Different fermentation processes produced variants of an anti-CD52 monoclonal antibody that have divergent in vitro and in vivo characteristics

The anti-CD52 antibody has already been approved for the treatment of patients with resistant chronic lymphocytic leukemia, relapsing-remitting multiple sclerosis, and has demonstrable efficacy against stem cell transplantation rejection. A CHO cell line expressing a humanized anti-CD52 monoclonal antibody (mAb-TH) was cultivated in both fed-batch and perfusion modes, and then purified. The critical quality attributes of these mAb variants were characterized and the pharmacokinetics (PK) properties were investigated. Results showed that the perfusion culture achieved higher productivity, whereas the fed-batch culture produced more aggregates and acid components. Additionally, the perfusion culture produced similar fucose, more galactose and a higher proportion of sialic acid on the anti-CD52 mAb compared to the fed-batch culture. Furthermore, the perfusion process produced anti-CD52 mAb had higher complement-dependent cytotoxicity (CDC) efficacy than that produced by the fed-batch culture, a result probably linked to its higher galactose content. However, antibody produced by fed-batch and perfusion cultures showed similar PK profiles in vivo. In conclusion, perfusion is a more efficient method than fed-batch process in the production of functional anti-CD52 monoclonal antibody. Product quality variants of anti-CD52 mAb were found in different cell culture processes, which demonstrated different physiochemical and biological activities, but comparable PK properties. Whether these observations apply to all mAbs await further investigation.     

Effect of process change from perfusion to fed-batch on product comparability for biosimilar monoclonal antibody

A fed-batch process for the production of biosimilar monoclonal antibody was developed. Since the brand product is produced by perfusion process, the impact of process change from perfusion to fed-batch on product quality and cell performance was evaluated. Perfusion culture was performed at 0.47–1.00 (v/v/d) perfusion rate by spin-filter method with 15–17 μm mesh. Culture parameters such as pH (6.8–7.2), dissolved oxygen (40–70% air saturation), temperature (37 °C) and agitation speed (250 rpm) were applied in both culture modes. In terms of cell performance, volumetric productivity increased 3.7 times while process performance increased 7.5 times in fed-batch culture due to 10 times higher scalability. Considering the glycosylation pattern and charge variants, no significant changes in product quality were observed upon process change, although intact IgG level slightly decreased in fed-batch mode. The change of production media showed more effect on glycosylation patterns than the operation in different culture modes. Furthermore, there were no differences in biological activity, including TNFα, FcγRIIIa, and C1q-binding affinity. Through a scale-up study from 3 L to 12,500 L, it was confirmed that cell performance and product quality could be maintained. In conclusion, product quality of the fed-batch process was comparable to that of the reference product.     

Achievement of high cell density and high antibody productivity by a controlled-fed perfusion bioreactor process

Controlled feeding of nutrient supplements to a cell culture to enhance monoclonal antibody productivity has been practiced widely in high-yield, fed-batch processes. In this study, a similar feeding concept has been applied to a perfused culture and evaluated for the effects on bioreactor productivity and product quality. Our experimental results show that, by using such a "controlled-fed perfusion" approach, the volumetric antibody productivity (antibody per liter per day) was significantly increased by nearly twofold over the perfusion process, and surpassed fed-batch and batch processes by almost tenfold. The substantial boost in the overall productivity is attributable primarily to the combined effects of increased cell density as well as reduced product dilution. Both were achieved through careful nutrient supplementation in conjunction with metabolite minimization. As the manufacturing process evolved from roller bottles to the controlled-fed perfusion bioreactor system, the immunoreactivity and the cDNA sequences of the antibody were well preserved. However, the product glycosylation distribution patterns did alter. The controlled-feed perfusion process demonstrated a unique encompassment of the advantages of fed-batch and perfusion methods; that is, high product concentration with high volume throughput. Therefore, it may be very suitable for large-scale production of monoclonal antibodies.     

Polymer‐mediated flocculation of transient CHO cultures as a simple,high throughput method to facilitate antibody discovery

Most biopharmaceutical drugs, especially monoclonal antibodies (mAbs), bispecific antibodies (BsAbs) and Fc‐fusion proteins, are expressed using Chinese Hamster Ovary (CHO) cell lines. CHO cells typically yield high product titers and high product quality. Unfortunately, CHO cell lines also generate high molecular weight (HMW) aggregates of the desired product during cell culture along with CHO host cell protein (HCP) and CHO DNA. These immunogenic species, co‐purified during Protein A purification, must be removed in a multi‐step purification process. Our colleagues have reported the use of a novel polymer‐mediated flocculation step to simultaneously reduce HMW, HCP and DNA from stable CHO cell cultures prior to Protein A purification. The objective of this study was to evaluate this novel “smart polymer” (SmP) in a high throughput antibody discovery workflow using transiently transfected CHO cultures. SmP treatment of 19 different molecules from four distinct molecular categories (human mAbs, murine mAbs, BsAbs and Fabs) with 0.1% SmP and 25 mM stimulus resulted in minimal loss of monomeric protein. Treatment with SmP also demonstrated a variable, concentration‐dependent removal of HMW aggregates after Protein A purification. SmP treatment also effectively reduced HCP levels at each step of mAb purification with final HCP levels being several fold lower than the untreated control. Interestingly, SmP treatment was able to significantly reduce high concentrations of artificially spiked levels of endotoxin in the cultures. In summary, adding a simple flocculation step to our existing transient CHO process reduced the downstream purification burden to remove impurities and improved final product quality. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:1393–1400, 2017     

Repurposing fed-batch media and feeds for highly productive CHO perfusion processes

Perfusion is a cell culture mode that is gaining popularity for the manufacture of monoclonal antibodies and their derivatives. The cell culture media supporting perfusion culture need to support higher cell densities than those used in fed-batch culture. Therefore, when switching from a fed-batch to a perfusion mode, a new medium need to be developed which supports high cell densities, high productivity, and favorable product quality. We have developed a method for deriving perfusion culture media based on existing fed-batch media and feeds. We show that we can obtain culture media that successfully support perfusion cultures in a single-use rocking bioreactor system at cell-specific perfusion rates below 25 pL⁻¹ cell⁻¹ day⁻¹. High productivities and favorable product quality are also achievable.     

Conversion of a CHO cell culture process from perfusion to fed-batch technology without altering product quality

During the development of a new drug product, it is a common strategy to develop a first-generation process with the aim to rapidly produce material for pre-clinical and early stage clinical trials. At a later stage of the development, a second-generation process is then introduced with the aim to supply late-stage clinical trials as well as market needs. This work was aimed at comparing the performance of two different CHO cell culture processes (perfusion and fed-batch) used for the production of a therapeutically active recombinant glycoprotein at industrial pilot-scale. The first-generation process was based on the Fibra-Cel packed-bed perfusion technology. It appeared during the development of the candidate drug that high therapeutic doses were required (>100mg per dose), and that future market demand would exceed 100 kg per year. This exceeded by far the production capacity of the first-generation process, and triggered a change of technology from a packed-bed perfusion process with limited scale-up capabilities to a fed-batch process with scale-up potential to typical bioreactor sizes of 15m(3) or more. The productivity per bioreactor unit volume (in product m(-3)year(-1)) of the fed-batch process was about 70% of the level reached with the first-generation perfusion process. However, since the packed-bed perfusion system was limited in scale (0.6m(3) maximum) compared to the volumes reached in suspension cultures (15m(3)), the fed-batch was selected as second-generation process. In fact, the overall process performance (in product year(-1)) was about 18-fold higher for the fed-batch compared to the perfusion mode. Data from perfusion and fed-batch harvests samples indicated that comparable product quality (relative abundance of monomers dimers and aggregates; N-glycan sialylation level; isoforms distribution) was obtained in both processes. To further confirm this observation, purification to homogeneity of the harvest material from both processes, followed by a complementary set of studies (e.g. full physico-chemical characterization, assessment of in vitro and in vivo bioactivity, comparative pharmacokinetics and pharmacodynamics studies in relevant species, etc.) would be required. Finally, this illustrates the need to fix the production process early during the development of a new drug product in order to minimize process conversion efforts and to shorten product development time lines.     

13C metabolic flux analysis identifies limitations to increasing specific productivity in fed-batch and perfusion

Industrial cell culture requires substantial energy to generate protein. The protein generated is not only the product of interest (IgG in this case), but also the protein associated with biomass. Here, ¹³C-Metabolic Flux Analysis (¹³C-MFA) was utilized to compare the stationary phase of a fed-batch process to a perfusion process producing the same product by the same clone. The fed-batch process achieved significantly higher specific productivity, approximately 60% greater than the perfusion process. In spite of this, a general lack of difference was observed when globally comparing glycolysis, pentose phosphate pathway, and TCA cycle fluxes. In contrast, gross growth rate was significantly different, approximately 80% greater in the perfusion process. This difference was concealed by a significantly greater death rate in the perfusion process, such that net growth rates were both similar and near-zero. When considering gross growth rate and IgG specific productivity, total protein specific productivity (Biomass+ IgG) differed little, offering rationale for the observed central carbon pathway similarities. Significant differences were identified in anaplerotic branched-chain amino acid (BCAA) contributions by ¹³C-MFA. The perfusion process exhibited markedly higher (up to three times) BCAA catabolism, an observation often associated with increased death.     

Identification of upstream culture conditions and harvest time parameters that affect host cell protein clearance

During early stage bioprocess development, characterizing interactions between unit operations is a key challenge. Such interactions include the release of host cell enzymes early in the process causing losses in product quality downstream. Using a CHO-expressed IgG1 system, the impact of cell culture duration was investigated using a 50 L bioreactor and performing scale-down protein A purification. While antibody titer doubled during the last week of culture, the post-protein A host cell protein (HCP) levels increased from 243 to 740 ppm. Effects of pH and temperature were then explored using fed-batch ambr250 bioreactors, and parameters enabling higher titers were linked to a decrease in post-protein A product purity. These trade-offs between titer and product quality were visualized using a window of operation. The downstream space was explored further by exposing shake flask material to shear representative of disc stack centrifugation, prior to purification, and by adding polishing chromatography. While product quality decreased with progressing cultivation, cells became more shear resistant. Polishing chromatography resulted in product fragmentation which increased fourfold from Day 10 to 24, adding constraint to achieving both efficient HCP clearance as well as high monomer purities. These examples highlight the importance of adopting integrated approaches to upstream and downstream development strategies to enable whole process optimization.     

High-level production of a monoclonal antibody in murine myeloma cells by perfusion culture using a gravity settler

A perfusion system is described for the production of a human monoclonal antibody in non-secreting murine myeloma (NS0) cells that was previously shown to be difficult to produce at high levels using fed-batch culture. The perfusion system was based on the use of a commercially available cell settler as the separation device to separate the cells from the culture. Separation efficiency of the cell settler was above 98%. Based on the growth and glucose consumption rates, fresh media was added to the culture and the turnover rate for the bioreactor was set at a maximum of 1.5 times the bioreactor volume per day. The perfusion process resulted in twice the maximum viable cell densities and up to three times the total protein production in a 53-day run period when compared to the fed-batch process. In addition, charge heterogeneity of the antibody as measured by ion exchange chromatography was lower for material purified from the perfusion runs compared to fed-batch. Perfusion mode of culture using a commercially available gravity settler is therefore a viable alternative to fed-batch mode for high-level production of this monoclonal antibody in NS0 cells.     

高通量灌流培养模型在生物工艺开发中的应用研究

近年来,连续型细胞培养由于其高单位体积产量、稳定的产品质量属性以及潜在的成本节约效应正成为生物大分子制药生产的工艺焦点。相比传统的流加培养模式,灌流培养因培养的连续性、操作的复杂性,致使其反应器规模培养需消耗大量培养基,产生更高人力成本,不能满足当今加速化高效化的工艺开发需求。为获得稳健的灌流培养工艺并控制较低成本,高通量灌流培养模型被用于批量化的小规模灌流培养,进行灌流培养前期的克隆筛选、培养基筛选及工艺参数优化等工作,为后期大规模培养提供实用性数据支持,同时也被用于预测大规模培养的细胞表型和产品质量属性。重点介绍了当前高通量系统包括摇瓶/摇管系统、多平行自动化系统以及微流控体系用作灌流培养的特征、具体应用及比较,同时论述当前高通量灌流培养系统在生物工艺领域发展所面临的机遇及挑战,并展望其应用前景。     

Application of "oxygen uptake rate-amino acids" associated mode in controlled-fed perfusion culture

Controlled-fed perfusion, a new operation mode, which combines the advantages of fed-batch and perfusion, has been reported to enhance monoclonal antibody productivity. The aim of the present study was to further enrich this mode by an "oxygen uptake rate-amino acids (OUR-AA)" strategy in which the feeding of amino acids was controlled according to the variation of OUR during perfusion. And the effects of this strategy on bioreactor productivity and product quality were evaluated. Experimental results indicated that by using this "OUR-AA" approach in controlled-fed perfusion mode a high viable cell density of more than 1.9 x 10(7)cells/ml was achieved and the productivity of mAb reached 325 mg/l/d, which was significantly increased by nearly twofold over those of the perfusion and fed-batch process. The residual concentrations of selected amino acids were controlled at a relative steady level by OUR during the culture. The immunoreactivity and the purity of the antibody were well preserved as the culture process was evolving from flask to the controlled-fed perfusion mode. The primary application of "OUR-AA" approach in controlled-fed perfusion mode may present a novel control strategy to enhance the culture performance and to display the potential of this approach in automatic control field.     

Identification and classification of host cell proteins during biopharmaceutical process development

As significant improvements in volumetric antibody productivity have been achieved by advances in upstream processing over the last decade, and harvest material has become progressively more difficult to recover with these intensified upstream operations, the segregation of upstream and downstream processing has remained largely unchanged. By integrating upstream and downstream process development, product purification issues are given consideration during the optimization of upstream operating conditions, which mitigates the need for extensive and expensive clearance strategies downstream. To investigate the impact of cell culture duration on critical quality attributes, CHO-expressed IgG1 was cultivated in two 2 L bioreactors with samples taken on days 8, 10, 13, 15, and 17. The material was centrifuged, filtered and protein A purified on a 1 ml HiTrap column. Host cell protein (HCP) identification by mass spectrometry (MS) was applied to this system to provide insights into cellular behavior and HCP carryover during protein A purification. It was shown that as cultivation progressed from day 8 to 17 and antibody titer increased, product quality declined due to an increase in post-protein A HCPs (from 72 to 475 peptides detected by MS) and a decrease in product monomer percentage (from 98% to 95.5%). Additionally, the MS data revealed an increase in the abundance of several classes of post-protein A HCPs (e.g., stress response proteins and indicators of cell age), particularly on days 15 and 17 of culture, which were associated with significant increases in total overall HCP levels. This provides new insight into the specific types of HCPs that are retained during mAb purification and may be used to aid process development strategies.     

Process intensification in fed-batch production bioreactors using non-perfusion seed cultures

ABSTRACT

Although process intensification by continuous operation has been successfully applied in the chemical industry, the biopharmaceutical industry primarily uses fed-batch, rather than continuous or perfusion methods, to produce stable monoclonal antibodies (mAbs) from Chinese hamster ovary (CHO) cells. Conventional fed-batch bioreactors may start with an inoculation viable cell density (VCD) of ~0.5 × 10⁶ cells/mL. Increasing the inoculation VCD in the fed-batch production bioreactor (referred to as N stage bioreactor) to 2–10 × 10⁶ cells/mL by introducing perfusion operation or process intensification at the seed step (N-1 step) prior to the production bioreactor has recently been used because it increases manufacturing output by shortening cell culture production duration. In this study, we report that increasing the inoculation VCD significantly improved the final titer in fed-batch production within the same 14-day duration for 3 mAbs produced by 3 CHO GS cell lines. We also report that other non-perfusion methods at the N-1 step using either fed batch or batch mode with enriched culture medium can similarly achieve high N-1 final VCD of 22–34 × 10⁶ cells/mL. These non-perfusion N-1 seeds supported inoculation of subsequent production fed-batch production bioreactors at increased inoculation VCD of 3–6 × 10⁶ cells/mL, where these achieved titer and product quality attributes comparable to those inoculated using the perfusion N-1 seeds demonstrated in both 5-L bioreactors, as well as scaled up to 500-L and 1000-L N-stage bioreactors. To operate the N-1 step using batch mode, enrichment of the basal medium was critical at both the N-1 and subsequent intensified fed-batch production steps. The non-perfusion N-1 methodologies reported here are much simpler alternatives in operation for process development, process characterization, and large-scale commercial manufacturing compared to perfusion N-1 seeds that require perfusion equipment, as well as preparation and storage vessels to accommodate large volumes of perfusion media. Although only 3 stable mAbs produced by CHO cell cultures are used in this study, the basic principles of the non-perfusion N-1 seed strategies for shortening seed train and production culture duration or improving titer should be applicable to other protein production by different mammalian cells and other hosts at any scale biologics facilities.     

Enhancing the functionality of a microscale bioreactor system as an industrial process development tool for mammalian perfusion culture

Without a scale-down model for perfusion, high resource demand makes cell line screening or process development challenging, therefore, potentially successful cell lines or perfusion processes are unrealized and their ability untapped. We present here the refunctioning of a high-capacity microscale system that is typically used in fed-batch process development to allow perfusion operation utilizing in situ gravity settling and automated sampling. In this low resource setting, which involved routine perturbations in mixing, pH and dissolved oxygen concentrations, the specific productivity and the maximum cell concentration were higher than 3.0 × 10⁶ mg/cell/day and 7 × 10 ⁷ cells/ml, respectively, across replicate microscale perfusion runs conducted at one vessel volume exchange per day. A comparative analysis was conducted at bench scale with vessels operated in perfusion mode utilizing a cell retention device. Neither specific productivity nor product quality indicated by product aggregation (6%) was significantly different across scales 19 days after inoculation, thus demonstrating this setup to be a suitable and reliable platform for evaluating the performance of cell lines and the effect of process parameters, relevant to perfusion mode of culturing.     

Perfusion culture process plus H2O2 stimulation for efficient astaxanthin production by Xanthophyllomyces dendrorhous

A semicontinuous perfusion culture process (repeated medium renewal with cell retention) was evaluated together with batch and repeated fed-batch processes for astaxanthin production in shake-flask cultures of Xanthophyllomyces dendrorhous. The perfusion process with 25% medium renewal every 12 h for 10 days achieved a biomass density of 65.6 g/L, a volumetric astaxanthin yield of 52.5 mg/L, and an astaxanthin productivity of 4.38 mg/L-d, which were 8.4-fold, 5.6-fold, and 2.3-fold of those in the batch process, 7.8 g/L, 9.4 mg/L, and 1.88 mg/L-d, respectively. The incorporation of hydrogen peroxide (H(2)O(2)) stimulation of astaxanthin biosynthesis into the perfusion process further increased the astaxanthin yield to 58.3 mg/L and the productivity to 4.86 mg/L-d. The repeated fed-batch process with 8 g/L glucose and 4 g/L corn steep liquor fed every 12 h achieved 42.2 g/L biomass density, 36.5 mg/L astaxanthin yield, and 3.04 mg/L-d astaxanthin productivity. The lower biomass and astaxanthin productivity in the repeated fed-batch than in the perfusion process may be mostly attributed to the accumulation of inhibitory metabolites such as ethanol and acetic acid in the culture. The study shows that perfusion process plus H(2)O(2) stimulation is an effective strategy for enhanced astaxanthin production in X. dendrorhous cultures.     

Mass spectrometric evaluation of upstream and downstream process influences on host cell protein patterns in biopharmaceutical products

For production of different monoclonal antibodies (mAbs), biopharmaceutical companies often use related upstream and downstream manufacturing processes. Such platforms are typically characterized regarding influence of upstream and downstream process (DSP) parameters on critical quality attributes (CQAs). CQAs must be monitored strictly by an adequate control strategy. One such process-related CQA is the content of host cell protein (HCP) which is typically analyzed by immunoassay methods (e.g., HCP-ELISA). The capacity of the immunoassay to detect a broad range of HCPs, relevant for the individual mAb-production process should be proven by orthogonal proteomic methods such as 2D gel electrophoresis or mass spectrometry (MS). In particular MS has become a valuable tool to identify and quantify HCP in complex mixtures. We evaluate up- and DSP parameters of four different biopharmaceutical products, two different process variants, and one mock fermentation on the HCP pattern by shotgun MS analysis and ELISA. We obtained a similar HCP pattern in different cell culture fluid harvests compared to the starting material from the downstream process. During the downstream purification process of the mAbs, the HCP level and the number of HCP species significantly decreased, accompanied by an increase in diversity of the residual HCP pattern. Based on this knowledge, we suggest a control strategy that combines multi product ELISA for in-process control and release analytics, and MS testing for orthogonal HCP characterization, to attain knowledge on the HCP level, clusters and species. This combination supports a control strategy for HCPs addressing safety and efficacy of biopharmaceutical products.     

Impact of dynamic online fed-batch strategies on metabolism, productivity and N-glycosylation quality in CHO cell cultures

As we pursue the means to improve yields to meet growing therapy demands, it is important to examine the impact of process control on glycosylation patterns to ensure product efficacy and consistency. In this study, we describe a dynamic on-line fed-batch strategy based on low glutamine/glucose concentrations and its impact on cellular metabolism and, more importantly, the productivity and N-glycosylation quality of a model recombinant glycoprotein, interferon gamma (IFN-gamma). We found that low glutamine fed-batch strategy enabled up to 10-fold improvement in IFN-gamma yields, which can be attributed to reduced specific productivity of ammonia and lactate. Furthermore, the low glutamine concentration (0.3 mM) used in this fed-batch strategy could maintain both the N-glycosylation macro- and microheterogeneity of IFN-gamma. However, very low glutamine (<0.1 mM) or glucose (<0.70 mM) concentrations can lead to decreased sialylation and increased presence of minor glycan species consisting of hybrid and high-mannose types. This shows that glycan chain extension and sialylation can be affected by nutrient limitation. In addition to nutrient limitation, we also found that N-glycosylation quality can be detrimentally affected by low culture viability. IFN-gamma purified at low culture viability had both lower sialylation as well as glycans of lower molecular masses, which can be attributed to extensive degradation by intracellular glycosidases released by cytolysis. Therefore, in order to maintain good N-glycosylation quality, there is a need to consider both culture viability and nutrient control setpoint in a nutrient-limiting fed-batch culture strategy. A greater understanding of these major factors that affect N-glycosylation quality would surely facilitate future development of effective process controls.     

Perfusion seed cultures improve biopharmaceutical fed‐batch production capacity and product quality

Volumetric productivity and product quality are two key performance indicators for any biopharmaceutical cell culture process. In this work, we showed proof‐of‐concept for improving both through the use of alternating tangential flow perfusion seed cultures coupled with high‐seed fed‐batch production cultures. First, we optimized the perfusion N‐1 stage, the seed train bioreactor stage immediately prior to the production bioreactor stage, to minimize the consumption of perfusion media for one CHO cell line and then successfully applied the optimized perfusion process to a different CHO cell line. Exponential growth was observed throughout the N‐1 duration, reaching >40 × 10⁶ vc/mL at the end of the perfusion N‐1 stage. The cultures were subsequently split into high‐seed (10 × 10⁶ vc/mL) fed‐batch production cultures. This strategy significantly shortened the culture duration. The high‐seed fed‐batch production processes for cell lines A and B reached 5 g/L titer in 12 days, while their respective low‐seed processes reached the same titer in 17 days. The shortened production culture duration potentially generates a 30% increase in manufacturing capacity while yielding comparable product quality. When perfusion N‐1 and high‐seed fed‐batch production were applied to cell line C, higher levels of the active protein were obtained, compared to the low‐seed process. This, combined with correspondingly lower levels of the inactive species, can enhance the overall process yield for the active species. Using three different CHO cell lines, we showed that perfusion seed cultures can optimize capacity utilization and improve process efficiency by increasing volumetric productivity while maintaining or improving product quality. © 2014 American Institute of Chemical Engineers Biotechnol. Prog., 30:616–625, 2014     

Analyzing the dynamics of cell growth and protein production in mammalian cell fed-batch systems using logistic equations

The logistic modeling approach was used to describe experimental viable cell density (X) and product concentration (P) data from two industrial fed-batch mammalian cell culture processes with maximum product concentrations in the 3.0-9.4 g/l range. In both cases, experimental data were well described by the logistic equations and the resulting specific growth rate and protein productivity profiles provided useful insights into the process kinetics. Subsequently, sensitivity equations for both the X and P models were analyzed which helped characterize the influence of model parameters on X and P time courses. This was augmented by conventional sensitivity analyses where five values of each model parameter, 25% apart, were used to generate X and P time courses. Finally, results from sensitivity analysis were used to simulate X and P time courses that were reflective of typical early- and late-stage fed-batch cell culture processes. Different combinations of the logistic model parameters were used to arrive at the same final product concentration demonstrating the ability of the logistic approach to describe the multitude of process paths that result in the same final product concentration. Overall, the capability of the logistic equations to well describe X and P data from fed-batch cultures, coupled with their ability to simulate the multitude of paths leading up to the desired cell density and product concentration profiles, make them a useful tool during mammalian cell fed-batch process development.     

A computer-aided approach to compare the production economics of fed-batch and perfusion culture under uncertainty

Fed-batch and perfusion culture dominate mammalian cell culture production processes. In this paper, a decision-support tool was employed to evaluate the economic feasibility of both culture modes via a case study based upon the large-scale production of monoclonal antibodies. The trade-offs between the relative simplicity but higher start-up costs of fed-batch processes and the high productivity but higher chances of equipment failure of perfusion processes were analysed. Deterministic analysis showed that whilst there was an insignificant difference (3%) between the cost of goods per gram (COG/g) values, the perfusion option benefited from a 42% reduction in capital investment and a 12% higher projected net present value (NPV). When Monte Carlo simulations were used to account for uncertainties in titre and yield, as well as the risks of contamination and filter fouling, the frequency distributions for the output metrics revealed that neither process route offered the best of both NPV or product output. A product output criterion was formulated and the options that met the criterion were compared based on their reward/risk ratio. The perfusion option was no longer feasible as it failed to meet the product output criterion and the fed-batch option had a 100% higher reward/risk ratio. The tool indicated that in this particular case, the probabilities of contamination and fouling in the perfusion option need to be reduced from 10% to 3% for this option to have the higher reward/risk ratio. The case study highlighted the limitations of relying on deterministic analysis alone.