding Strategy Development

In general, medium development for a fed-batch process involves batch medium and feed concentrate development, as well as feeding strategy optimization. Several approaches can be used systematically, such as single-component titration, spent medium analysis, and medium blending. 47 , 48 Due to safety concerns related to transmissible spongiform encephalopathy (TSE) and other contaminants, bovine serum and animal-derived raw materials should be avoided if possible. After two decades of media development and host cell adaptation, fully chemically defined media consisting of amino acids, vitamins, trace elements, inorganic salts, lipids and insulin or insulin-like growth factors, have been developed and implemented in large-scale mAb production, but not all antibody production cell lines can achieve high yield in chemically defined media. Addition of animal-component-free hydrolysates to chemically defined media is a common approach to increase cell density, culture viability and productivity in a timely manner. Hydrolysates are protein digests composed of amino acids, small peptides, carbohydrates, vitamins and minerals that provide nutrient supplements to the media. 49 , 50 Non-animal derived hydrolysates from soy, wheat and yeast are used commonly in cell culture media and feeds; however, because of its composition complexity and lot-to-lot variations, hydrolysates can be a significant source of medium variability.

While the most common approach to develop a feed medium is to concentrate the basal medium, sophisticated optimization of feed composition and feeding strategy requires consideration of nutrient consumption, by-product accumulation and the balance between promoting growth versus volumetric productivity. 51 , 52 Previous studies indicated that by-products such as lactate and ammonia could be minimized by maintaining low glucose and glutamine concentrations through frequent or continuous feeding; 53 however, the operational complexity and cost of validating continuous feeding strategies have generally made them less desirable for large-scale manufacturing. Step-wise bolus addition of the feed solution to the production bioreactor is most widely used in industry due to its simplicity and scalability. In general, medium development is labor-intensive and time-consuming. A combination of high-throughput cell culture scale-down systems with statistical design of experiment (DOE) approaches is commonly applied to shorten development time. 54 , 55

While optimization of cell culture media is often considered to be cell line dependent and best accomplished if based on the metabolism and nutrient consumption of specific cell lines, the aggressive timelines under which cell culture processes are developed requires development of a “platform” approach for optimization of cell culture processes. While the platform process might not provide the greatest volumetric productivity that could be achieved with specific cell lines, it will have wide applicability across multiple cell lines such that it can be implemented with minimal modifications for cell lines derived within the company. Hence, development of the platform process is accomplished with multiple cell lines that are representative of the various growth, productivity and metabolic phenotypes commonly observed. If business need dictates that processes for specific cell lines be optimized further, the platform process could be used as a starting point to enhance the cell culture process to achieve specific process goals such as higher volumetric productivities. Titers as high as 8 g/L have been achieved with such process enhancements; Figure 3 illustrates antibody concentration profiles for the same cell line when operated under the platform media or enhanced media.

The antibody concentration profile shown for the same cell line, but grown with “platform” media, which will be applicable across multiple cell lines with minimal modifications and the “enhanced” media, that is specifically optimized for maximizing the volumetric productivity of this cell line.

Bioreactor Optimization and Scale Up

Culture operating parameter optimization is required to achieve high expression of product with acceptable product quality profiles. These parameters are physical, chemical and biological in nature. Physical parameters include temperature, gas flow rate and agitation speed, while chemical parameters include dissolved oxygen and carbon dioxide, pH, osmolality, redox potential and metabolite levels, including substrate, amino acid and waste by-products. Biological parameters are used for determining the physiological state of the culture and include viable cell concentration, viability and a variety of intracellular and extra-cellular measurements such as NADH, LDH levels, mitochondrial activity and cell cycle analysis. Variations in the micro-environment parameters from optimal levels can have a dramatic impact on culture performance, productivity and product quality. A typical stirred tank bioreactor is equipped with temperature, pressure, agitation, pH and dissolved oxygen controls. Figure 4 illustrates the affects of cell culture operating strategies and parameters on culture environmental conditions such as dissolved oxygen (DO), pH, osmolality, dissolved CO₂, mixing, hydrodynamic shear and how the environment consequently influences measures of process performances such as cell growth, metabolite concentrations, product titer and product quality.

Cell culture process operating parameters affect process performance and product quality.

Due to the complexity of protein products that include isoforms and microheterogeneities, the performance of the cell culture process can have significant effects on product quality and potency, especially with respect to glycosylation, post-transcriptional modifications and impurity profiles. 44 – 46 , 56 Therefore, the bioreactor operating parameters have to be optimized and characterized thoroughly to improve process performance and understanding of how the process affects product quality. Significant progress has been made in the last two decades in understanding the impact of the cellular environment on culture physiology and its subsequent impact on productivity, product quality and downstream processes.

Another reason for the resurgence of research activity and innovation in this area can be attributed to the United States Food and Drug Administration's (FDA) process analytical technology (PAT) initiative. 57 The PAT directive is a “system for designing, analyzing, and controlling manufacturing through timely measurements (i.e., during processing) of critical quality and performance attributes of raw and in-process materials and processes, with the goal of ensuring final product quality”. It also encourages a better understanding of the manufacturing process by identifying relationships between process parameters and reproducibility, culture performance and product quality attributes. Although originally conceptualized for small molecule manufacturing processes, it is increasingly being extended to biological processes, which are inherently more complex. 58

Process parameters can be measured either on-line (or at-line by direct connection to calibrated analyzers) or off-line via operator intervention. Typical examples of off-line measurements include pH (usually for verification of on-line pH readings), cell counting and viability measurements using a hemocytometer or automated cell counters, packed cell volume, osmolality and certain metabolite concentrations. Accurate gas and liquid flow measurements are typically conducted using mass flow meters and magnetic meters. Temperature can be measured accurately using commercially available resistance temperature devices (RTD), although thermocouples can also be used; this parameter is usually shifted during the course of the fed-batch culture to extend culture longevity, potentially by manipulating the cell cycle. The temperature shift of the culture is often from 37°C to 30–35°C at 48 hours post inoculation, which can retain cells in G₁ phase longer, and therefore delay the onset of apoptosis. 59 – 61

Dissolved oxygen is typically controlled at a specific set point, usually between 20–50% of air saturation in order to prevent dissolved oxygen limitation, which might lead to excessive lactate synthesis, and excessively high dissolved oxygen concentrations that could lead to cytotoxicity. 62 The Clark type electrode is still the most commonly used for measurement of dissolved oxygen. In this type of electrode, oxygen diffuses through a permeable membrane and is reduced at a negatively polarized cathode (platinum) with respect to a reference anode. The cathode and anode are separated by an electrolyte solution and the reduction of oxygen generates a voltage dependent current that is directly proportional to the dissolved oxygen concentration. Although cell growth is relatively insensitive to dissolved oxygen in the range 20–100% air saturation, 63 , 64 the dissolved oxygen level can significant affect product quality. Kunkel et al. reported that reduction in dissolved oxygen caused decreased glycosylation of antibody N-glycan chains. 65

Dissolved CO₂ is also an important process variable because it can accumulate to inhibitory levels at values greater than 120–150 mm Hg 66 – 68 and affects product quality. Even though dissolved CO2 sensors are commercially available, e.g., from YSI Inc., (Yellow Springs, OH) or Metler Toledo (Columbus, OH), dissolved CO₂ is still measured using off-line blood gas analyzers such as those from Nova Biomedical (Waltham, MA). The use of in-situ sensors is not required because it is generally possible to match CO₂ profiles at different scales by the correct choice of bioreactor sparger design, agitation speed and gas sparge rates. Measurement of oxygen uptake and CO₂ production rates can also be achieved using on-line mass spectrometry. Unlike microbial fermentations, this type of analysis is rarely conducted due to the cost of such instrumentation and the lack of sensitivity of measurements at the very low rates of metabolism commonly observed in animal cells.

Since even a small deviation of 0.1 units from the optimal pH value can significantly impact culture growth and metabolism, in particular glucose consumption and lactate production, pH is an important variable to measure and control. 69 , 70 Cell culture media usually contains sodium bicarbonate as buffering agent, and pH is usually tightly controlled with a combination of CO₂ sparging to reduce pH and base addition to increase it. High pH (≥7.0) is usually preferred for initial cell growth phase, which is usually accompanied by lactate accumulation. When lactate accumulation exceeds the buffering capacity of the culture medium, pH drifts downward, which could trigger base addition leading to increased osmolality of the culture medium. This could be risky in cell lines that synthesize excessive amounts of lactate since high pH, high lactate and high osmolality cascade often causes delayed cell growth and accelerated cell death. When cell growth has ceased, lactate is either produced at a much lower rate or consumed. The concomitant upward drift in pH is counteracted by CO₂ sparging. Thus, the pH set-point and control strategy, e.g., dead band, are intimately linked to dissolved CO₂ levels, base consumption for pH control and therefore, osmolality.

While a pH control strategy characterized by a wide dead band around the set-point that would allow the culture pH to drift without triggering the addition of base or CO₂, could be a viable alternative to control either the osmolality or dissolved CO₂, it is generally not preferred due to potential variability in pH profiles that could be observed in different scales. Thus, balancing the impact of pH on cell growth, lactate synthesis, osmolality and dissolved CO₂ profiles needs to be a key consideration during process optimization. These considerations make the accurate measurement of pH even more imperative. pH probes typically consist of a 0.2–0.5 mm glass membrane fabricated from silicate groups containing sodium that form a hydrated gel layer on the membrane when placed in liquid. An Ag/AgCl₂ electrode in KCl electrolyte saturated with AgCl₂ is used to measure the change in potential of the outer surface of the membrane caused by changes in the medium pH. Use of pH probes for extended culture duration could lead to drift and reduced sensitivity, and hence on-line measurements are verified with periodic off-line measurements.

Most cell culture media are designed to have an osmolality in the range 270–330 mOsm/kg. Culture osmolality is routinely measured using freezing-point depression osmometry. Various commercial systems are available, although the analyzers from Advanced Instruments (Norwood, MA) are the most commonly employed in cell culture and are capable of measuring osmolality in the range of 0–1,500 mOsm/kg of water. The impact of osmolality is cell line specific; deZengotita et al. reported growth inhibition with increasing osmolality and effects on cell specific productivity. 71 These deleterious effects could be exacerbated when combined with high dissolved CO₂ levels that could occur in high cell density cultures, 72 and hence it is vital to ensure during process development that the osmolality profile is acceptably low, especially towards the latter stages of the cell culture process. There are also examples, however, where a high culture osmolality has been used to leverage an increase in specific productivity balanced with a reduction in cell growth to yield an increased volumetric productivity compared to lower osmolality. 73 , 74

Cell culture metabolites such as glucose, lactate, glutamine and glutamate are commonly measured off-line using enzymatic biosensors specific to the measured analyte. These measurements are important not only for maintaining substrate levels above critical levels via feeding strategies, but also in developing processes with reduced by-product formation. Commercially available instruments include the YSI 2700 from YSI Inc., (Yellow Springs, OH) or Nova Bioprofile 400 from Nova Biomedical (Waltham, MA). These analyzers employ biosensors where the reaction of a substrate with the enzyme produces a product that can be readily measured. For example, glucose can be detected using glucose oxidase in the presence of excess oxygen to produce gluconic acid and hydrogen peroxide. A second reaction between fluorescein and the H₂O₂ produced from the first reaction produces a fluorescent signal that correlates directly to the glucose concentration. In addition to the quantification of metabolites, the Nova Bioprofile 400 can also measure pH, dissolved gases (O₂ and CO₂), NH₄ + (0.20–25.00 mM), Na + (40.0–220.0 mM), K + (1.00–25.0 mM) and Ca ++ (0.10–10.0 mM). It is important to point out that accurate measurements with these systems require proper maintenance and calibration procedures.

Cell concentration and viability measurements are critical in developing cell culture processes and are used for determining culture physiology in response to operating conditions and calculation of growth rates, specific consumption/production rates of metabolites and cell specific productivity. The most common method for measuring cell concentration and viability is via Trypan Blue exclusion microscopy. This method depends upon the ability of cells with intact membranes, i.e., live cells, to exclude Trypan Blue; those that stain blue are classified as dead cells. A number of automated analyzers that exploit this method and are coupled to image analysis are commercially available (Cedex, Innovatis, Bielefeld, Germany and Vi-Cell, Beckman Coulter, Fullerton, CA). These analyzers also allow the determination of cell size. In many cell culture processes, the mean cell size can change by as much as 50% (or over a 3-fold change cell volume). 75 In these cases, it is insufficient to measure viable or total cell concentration. Instead, packed cell volume (or viable packed cell volume) is determined using centrifugation based methods; this is more likely to provide an accurate representation of the cell mass since it avoids instrument associated variability, which is especially useful during technology transfer between different sites.

The Trypan Blue exclusion method does not allow measurements other than live or dead. Multi-parameter flow cytometry using fluorescent dyes such as propidium iodide and annexin V or caspase 5 can be used to quantify live/dead cells and apoptotic cell populations. This is now possible in cell culture laboratory settings using relatively simple 96-well plate based systems and specifically designed measurement kits for such analyses, as well as a multitude of other cell based assays (Guava Technologies, Hayward, CA). Measurements of cell metabolic activity can be quantified by on-line oxygen uptake rate measurements or off-line cell mitochondrial activity using FACS.

After development, process performances achieved on small scales should be maintained during scale up. A typical large-scale cell culture process consists of a number of unit operations, including seed train, inoculum train, and production run ( Fig. 5 ). Each step has its key process performance indicators such as cell growth, viability and titer, along with appropriate product quality attributes. The success of process scale up is usually measured by these key process indicators and product quality attributes that meet pre-defined criteria.