Validation of a CFD model for cell culture bioreactors at large scale and its application in scale-up.

Among all the operating parameters that control the cell culture environment inside bioreactors, appropriate mixing and aeration are crucial to ensure sufficient oxygen supply, homogeneous mixing, and CO2 stripping. A model-based manufacturing facility fit approach was applied to define agitation and bottom air flow rates during the process scale-up from laboratory to manufacturing, of which computational fluid dynamics (CFD) was the core modeling tool. The realizable k-ε turbulent dispersed Eulerian gas-liquid flow model was established and validated using experimental values for the volumetric oxygen transfer coefficient (kLa). Model validation defined the process operating parameter ranges for application of the model, identified mixing issues (e.g., impeller flooding, dissolved oxygen gradients, etc.) and the impact of antifoam on kLa. Using the CFD simulation results as inputs to the models for oxygen demand, gas entrance velocity, and CO2 stripping aided in the design of the agitation and bottom air flow rates needed to meet cellular oxygen demand, control CO2 levels, mitigate risks for cell damage due to shear, foaming, as well as fire hazards due to high O2 levels in the bioreactor gas outlet. The recommended operating conditions led to the completion of five manufacturing runs with a 100% success rate. This model-based approach achieved a seamless scale-up and reduced the required number of at-scale development batches, resulting in cost and time savings of a cell culture commercialization process.

A CFD model for predicting protein aggregation in low-pH virial inactivation for mAb production.

Significant amounts of soluble product aggregates were observed in the low-pH viral inactivation (VI) operation during an initial scale-up run for an immunoglobulin-G 4 (IgG4) monoclonal antibody (mAb IgG4-N1). Being earlier in development, a scale-down model did not exist, nor was it practical to use costly Protein A eluate (PAE) for testing the VI process at scale, thus, a computational fluid dynamics (CFD)-based high-molecular weight (HMW) prediction model was developed for troubleshooting and risk mitigation. It was previously reported that the IgG4-N1 molecules upon exposure to low pH tend to change into transient and partially unfolded monomers during VI acidification (i.e., VIA) and form aggregates after neutralization (i.e., VIN). Therefore, the CFD model reported here focuses on the VIA step. The model mimics the continuous addition of acid to PAE and tracks acid distribution during VIA. Based on the simulated low-pH zone (≤pH 3.3) profiles and PAE properties, the integrated low-pH zone (ILPZ) value was obtained to predict HMW level at the VI step. The simulations were performed to examine the operating parameters, such as agitation speed, acid addition rate, and protein concentration of PAE, of the pilot scale (50-200 L) runs. The conditions with predictions of no product aggregation risk were recommended to the real scale-up runs, resulted in 100% success rate of the consecutive 12 pilot-scale runs. This study demonstrated that the CFD-based HMW prediction model could be used as a tool to facilitate the scale up of the low-pH VI process directly from bench to pilot/production scale.

Protein aggregation and mitigation strategy in low pH viral inactivation for monoclonal antibody purification.

Significant amounts of soluble product aggregates were observed during low-pH viral inactivation (VI) scale-up for an IgG4 monoclonal antibody (mAb IgG4-N1), while small-scale experiments in the same condition showed negligible aggregation. Poor mixing and product exposure to low pH were identified as the root cause. To gain a mechanistic understanding of the problem, protein aggregation properties were studied by varying critical parameters including pH, hold time and protein concentration. Comprehensive biophysical characterization of product monomers and aggregates was performed using fluorescence-size-exclusion chromatography, differential scanning fluorimetry, fluorescence spectroscopy, and dynamic light scattering. Results showed IgG4-N1 partially unfolds at about pH 3.3 where the product molecules still exist largely as monomers owing to strong inter-molecular repulsions and favorable colloidal stability. In the subsequent neutralization step, however, the conformationally changed monomers are prone to aggregation due to weaker inter-molecular repulsions following the pH transition from 3.3 to 5.5. Surface charge calculations using homology modeling suggested that intra-molecular repulsions, especially between CH2 domains, may contribute to the IgG4-N1 unfolding at ≤ pH 3.3. Computational fluid dynamics (CFD) modeling was employed to simulate the conditions of pH titration to reduce the risk of aggregate formation. The low-pH zones during acid addition were characterized using CFD modeling and correlated to the condition causing severe product aggregation. The CFD tool integrated with the mAb solution properties was used to optimize the VI operating parameters for successful scale-up demonstration. Our research revealed the governing aggregation mechanism for IgG4-N1 under acidic conditions by linking its molecular properties and various process-related parameters to macroscopic aggregation phenomena. This study also provides useful insights into the cause and mitigation of low-pH-induced IgG4 aggregation in downstream VI operation.

A carbon dioxide stripping model for mammalian cell culture in manufacturing scale bioreactors.

Control of carbon dioxide within the optimum range is important in mammalian bioprocesses at the manufacturing scale in order to ensure robust cell growth, high protein yields, and consistent quality attributes. The majority of bioprocess development work is done in laboratory bioreactors, in which carbon dioxide levels are more easily controlled. Some challenges in carbon dioxide control can present themselves when cell culture processes are scaled up, because carbon dioxide accumulation is a common feature due to longer gas-residence time of mammalian cell culture in large scale bioreactors. A carbon dioxide stripping model can be used to better understand and optimize parameters that are critical to cell culture processes at the manufacturing scale. The prevailing carbon dioxide stripping models in literature depend on mass transfer coefficients and were applicable to cell culture processes with low cell density or at stationary/cell death phase. However, it was reported that gas bubbles are saturated with carbon dioxide before leaving the culture, which makes carbon dioxide stripping no longer depend on a mass transfer coefficient in the new generation cell culture processes characterized by longer exponential growth phase, higher peak viable cell densities, and higher specific production rate. Here, we present a new carbon dioxide stripping model for manufacturing scale bioreactors, which is independent of carbon dioxide mass transfer coefficient, but takes into account the gas-residence time and gas CO2 saturation time. The model was verified by CHO cell culture processes with different peak viable cell densities (7 to 12 × 106 cells mL-1 ) for two products in 5,000-L and 25,000-L bioreactors. The model was also applied to a next generation cell culture process to optimize cell culture conditions and reduce carbon dioxide levels at manufacturing scale. The model provides a useful tool to understand and better control cell culture carbon dioxide profiles for process development, scale up, and characterization. Biotechnol. Bioeng. 2017;114: 1184-1194. © 2016 Wiley Periodicals, Inc.

Combined metabolomics and proteomics reveals hypoxia as a cause of lower productivity on scale-up to a 5000-liter CHO bioprocess.

Large-scale bioprocessing is key to the successful manufacturing of a biopharmaceutical. However, cell viability and productivity are often lower in the scale-up from laboratory to production. In this study, we analyzed CHO cells, which showed lower percent viabilities and productivity in a 5-KL production scale bioreactor compared to a 20-L bench-top scale under seemingly identical process parameters. An increase in copper concentration in the media from 0.02 µM to 0.4 µM led to a doubling of percent viability in the production scale albeit still at a lower level than the bench-top scale. Combined metabolomics and proteomics revealed the increased copper reduced the presence of reactive oxygen species (ROS) in the 5-KL scale process. The reduction in oxidative stress was supported by the increased level of glutathione peroxidase in the lower copper level condition. The excess ROS was shown to be due to hypoxia (intermittent), as evidenced by the reduction in fibronectin with increased copper. The 20-L scale showed much less hypoxia and thus less excess ROS generation, resulting in little to no impact to productivity with the increased copper in the media. The study illustrates the power of 'Omics in aiding in the understanding of biological processes in biopharmaceutical production.

Hypoxia influences protein transport and epigenetic repression of CHO cell cultures in shake flasks.

Shake flasks and bench-top bioreactors are widely used for cell culture process development, however, culture performances significantly differ between them. In order to apply the results received from small-scale cultures to production scale, it is important to understand the mechanisms underlying the differences between various culture systems. This study analyzes the expression patterns of Chinese hamster ovary (CHO) cells producing IgG-fusion protein B0 cultured in shake flasks and 5-L bench-top bioreactors by CHO-specific DNA microarrays. The data show that hypoxia was present in shake flask cultures but not in controlled, bench-top bioreactors. Hypoxic conditions appeared to be associated with epigenetic repression resulting in decreased cell culture performance and protein productivity, which is also present during large-scale bioreactor operations due to oxygen gradients. High protein productivity was associated with increased cellular machinery for protein transport and secretion in conjunction with decreased epigenetic repression in bench-top bioreactor cultivation. Metal ions could improve cell growth and protein production under hypoxia and this condition could be mimicked in small-scale bioreactors to facilitate cell culture process scale-up.

WITHDRAWN: Aminoglycoside phosphotransferase II gene as primary selection marker for Pichia pastoris producing full-length monoclonal antibody.

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Reduction of N-terminal methionylation while increasing titer by lowering metabolic and protein production rates in E. coli auto-induced fed-batch fermentation.

A standard fed-batch fermentation process using 1 mM isopropyl-ß-D: -thiogalactopyranoside (IPTG) induction at 37 °C in complex batch and feed media had been developed for manufacturing of a therapeutic protein (TP) expressed in inclusion bodies (IBs) by E. coli BL21 (DE3) driven by T7 promoter. Six unauthentic TP N-terminal variants were identified, of which methionylated TP (Met-TP) ratio was predominant. We hypothesized that lowering metabolic and protein production rates would reduce the Met-TP ratio while improving TP titer. The standard process was surprisingly auto-induced without added IPTG due to galactose in the complex media. Without changing either the clone or the batch medium, a new process was developed using lower feed rates and auto-induction at 29 °C after glucose depletion while increasing induction duration. In comparison to the standard process, the new process reduced the unauthentic Met-TP ratio from 23.6 to 9.6 %, increased the TP titer by 85 %, and the specific production yield from 210 to 330 mg TP per gram of dry cell weight. Furthermore, the TP recovery yield in the purified IBs was improved by ~20 %. Adding together, ~105 % more TP recovered in the purified IBs from per liter of fermentation broth for the new process than the standard process. The basic principles of lowering metabolic and production rates should be applicable to other recombinant protein production in IBs by fed-batch fermentations.

Cell culture and gene transcription effects of copper sulfate on Chinese hamster ovary cells.

This study reports the effects of varying concentrations of copper sulfate on the metabolic and gene transcriptional profile of a recombinant Chinese hamster ovary (CHO) cell line producing an immunoglobulin G (IgG)-fusion protein (B0). Addition of 50 µM copper sulfate significantly decreased lactate accumulation in the cultures while increasing viable cell density and protein titer. These changes could be seen from day 6 and became increasingly evident with culture duration. Reducing the copper sulfate concentration to 5 µM retained all the above beneficial effects, but with the added benefit of reduced levels of the aggregated form of the B0 protein. To profile the cellular changes due to copper sulfate addition at the transcriptional level, Affymetrix® CHO microarrays were used to identify differentially expressed genes related to reduced cellular stresses and facilitated cell cycling. Based on the microarray results, down-regulation of the transferrin receptor and lactate dehydrogenase, and up-regulation of a cytochrome P450 family-2 polypeptide were then confirmed by Western blotting. These results showed that copper played a critical role in cell metabolism and productivity on recombinant CHO cells and highlighted the usefulness of microarray data for better understanding biological responses on medium modification.

Modeling kinetics of a large-scale fed-batch CHO cell culture by Markov chain Monte Carlo method.

Markov chain Monte Carlo (MCMC) method was applied to model kinetics of a fed-batch Chinese hamster ovary cell culture process in 5,000-L bioreactors. The kinetic model consists of six differential equations, which describe dynamics of viable cell density and concentrations of glucose, glutamine, ammonia, lactate, and the antibody fusion protein B1 (B1). The kinetic model has 18 parameters, six of which were calculated from the cell culture data, whereas the other 12 were estimated from a training data set that comprised of seven cell culture runs using a MCMC method. The model was confirmed in two validation data sets that represented a perturbation of the cell culture condition. The agreement between the predicted and measured values of both validation data sets may indicate high reliability of the model estimates. The kinetic model uniquely incorporated the ammonia removal and the exponential function of B1 protein concentration. The model indicated that ammonia and lactate play critical roles in cell growth and that low concentrations of glucose (0.17 mM) and glutamine (0.09 mM) in the cell culture medium may help reduce ammonia and lactate production. The model demonstrated that 83% of the glucose consumed was used for cell maintenance during the late phase of the cell cultures, whereas the maintenance coefficient for glutamine was negligible. Finally, the kinetic model suggests that it is critical for B1 production to sustain a high number of viable cells. The MCMC methodology may be a useful tool for modeling kinetics of a fed-batch mammalian cell culture process.

Effects of culture conditions on N-glycolylneuraminic acid (Neu5Gc) content of a recombinant fusion protein produced in CHO cells.

CHO cells express glycoproteins containing both the N-acetylneuraminic acid (Neu5Ac) and minor amounts of the N-glycolylneuraminic acid (Neu5Gc) forms of sialic acid. As Neu5Gc is not expressed in humans and can be recognized as a foreign epitope, there is the potential for immunogenicity issues for glycoprotein therapeutics. During process development of a glycosylated fusion protein expressed by CHO cells, a number of culture conditions were identified that affected the Neu5Gc content of the recombinant glycoprotein. Sodium butyrate (SB), a well-known additive reported to enhance recombinant protein productivity in specific cases, minimally affected product titers here, but did decrease Neu5Gc levels by 50-62%. A shift in culture temperature to a lower value after the exponential growth phase was used to extend the culture period. It was found that the Neu5Gc levels were 59% lower when the temperature shift occurred later near the stationary phase of the culture compared to an early-temperature shift, near the end of the exponential growth phase. Studies on the effects of pCO(2) with this product showed that the Neu5Gc levels were 46% lower at high pCO(2) conditions (140 mmHg) compared to moderate pCO(2) levels (20-80 mmHg). Finally, a comparison of sodium carbonate versus sodium hydroxide as the base used for pH control resulted in a reproducible 33% decrease in Neu5Gc in bioreactors using sodium hydroxide. These results are of practical importance as SB is a commonly tested additive, and the other factors affecting Neu5Gc can conveniently be used to reduce or control Neu5Gc in processes for the manufacture of glycoprotein therapeutics.

Feed development for fed-batch CHO production process by semisteady state analysis.

Semisteady state cultures are useful for studying cell physiology and facilitating media development. Two semisteady states with a viable cell density of 5.5 million cells/mL were obtained in CHO cell cultures and compared with a fed-batch mode control. In the first semisteady state, the culture was maintained at 5 mM glucose and 0.5 mM glutamine. The second condition had threefold higher concentrations of both nutrients, which led to a 10% increase in lactate production, a 78% increase in ammonia production, and a 30% reduction in cell growth rate. The differences between the two semisteady states indicate that maintaining relatively low levels of glucose and glutamine can reduce the production of lactate and ammonia. Specific amino acid production and consumption indicated further metabolic differences between the two semisteady states and fed-batch mode. The results from this experiment shed light in the feeding strategy for a fed-batch process and feed medium enhancement. The fed-batch process utilizes a feeding strategy whereby the feed added was based on glucose levels in the bioreactor. To evaluate if a fixed feed strategy would improve robustness and process consistency, two alternative feeding strategies were implemented. A constant volume feed of 30% or 40% of the initial culture volume fed over the course of cell culture was evaluated. The results indicate that a constant volumetric-based feed can be more beneficial than a glucose-based feeding strategy. This study demonstrated the applicability of analyzing CHO cultures in semisteady state for feed enhancement and continuous process improvement.

Scale-up analysis for a CHO cell culture process in large-scale bioreactors.

Bioprocess scale-up is a fundamental component of process development in the biotechnology industry. When scaling up a mammalian cell culture process, it is important to consider factors such as mixing time, oxygen transfer, and carbon dioxide removal. In this study, cell-free mixing studies were performed in production scale 5,000-L bioreactors to evaluate scale-up issues. Using the current bioreactor configuration, the 5,000-L bioreactor had a lower oxygen transfer coefficient, longer mixing time, and lower carbon dioxide removal rate than that was observed in bench scale 5- and 20-L bioreactors. The oxygen transfer threshold analysis indicates that the current 5,000-L configuration can only support a maximum viable cell density of 7 x 10(6) cells mL(-1). Moreover, experiments using a dual probe technique demonstrated that pH and dissolved oxygen gradients may exist in 5,000-L bioreactors using the current configuration. Empirical equations were developed to predict mixing time, oxygen transfer coefficient, and carbon dioxide removal rate under different mixing-related engineering parameters in the 5,000-L bioreactors. These equations indicate that increasing bottom air sparging rate is more efficient than increasing power input in improving oxygen transfer and carbon dioxide removal. Furthermore, as the liquid volume increases in a production bioreactor operated in fed-batch mode, bulk mixing becomes a challenge. The mixing studies suggest that the engineering parameters related to bulk mixing and carbon dioxide removal in the 5,000-L bioreactors may need optimizing to mitigate the risk of different performance upon process scale-up.

Identifying inhibitory threshold values of repressing metabolites in CHO cell culture using multivariate analysis methods.

Elevation of lactate, ammonia, osmolality, and carbon dioxide to inhibitory levels was reported to have adverse effects on cell growth and protein productivity in mammalian cell culture. Multivariate analysis methods were used to investigate the roles of these repressing metabolites in a fed-batch CHO cell culture for antibody fusion protein B1 (B1) production. Principal Factor Analysis methodology was applied to manufacturing-scale data of 112 cell culture runs, which identified threshold values of four repressing metabolites as follows: (1) ammonium levels above 5.1 mM inhibit cell growth; (2) both lactate and osmolality levels above 58 mM and 382 mOsm/kg affect cell viability; and (3) carbon dioxide levels at or above 111 mmHg reduce protein quality. These threshold values were then verified by simulations using Monod-type equations and Canonical Correlation. These results suggest that adverse effects on cell growth, productivity, and product quality may be minimized under the ideal cell culture condition, in which the peak values of all four repressing metabolites are maintained below the threshold values. This strategy was evaluated in 45 cell culture runs in 50-L bioreactors. Eight out of 45 runs were operated under the ideal condition, while the remaining 37 runs had at least one repressing metabolite with peak value at or above the threshold. In comparison to the remaining runs, the eight cell culture runs under the ideal condition had 17%, 40%, and 11% higher values in peak viable cell density, final B1 titer, and quality attribute, respectively. The unique methodology used in this study may be generally applicable in characterizing cell culture processes.

Purification, cloning, and functional expression of phenylalanine aminomutase: the first committed step in Taxol side-chain biosynthesis.

The conversion of alpha-phenylalanine to beta-phenylalanine is the first committed step in the biosynthesis of the C-13 side chain of Taxol. Thus, the novel enzyme responsible for this step, phenylalanine aminomutase (PAM), is of considerable interest for studies of Taxol biosynthesis and represents a potential target for genetic engineering. A method is described for purifying PAM from Taxus chinensis cell cultures. The purified enzyme has a K(m) of 1.1mM, a V(max) of 110.1 microm/min/mg protein, a pH optimum of 7.5-8.0, and a denatured molecular weight of about 80 kDa. Peptide sequences derived from the purified protein were used to design and synthesize degenerate primers enabling the PCR synthesis of the PAM cDNA. The PAM cDNA encodes a protein of 687 amino acid residues with a deduced molecular weight of 75.3 kDa. The PAM cDNA was cloned and expressed in Escherichia coli, and PAM activity was demonstrated. As a gene symbol for the PAM enzyme, pam is proposed. Protein sequence alignments of PAM, phenylalanine ammonia-lyase (PAL), and histidine ammonia-lyase (HAL) sequences exhibit significant similarity providing insight into potential active site residues of PAM.