Efficient and stable production of Modified Vaccinia Ankara virus in two-stage semi-continuous and in continuous stirred tank cultivation systems

One important aim in cell culture-based viral vaccine and vector production is the implementation of continuous processes. Such a development has the potential to reduce costs of vaccine manufacturing as volumetric productivity is increased and the manufacturing footprint is reduced. In this work, continuous production of Modified Vaccinia Ankara (MVA) virus was investigated. First, a semi-continuous two-stage cultivation system consisting of two shaker flasks in series was established as a small-scale approach. Cultures of the avian AGE1.CR.pIX cell line were expanded in the first shaker, and MVA virus was propagated and harvested in the second shaker over a period of 8–15 days. A total of nine small-scale cultivations were performed to investigate the impact of process parameters on virus yields. Harvest volumes of 0.7–1 L with maximum TCID50 titers of up to 1.0×109 virions/mL were obtained. Genetic analysis of control experiments using a recombinant MVA virus containing green-fluorescent-protein suggested that the virus was stable over at least 16 d of cultivation. In addition, a decrease or fluctuation of infectious units that may indicate an excessive accumulation of defective interfering particles was not observed. The process was automated in a two-stage continuous system comprising two connected 1 L stirred tank bioreactors. Stable MVA virus titers, and a total production volume of 7.1 L with an average TCID50 titer of 9×107 virions/mL was achieved. Because titers were at the lower range of the shake flask cultivations potential for further process optimization at large scale will be discussed. Overall, MVA virus was efficiently produced in continuous and semi-continuous cultivations making two-stage stirred tank bioreactor systems a promising platform for industrial production of MVA-derived recombinant vaccines and viral vectors.

Introduction Similar to the manufacturing of antibodies, growth factors or hormones, the production of viral vaccines and vectors for gene therapy in batch cultivation is still the standard technology. Moving from batch to continuous operation can significantly increase productivity, improve the quality of products, and reduce the footprint of equipment and facilities required for production [1]. The upstream phase of continuous processes is faster and more efficient compared to batch processes because smaller bioreactors are required, volumetric yields are higher and plant down-time is reduced [2]. Hence, continuous virus production may also help to increase significantly the manufacturing capacity and to meet the global demand for low cost viral vaccines of an ever-growing world population.
One potential platform for continuous production of viruses is a two-stage stirred tank bioreactor (TSB) system. A TSB system consists of one vessel for continuous propagation of cells connected in series with a second vessel, where the desired product is obtained [3,4]. The physical separation of the cell growth vessel from the production bioreactor allows stable operation of processes involving lytic viruses. TSB systems have been used for the production of poliovirus and adenovirus [4], for production of recombinant proteins using baculovirus [5], and for continuous production of influenza A/PR/8/34 virus [6]. In the latter, virus production was maintained over a time period of 18 d but process yields were lower than for batch cultivations due to oscillations of virus titers. These oscillations were generated by the accumulation of defective interfering particles (DIPs) that spontaneously arise due to error-prone viral replication of RNA viruses with high mutation rates. DIPs are replication-deficient and require coinfections with wildtype or helper viruses for successful propagation. At very high multiplicity of infection (moi), the replication capacity of the helper viruses is limited by DIPs which is known as "passage effect" or "Von Magnus effect" [5][6][7][8].
One virus that has a great potential for expression of recombinant antigens or as a viral vaccine vector is Modified Vaccinia Ankara (MVA) virus, a DNA virus that can accommodate large recombinant inserts and is described to be safe for humans and animals [9]. Recombinant vector vaccines based on MVA against influenza virus [10], Ebola virus [11,12], HIV [13], tuberculosis [14], chykungunya virus [15], smallpox [16], respiratory syncytial virus [17], malaria [18,19], bluetongue virus [20], West Nile virus [21], and also veterinary vaccines against the tick-born parasite Babesia bovis [22], have been described. One challenge in MVA production is the property that a large fraction of infectious units remain cell-associated. Because cultivation in a single-cell format interferes with the spread of MVA, processes have been developed where the virus is propagated in suspended aggregates of 20-100 cells [23]. Recently, a novel MVA virus isolate, named MVA-CR19, has been generated that can be produced at high yields in non-aggregated avian suspension cells in chemically defined media [24], which makes MVA an interesting candidate for exploring process options towards continuous vaccine manufacturing.
When a fraction of a culture is replaced with fresh media at regular time intervals, the mode of operation is defined as "semi-continuous". Compared to fully continuous operation in bioreactors, a scale-down of semi-continuous cultures can be easily achieved for studying the impact of process parameters on cell growth and virus propagation. In addition, semi-continuous cultures can be set to medium exchange regimes that can approach continuous cultivations [25]. To name one recent example, semi-continuous cultivations using shake flasks have been used for propagation of the rat hybridoma cell line TFL-P9 [26]  operation have been used for two-stage production of baculovirus-based recombinant proteins resulting in high yields [27].
Here, we describe results for the establishment of semi-continuous and continuous processes for production of MVA virus (MVA-CR19, and a recombinant MVA virus that expresses green-fluorescent-protein (GFP), MVA-CR19.GFP) in the avian suspension cell line AGE1.CR.pIX in a chemically defined medium (all from ProBioGen AG, Germany) [28][29][30].
First, a small-scale two-stage semi-continuous cultivation (SSC) system using shaker flasks was established for cell growth and virus propagation at exchange rates that approximated the dilution rates of continuous TSB systems. The impact of process parameters such as the residence time (RT) and the addition of fresh medium on virus yields were analyzed. Furthermore, by using MVA-CR19.GFP, recombinant protein expression and viral stability at the genetic level was evaluated over a time period of 15 d of cultivation. Finally, cell growth, glucose and lactate concentrations, pH values and virus yields were monitored in a TSB system (two 1 L stirred tank bioreactors), and compared to SSC cultivations. The observed genetic stability and high infectious titers demonstrate the feasibility for highly efficient continuous production of MVA viruses.

Cell line and Modified Vaccinia Ankara virus genotypes
The avian cell line AGE1.CR.pIX (ProBioGen AG, Germany) was grown in a chemically defined medium CD-U3 (powder-based, PAA, Austria; liquid, Biochrom-Merck, Germany) supplemented with 2 mM of L-glutamine (Sigma-Aldrich, Germany), 2 mM L-alanine (Fluka Analytical, Sigma-Aldrich, Germany) and 10 ng/mL Long 1 R 3 IGF-I (SAFC Biosciences, USA). Cells were inoculated at a concentration of 0.8×10 6 cells/mL and passaged in shaker flasks (125 mL Erlenmeyer culture flasks, 2 μm vent cap with baffles; Corning, USA) at 37˚C, 5% CO 2 in air, and 185 rpm [31]. Previous studies have shown that this cell line has stable growth characteristics and can be used for MVA virus production [29,31]. The MVA virus isolates MVA-CR19 (virus seed: 4.5×10 8 virions/mL, TCID 50 ) and MVA-CR19.GFP (virus seed: 1.0×10 9 virions/mL, FFU; 1×FFU = 0.7×TCID 50 ) with a green-fluorescent-protein insertion cassette were used (both isolates from ProBioGen AG, Germany). Before infection, the virus seed was sonicated in a water bath at room temperature for 1 min. An moi of 0.05 (ratio of the number of infectious virions to the number of cells) was used in all cultivations.
A SSC system using two shaker flasks (250 mL and 125 mL Erlenmeyer Culture Flasks with a 2 μm vent cap and without baffles; Corning, USA) in series was established as a scale-down model for design and parameter studies regarding TSB optimization. All related abbreviations, volumes and the operation mode of the system are described in Fig 1. The shakers were maintained in an orbital shaking incubator (Infors HT Multitron, Switzerland) at 37˚C, 185 rpm and 5% CO 2 in air. Cells were grown in batch mode for up to 96 h and infection was carried out at an moi of 0.05. Samples of 3-5 mL for measuring cell concentration, viability, pH, metabolite concentrations, and virus concentration in the small cell bioreactor (SCB) and the small virus bioreactor (SVB) were taken twice a day for process monitoring. Small volume losses after sampling were corrected by adding fresh medium. After sampling, medium exchanges and addition of fresh medium were carried out. The volumes exchanged were determined with the following equations: Where n is the sample number, V is volume, t n is the time at sampling "n", t n-1 the time at sampling "n-1", D SCB is the dilution rate of SCB, and FM is fresh medium. The dilution rate of SCB (D SCB ) was the same in all SSC experiments. The equations were obtained by performing a material balance, where the dilution rate of the TSB system F 4 /(V CB + V VB ) is equal to the dilution rate of CB (see Fig 1B). Based on previous experiments [31], a maximum specific cell growth rate of 0.02 h -1 for AGE1.CR.pIX was used to determine the parameters for all SSC cultivations. Due to the significant amount of samples taken and time required for one SSC run (2 weeks, approximately 36 samples) compared to batch cultivations (7 d, approximately 12 samples) only one cultivation was carried out per SSC experiment (unless the opposite is indicated).

Evaluation of the influence of process variables on virus yields and virus stability
To evaluate the influence of RT on MVA-CR19 virus yields, the volume of SVB was modified to obtain a RT of 25, 35, and 64 h in the SVB (keeping all other variables constant). Also, the effect of omitting the addition of fresh medium to the VB (F 3 , Fig 1B) was evaluated for one SSC cultivation by reducing V 3 to zero ( Fig 1A). The stability of MVA-CR19 virus was done using the MVA-CR19.GFP recombinant strain under two criteria. The first criterion was that, if the recombinant virus is stable, then the ratio of the total infectious virus population (IVP) to the protein-expressing infectious virus population (PEIVP) should be constant during cultivation time. The PEIVP was measured by determining a GFP-derived TCID 50 by fluorescence microscopy (described in section 2.4.2). This ratio was determined with the following equation: With IVP and PEIVP the mean of a technical triplicate. The second criterion used was a genetic analysis of the GFP insertion cassette using a polymerase chain reaction (PCR) protocol (described in detail in section 2.4.2). The samples analyzed with both criteria were taken from the first and last harvest of two SSC cultivations operated over 16 d, one with 25 h RT in the SVB and a second with 40 h RT in the SVB.
Continuous production of MVA virus in a two-stage stirred tank bioreactor system A bioreactor system consisting of two 1 L stirred tank bioreactors (Biostat B Plus, Sartorius) was established (similar to Frensing et al. 2013, Fig 1B). The first bioreactor (Cell Bioreactor, CB) was inoculated with AGE1.CR.pIX cells at 1×10 6 cells/mL and operated at 37˚C, 120 rpm with Rushton impellers, 40% oxygen saturation and 850 mL working volume (wv). Oxygen saturation was controlled using pulsed aeration with pure oxygen. The pH value was not controlled and only monitored during the batch phase to avoid values below 6.9. When the cell concentration in the CB reached at least 5.0×10 6 cells/mL, 350 mL from the CB were transferred to the second vessel VB. Working volumes were corrected to 850 mL in CB and 440 mL in VB by adding fresh CD-U3 medium and continuous culture was initiated 2 h later and maintained without infection for 8 d. The dilution rate of CB (D CB ) was as reported previously [6], and the dilution rate of VB (D VB ) was 0.04 h -1 (25 h RT). Temperature of VB was 37˚C, oxygen concentration was at 40-50% saturation, and the 440 mL wv was maintained with a dip tube. Before infection, a 1:1 dilution of VB was carried out, and the cultivation continued at 440 mL wv. MVA-CR19 virus was added to VB at an moi of 0.05. The peristaltic pumps used were Ismatec Reglo-Digital MS2/8-160 (Pump 1 and 2, Fig 1B; Cole-Parmer GmbH, Germany), and Watson Marlow 101U/R (Pump 3, Fig 1B; Waston-Marlow Fluid Technology Group, UK). Samples of 5-6 mL were taken twice a day from both vessels for measuring cell concentration, viability, off-line pH, metabolite concentrations, and virus concentration.

Analytics
Cell concentration, viability, and metabolite concentrations. A ViCell TM XR cell viability analyzer (Beckman Coulter GmbH, Germany) was used for determining AGE1.CR.pIX cell concentration and viability, with a standard deviation of 5% [28]. Glucose and lactate were determined to avoid media limitations using a BioProfile 100 Plus (Nova) analyzer; the relative standard deviation of the method is 1.9% for glucose and 10.5% for lactate, respectively.
Virus quantification assay, and polymerase chain reaction (PCR) protocol used for MVA-CR19.GFP virus stability analysis. The concentration of infectious virus particles was quantified by a TCID 50 assay as described previously [29]. In addition, the GFP-derived TCID 50 titer was obtained by measuring cell fluorescence using a fluorescence microscope (λ 495 nm, Axio Observer A1, Zeiss, Germany). The GFP-assay was carried out immediately before performing the regular TCID 50 staining procedure. The PCR was carried out by mixing the infected cell suspension (80 μL) with 20 μL of QuickExtract DNA Extraction Solution 1.0 (Epicentre, USA) and heated to 65˚C for 10 min and to 98˚C for 5 min. Of this preparation, 4 μL were used in a PCR reaction in a final volume of 20 μL with 0.15 μL Taq polymerase (Qiagen, Germany), 200 nM of each primer, and 125 μM of each nucleotide. The sequence of the primer pairs that span deletion sites II, III and IV of the viral genome have been published previously [30]. The expected sizes of the amplification products are 354, 447, and 502 bp for wildtype virus deletion sites II to IV, and 1285 for deletion site III in MVA-CR19.GFP. Thermocycling was initiated with 94˚C for 80 s, followed by 35 cycles of 94˚C for 20 s, 55˚C for 20 s and 72˚C for 90 s, and terminated with 72˚C for 5 min. Amplicons were separated by electrophoreses in 1.5% agarose gels.

Productivity indicators of the cultivation systems
The productivity of batch, semi-continuous and continuous cultivation systems was determined based on two parameters: time yield (TY) and space-time yield (STY). The following equations were used for all three cultivation modes: Where t n is the total operational time (initial batch phase plus virus production phase for semi-continuous and continuous), TCID 50H;t n is the TCID 50 of a harvest at time t n (if no harvest is taken at time t n its value is zero), and V H;t n is the harvest volume collected at time t n . Eqs 6 and 7 were also used for estimating the productivity of a hypothetical batch process consisting of two parallel 645 mL bioreactors (8 d batch cycle). Considering possible mass transfer limitations for larger scales, the (maximum) productivity of a hypothetical batch cultivation was estimated using virus titers obtained in small-scale cultivations, i.e. the titers of BM-A, BM-B, and BM-C shown in Table 1. This hypothetical system was chosen as a comparison to the TSB system, because it represents the alternative given up when the decision of operating both vessels in continuous mode is taken (opportunity cost). From here onward this hypothetical process is referred as the batch process.  (Table 1).

Results and discussion
MVA-CR19 virus titers obtained in these 50 mL batch experiments were similar to those previously described for MVA wild type virus replicated in AGE1.CR and AGE1.CR.pIX cells [31]. In particular, these experiments confirmed that the new genotype MVA-CR19 efficiently replicates in single cells and does not require cell agglomeration at the time of infection [24]. Taking into account the initial batch phase of the continuous experiment T25 (Fig 2A), where cell concentrations up to 5×10 6 cells/mL were achieved in a 1 L bioreactor in batch mode, it should also be possible to obtain high virus titers at larger batch volumes.

Semi-continuous cultivation
Cells and MVA virus propagation in the semi-continuous system. To start the cultivation, AGE1.CR.pIX cells were seeded at a concentration of 0.8×10 6 cells/mL in SCB and SVB and maintained in batch mode for 3-4 d. Results of one representative cultivation are shown in Fig 2A, 2B, 2C and 2D (experiment SM25-A, Table 1). After the initial batch phase, medium replacements at regular intervals were initiated (12-15 h) and a semi-continuous steady-state was successfully obtained for at least 2 weeks. Viable cell concentrations in the SCB fluctuated in a range of 8-12×10 6 cells/mL with viabilities above 90% (Fig 2B). No limitation of glucose was observed, and levels of lactate were about 20 mmol/L, as shown in Fig 2C. SVB was infected with MVA virus after 3-4 d of batch growth, and the semi-continuous mode with harvesting was started 12 h p.i. The cell concentration initially also fluctuated in a similar range as for the SCB, but then fluctuations decreased as a consequence of progressing virus replication. Cell viabilities of 90% or more were observed in SVB for the first days, but dropped after 12 d (Fig 2B). The virus titers increased for about 4-5 d before a stationary phase was achieved (Fig 2D). Final TCID 50 values between 1×10 7 −1×10 9 virions/mL, were obtained that are similar to those of batch cultivations and published data [24,31]. In contrast  1.0×10 5 virions/mL. The TCID 50 titers showed the typical pattern of virus replication, an initial increase followed by a stationary phase. Depending on the RT in the SVB, the increase in virus titers differed significantly. With the lowest RT (SM25-B, 25 h), the increase was fast and high titers were achieved within 2 d (!1×10 8 virions/mL, Fig 3). Surprisingly, virus increase was delayed with higher RT (SM35-B and SM64, 35 and 64 h). Nevertheless, for both cultivations final virus titers in the order of 1×10 8 virions/mL were obtained.
Also, to test whether high virus yields can be obtained by reducing the amount of fresh medium added to SVB, one experiment was performed without the addition of fresh medium into the virus vessel (SM35-C; Table 1, Fig 3). With fluctuations in TCID 50 titers not exceeding 1×10 5 virions/mL, this cultivation resulted in the lowest virus titers among all experiments. This is in agreement with previous studies (performed with influenza A virus, however) which showed that addition of fresh medium at time of infection is usually required for obtaining high virus yields in batch processes [32]. Despite the differences during the initial increase in virus titers (8-10 d), all SSC cultivations achieved comparable maximum TCID 50 titers in the stationary phase with fluctuations of less than 2 log units. Taking additionally into account the results of the SSC cultivations, a RT of 25 h was therefore used to scale up the virus bioreactor in the continuous cultivation.
Productivity of the semi-continuous experiments. As a general tendency, a higher productivity was obtained for experiments with lower RT in SVB. The TY was 1.0×10 9 , 4.1×10 8 , and 2.0×10 8 virions/h for the experiments SM25-B, SM-35-B and SM64, respectively ( Table 1). The best STY was 1.0×10 9 , 3.6×10 8 , and 1.  Continuous production of MVA virus batch processes. It has to be taken into account, however, that a batch process is more efficient than SSC for low volume MVA vaccine production (single batch campaigns).

Analysis of MVA-CR19.GFP virus stability in semi-continuous cultivations at 25 h and 40 h of residence time.
In order to investigate the genetic stability of the MVA virus over extended cultivation periods (i.e. the risk to lose the recombinant GFP protein), the MVA-CR19.GFP virus was propagated for 16 d in SSC, and the TCID 50 as well as the GFP-derived TCID 50 were determined (25 h RT, Fig 4A; 40 h RT, Fig 4D). For both RT experiments, the time course and the absolute values of both TCID 50 titers were similar over the whole cultivation period. At 25 h RT, a Ratio-TCID50 of 1.4 and 2.0 was obtained for the first and the last harvest, respectively (Fig 4B and 4C). At 40 h RT, the ratios were 1.6 and 1.0, respectively (Fig 4E  and 4F). Considering that the error range of the TCID 50 assay is a least 0.3 log units due to the dilution steps chosen for titrations, this variation is not significant. The Ratio-TCID50 of 1.0 and 2.0 after 16 d of culture in both RT experiments suggests that the MVA virus is genetically stable. Interestingly, the MVA-CR19.GFP virus titers were higher for a RT of 40 h rather than 25 h. One potential explanation may be that the incorporation of a recombinant insert may have slightly prolonged the virus replication cycle so that 25 h RT may be too short for efficient propagation in the SVB.
In addition, the genetic stability of MVA-CR19.GFP virus was analyzed using PCR of the first and last harvest of both SSC cultivations. For the two RT experiments, the GFP insertion cassette amplified by this method was visible in the deletion segment 3 (Del 3) of the first (0 d p.i.) and last harvest (16 d p.i.) with a size of 1428 kbp (Fig 4G). The fact that this band was visible in the first and last harvests, and that no smaller gene fragments where detected in this cultivation, supports the finding regarding the genetic stability of MVA-CR19.GFP discussed above. For longer cultivations and for the production of other recombinant antigens, these results have to be confirmed. In general, however, MVA-CR19 seems to be an excellent candidate for continuous viral vector production.

Continuous cultivations
Cell and MVA virus propagation in the continuous bioreactor. The continuous bioreactor system (experiment T25, Table 1) was successfully operated for 30 d, as shown in Fig 5. During the startup of the process (-12 d to -8 d), the cell concentration in the CB reached values of 5.0×10 6 cells/mL in batch operation with cell viabilities well above 90% (Fig 5A and 5B), and μ max of 0.0150 h -1 . Both, the maximum cell concentrations and the μ max are in accordance with results reported previously by Lohr et al (2009). Immediately before the continuous culture was initiated, a concentration of about 2.5×10 6 cells/mL was reached in both vessels by 1:1 dilution with fresh medium. Once the continuous operation was started, the cell concentration in the CB increased initially to 5.0×10 6 cells/mL, and finally decreased to 3.0×10 6 cells/mL with 85% viability. Nevertheless, cells could be maintained stable at these viabilities for the rest of the experiment. Also, the continuous process was maintained without infection of VB for the next 8 d (-7 d to 0 d p.i., Fig 5A), in order to evaluate cell growth in the second vessel. Finally, the cells concentration in the VB reached up to 9.0×10 6 cells/mL, well above the anticipated 5.0×10 6 cells/mL of CB. One possible explanation is that the dip tube of the VB, used to extract the harvest, might have acted as a settler as it had a relatively low withdrawal rate and a high internal diameter as reported previously [33]. Achieving high cell concentrations, the glucose concentration in the VB dropped to about 10 mmol/L (Fig 5C). Therefore the 50% of medium of the VB was exchanged before infection with MVA-CR19 virus. After the infection (moi 0.05), the cell concentration and the viability in VB decreased to 5.0×10 6 cells/mL and 70%, respectively, as expected from the SSC experiments described above. After three days of continuous cultivation, the TCID 50 reached values close to 1.0×10 8 virions/mL, and a stable MVA production was maintained for 18 d p.i. with a maximum titer of 6.0×10 8 virions/mL, very similar to batch cultivations [31]. A total number of 6.0×10 11 virions were collected from the harvest, with a total production volume of 7.1 L, which corresponds to an average TCID 50 of 9×10 7 virions/mL (also see data for T25 in Table 1). As before, the virus titers fluctuated in a range not larger than 1 log unit (see SSC experiments). This low level of fluctuations of infectious titers over process time together with the observed genomic stability of MVA-CR19.GFP suggests that interference by defective particles [34,35] is not a phenomenon that limits continuous MVA replication.
In Fig 5D, the time course of the TCID 50 of the VB and the harvest bottle are depicted. Note that, while the TCID 50 of VB represents the virus concentration in the vessel at a given time point, the TICD 50 of the harvest represents the value that results from accumulating virus production over a period of 8-12 h. During this time period, part of the MVA virus could be inactivated by host cell hydrolases released to the supernatant. Thus, the slightly lower TCID 50 titers obtained in the harvest compared to the VB might be closer to the real TCID 50 that will be obtained in a continuous process with a harvest bottle connected to the VB.
Interestingly, the TSB results resembles some of the results obtained with the semi-continuous cultivation system. Experiments SM25-A and SM25-B were performed with a RT in SVB identical to the VB of the TSB system. Virus titers from SM25-A ( Fig 2D) showed a similar  Fig 3), was even closer to the virus dynamics obtained with the TSB system because the harvest volume was correctly calculated using Eq 4 (a wrong calculation of the first harvest volume of SM25-A diluted the virus below 1×10 5 virus/mL between 0-4 d p.i.). This confirms that SSC could serve as a scale-down model of the TSB system, and is in line with previous work performed by Van [27]. In addition, it confirms studies regarding the use of simple non-instrumented batch and semi-continuous cultures for the design and optimization of continuous animal cell cultures [26]. Overall, our results show that these concepts can even be applied for two-stage virus cultivations systems using shaker flasks.
Productivity of the continuous process. The TY of the TSB system was 1.2×10 9 virions/ h, and the STY was 1.7×10 8 virions/(L h) for a total of 21.7 d of operation (17.7 d of virus propagation). The time course of TY and STY over the production time is shown in Fig 6A and 6B. As a comparison, data of an hypothetical batch process (10 7 virions/mL and 10 8 virions/mL at toh) are also included. This figure shows that both the TY and the STY of the TSB started below the productivity of a batch. After 7 days, the productivity of the TSB approached the batch process and remained constant. In other words, the TSB system can be equally or more efficient than a batch production system, if more than two batch-cycles are performed (see detail in Table 1).

Conclusions
Continuous and semi-continuous production of MVA virus was evaluated and compared against batch cultivations using MVA-CR19 and MVA-CR19.GFP virus isolates that allow efficient replication in non-agglomerated avian AGE1.CR.pIX suspension cells. A small-scale approach, using a two-stage semi-continuous cultivation (SSC) system, was used to support the establishment of a two-stage continuous stirred tank bioreactor (TSB) system that showed stable production of cells over 2-3 weeks of cultivation.
A higher residence time in the SSC system resulted in a higher delay before virus titers increased, but had little impact on the final titers of the MVA-CR19 isolate in the stationary phase. A critical parameter for high yields appears to be the incorporation of a stream of fresh medium in the virus bioreactor, to remove spent medium including compounds inhibiting virus replication and to avoid limitation of cell-relevant metabolites during virus replication.
Evaluation of continuous production of MVA was facilitated with the SSC system because high virus titers were obtained throughout the process interval without oscillations of infectious units at different residence times. The stable titers suggest that a "von Magnus effect" due to formation of DIPs is highly unlikely for MVA. This observation is also consistent with the results from assays for maintenance of recombinant inserts by titration against the fluorescence GFP transgene and by PCR analysis. These assays demonstrated that MVA is stable for at least 16 d of continuous production.
A scale up to a TSB system for MVA-CR19 virus propagation was successful and showed high TCID 50 titers, again with only small random fluctuations over 18 d of virus production and with productivity indicators comparable to repeated-batch cultivations. However, titers appeared to be lower for the recombinant virus that expresses GFP if the RT was only 25 h. This observation may indicate that MVA-CR19.GFP may have longer replication cycles under the chosen conditions and that the RT has to be adjusted accordingly for scale-up.
Overall, our results demonstrate that at least some recombinant MVA virus strains can be stably and efficiently propagated in TSB systems designed for continuous and semi-continuous production of MVA-based recombinant vaccines and viral vectors.