The production of recombinant glycoproteins from mammalian cell cultures requires robust processes that can achieve high protein yield while ensuring the efficacy of these proteins as human therapeutics. We describe two approaches currently being developed in our group to genetically engineer cell lines with desirable characteristics for recombinant protein production. To enhance the degree of sialylation in the glycoprotein product, we propose to increase intracellular sialic acid availability by overexpressing the CMP-sialic acid transporters. We are also interested in engineering mammalian cells that can proliferate at reduced cultivation temperatures. Low temperature cultivation of mammalian cells has been shown to enhance glycoprotein production but reduces cell growth. It is hypothesized that a mutant cell line that can proliferate at low temperatures may be coupled with low temperature cultivation to improve recombinant protein production. / Singapore-MIT Alliance (SMA)

<p>The goal of this work was to contribute to the fed-batch process optimisation task by deriving parameters that have considerable impact on productivity as well as product quality The chosen parameters were I) the design of the glucose feed profile, II) the choice of induction strategy, with respect to the method of addition, and III) the time of the induction, with respect to the specific glucose consumption rate. </p><p>The present fed-batch experiments using the lacUV5-promoter, for production of b-galactosidase, have shown that a high glucose feed rate gives a specific production rate, q_p, that is twice as high, after induction, compared to a feed rate that is 2.5 times lower. The constant accumulation of lacZ-mRNA indicates that the translational capacity is initially limiting the synthesis machinery, but after four hours of maximum specific production and a corresponding drop in lacZ-mRNA production, the cultivation is likely to be transcription limited. The high feed-rate system resulted in high accumulation of β-galactosidase, corresponding to 40% of total cellular proteins.</p><p>By design of feed profiles in a fed-batch process the detrimental effects of overflow metabolism, giving acetic acid formation, can be avoided. However, the results show that a one-dose addition of isopropyl-β-D-galactopyranoside (IPTG), provokes a non-growth associated production of acetic acid. This response can be alleviated by; lowering the inducer concentration (in this case to below 165 μM), by further reducing the feed rate of glucose or by using alternative induction methods. The use of a stepwise addition or a feed of IPTG thus delayed and reduced the level of acetic acid accumulation. It was also shown that a small change in the time-point of induction lead to large variability, regarding both productivity and acetic acid accumulation, in a fed-batch cultivation, </p><p>In order to further investigate the protein quality two additional proteins were studied in fed-batch cultivations using high and low glucose feed. The aim was to prove the hypothesis that the feed related change in the rate of synthesis of the nascent polypeptide controls the product quality. For the two proteins: Zb-MalE (wt) and Zb-MalE31 (mutant), the transcription rate, in terms of amount of IPTG, and translation rate, in terms of changes in feed rate, influences the percentage of inclusion body formation and degradation of nascent polypeptide. The data show a higher rate of inclusion body formation for the model protein Zb-MalE31 during high feed rate cultivations, as well as at high levels of inducer. Furthermore, the rate of proteolysis was significantly higher for a high feed rate. The high feed rate thus results in a higher rate of synthesis but a lower corresponding quality, for the model proteins studied.</p><p>In the present investigation of fed-batch cultivations using several different expression vectors, it was found that the central alarmone guanosine tetraphosphate (ppGpp) was formed at both high and low feed rates upon induction. It could be shown, however, that by secretion of Zb-MalE to the periplasm, the stringent response could be avoided. This might be due to the decreased burden on the host where the secretion of product further seems to make the cell able to redirect the carbon flux from overflow metabolism, since no acetic acid was produced. The secretion also demonstrates that the growth arrest could be aborted, which is otherwise gained in the P_malKproduction system.</p><p>A novel fed-batch process based on the promoters for the universal stress proteins A and B (P_uspA, P_uspB) was designed to make use of these powerful promoters in an industrial production context. It was concluded that the process had to start from a high specific growth rate and induction was performed once a limiting feed started. This was done to purposely induce the stringent response and/or acetic acid accumulation since this was required for induction. In the suggested system, induction has to be performed and maintained at continuous substrate feeding, whilst avoiding exceeding the cellular capacity, since the stationary phase starvation alone did not lead to production. In conclusion, a new stress induction based production system was achieved resulting in high accumulations of product protein without any detected metabolic side effects.</p>

The goal of this work was to contribute to the fed-batch process optimisation task by deriving parameters that have considerable impact on productivity as well as product quality The chosen parameters were I) the design of the glucose feed profile, II) the choice of induction strategy, with respect to the method of addition, and III) the time of the induction, with respect to the specific glucose consumption rate. The present fed-batch experiments using the lacUV5-promoter, for production of b-galactosidase, have shown that a high glucose feed rate gives a specific production rate, qp, that is twice as high, after induction, compared to a feed rate that is 2.5 times lower. The constant accumulation of lacZ-mRNA indicates that the translational capacity is initially limiting the synthesis machinery, but after four hours of maximum specific production and a corresponding drop in lacZ-mRNA production, the cultivation is likely to be transcription limited. The high feed-rate system resulted in high accumulation of β-galactosidase, corresponding to 40% of total cellular proteins. By design of feed profiles in a fed-batch process the detrimental effects of overflow metabolism, giving acetic acid formation, can be avoided. However, the results show that a one-dose addition of isopropyl-β-D-galactopyranoside (IPTG), provokes a non-growth associated production of acetic acid. This response can be alleviated by; lowering the inducer concentration (in this case to below 165 μM), by further reducing the feed rate of glucose or by using alternative induction methods. The use of a stepwise addition or a feed of IPTG thus delayed and reduced the level of acetic acid accumulation. It was also shown that a small change in the time-point of induction lead to large variability, regarding both productivity and acetic acid accumulation, in a fed-batch cultivation, In order to further investigate the protein quality two additional proteins were studied in fed-batch cultivations using high and low glucose feed. The aim was to prove the hypothesis that the feed related change in the rate of synthesis of the nascent polypeptide controls the product quality. For the two proteins: Zb-MalE (wt) and Zb-MalE31 (mutant), the transcription rate, in terms of amount of IPTG, and translation rate, in terms of changes in feed rate, influences the percentage of inclusion body formation and degradation of nascent polypeptide. The data show a higher rate of inclusion body formation for the model protein Zb-MalE31 during high feed rate cultivations, as well as at high levels of inducer. Furthermore, the rate of proteolysis was significantly higher for a high feed rate. The high feed rate thus results in a higher rate of synthesis but a lower corresponding quality, for the model proteins studied. In the present investigation of fed-batch cultivations using several different expression vectors, it was found that the central alarmone guanosine tetraphosphate (ppGpp) was formed at both high and low feed rates upon induction. It could be shown, however, that by secretion of Zb-MalE to the periplasm, the stringent response could be avoided. This might be due to the decreased burden on the host where the secretion of product further seems to make the cell able to redirect the carbon flux from overflow metabolism, since no acetic acid was produced. The secretion also demonstrates that the growth arrest could be aborted, which is otherwise gained in the PmalK production system. A novel fed-batch process based on the promoters for the universal stress proteins A and B (PuspA, PuspB) was designed to make use of these powerful promoters in an industrial production context. It was concluded that the process had to start from a high specific growth rate and induction was performed once a limiting feed started. This was done to purposely induce the stringent response and/or acetic acid accumulation since this was required for induction. In the suggested system, induction has to be performed and maintained at continuous substrate feeding, whilst avoiding exceeding the cellular capacity, since the stationary phase starvation alone did not lead to production. In conclusion, a new stress induction based production system was achieved resulting in high accumulations of product protein without any detected metabolic side effects. / <p>QC 20101008</p>

Transglutaminases (EC 2.3.2.13) are enzymes that catalyze an acyl transfer reaction between a &gamma / -carboxyamide group of a peptide bound glutaminyl residue (acyl donor) and a variety of primary amines (acyl acceptors), including the amino group lysine. Transglutaminase has a potential in obtaining proteins with novel properties, improving nutritional quality of foods with the addition of essential amino acids, preparing heat stable gels, developing rheological properties and mechanical strength of foods and reducing the applications of food additives. The aim of this study is to develop intracellular and extracellular microbial protransglutaminase (pro-MTG) producing recombinant Pichia pastoris strains by using genetic engineering techniques. In this context first,protransglutaminase gene (pro-mtg) from Streptomyces mobaraensis was amplified by PCR both for intracellular and extracellular constructs using proper primers then they were cloned into the pPICZ&alpha / -A expression vectors, separately. Both intracellular (pPICZ&alpha / A::pro-mtgintra) and extracellular (pPICZ&alpha / A::pro-mtgextra) constructs were prepared with strong alcohol oxidase 1 promoter which is induced by methanol. Pichia pastoris X33 cells were transfected by linear pPICZ&alpha / A::pro-mtgintra and pPICZ&alpha / A::pro-mtgextra, separately and plasmids were integrated into the Pichia pastoris X33 genome at AOX1 locus. After constructing the recombinant P. pastoris strains, batch shaker bioreactor experiments were performed for each recombinant cell and the best producing strains were selected according to Dot blot and SDS-PAGE analyses. The selected recombinant P. pastoris strains, carrying pPICZ&alpha / A::promtgextra gene and pPICZ&alpha / A::pro-mtgintra gene in their genome were named as E8 and I1, respectively. Afterwards, a controlled pilot scale bioreactor experiment in a working volume of 1 L was performed with E8 clone and produced pro-MTG was activated by Dispase I. The variations in the recombinant MTG activity, cell concentration, total protease activity, AOX activity and organic acid concentrations throughout the bioprocess were analyzed and specific growth rates, specific consumption rates and yield coefficients were calculated regarding to measured data. Maximum MTG activity was obtained as 4448 U L- 1 and the maximum cell concentration was measured as 74.1 g L-1 at t=36 h of the bioprocess. In this study, an active transglutaminase enzyme was produced extracellularly by P. pastoris for the first time and the third highest extracellular MTG activity was achieved with E8 clone.

Disposable technology has gained increasing acceptance in the biopharmaceutical industry over the last decade, and provides many advantages over conventional stainless steel equipment. Disposable rocking bioreactors (RBs) are widely employed for cultivation of recombinant mammalian and insect cell lines, although the perception of inadequate mass transfer has prevented their application to bioprocesses based on microbial platforms. In an effort to thoroughly evaluate the suitability of disposable RBs for cultivation of aerobic microorganisms, a comparative study of one-dimensional (1D) and two-dimensional (2D) disposable RBs, and the conventional stirred tank reactor (STR) was performed. The comparison involved: 1) physical characterization of oxygen mass transfer efficiency and mixing intensity, 2) batch cultivation of Escherichia coli BL21 for comparison of growth characteristics, and 3) batch cultivation of recombinant E. coli BL21 expressing a clinical therapeutic, hCD83ext (the extracytoplasmic domain of human CD83). Oxygen mass transfer (evaluated as the mass transfer coefficient, kLa) was comparable between the 1D RB and STR (approximately 150 h-1) at low working volume (WV), declining linearly with increasing WV, while kLa was highest in the 2D RB for all tested WVs, providing the maximum kLa (394 h-1) at 3 L WV. Fast mixing (t95 of 8-20 s) was observed in all three systems for water and aqueous carboxymethylcellulose (CMC) solutions. Batch growth characteristics of E. coli BL21 were similar in each system, although acetate accumulation was significant in the 1D RB. Batch production of GST-hCD83ext (glutathione S-transferase-hCD83ext fusion protein) resulted in similar soluble protein yields and inclusion body formation between bioreactors. Although cell growth and protein expression were comparable between all bioreactors, the 1D RB is not considered a suitable cultivation system for E. coli under experimental conditions given the significant acetate accumulation observed and high supplemental oxygen requirement for low cell density cultures. On the other hand, considering its formidable mass transfer capacity and overall performance in batch cultivations, the CELL-tainer® is an attractive alternative to the STR for cultivation of recombinant E. coli expressing high value therapeutic proteins.

Over the past decade, plants have been used as expression hosts for the production of pharmaceutically important and commercially valuable proteins. Plants offer many advantages over other expression systems such as lower production costs, rapid scale up of production, similar post-translational modification as animals and the low likelihood of contamination with animal pathogens, microbial toxins or oncogenic sequences. However, improving recombinant protein yield remains one of the greatest challenges to molecular farming. In-Plant Activation (InPAct) is a newly developed technology that offers activatable and high-level expression of heterologous proteins in plants. InPAct vectors contain the geminivirus cis elements essential for rolling circle replication (RCR) and are arranged such that the gene of interest is only expressed in the presence of the cognate viral replication-associated protein (Rep). The expression of Rep in planta may be controlled by a tissue-specific, developmentally regulated or chemically inducible promoter such that heterologous protein accumulation can be spatially and temporally controlled. One of the challenges for the successful exploitation of InPAct technology is the control of Rep expression as even very low levels of this protein can reduce transformation efficiency, cause abnormal phenotypes and premature activation of the InPAct vector in regenerated plants. Tight regulation over transgene expression is also essential if expressing cytotoxic products. Unfortunately, many tissue-specific and inducible promoters are unsuitable for controlling expression of Rep due to low basal activity in the absence of inducer or in tissues other than the target tissue. This PhD aimed to control Rep activity through the production of single chain variable fragments (scFvs) specific to the motif III of Tobacco yellow dwarf virus (TbYDV) Rep. Due to the important role played by the conserved motif III in the RCR, it was postulated that such scFvs can be used to neutralise the activity of the low amount of Rep expressed from a “leaky” inducible promoter, thus preventing activation of the TbYDV-based InPAct vector until intentional induction. Such scFvs could also offer the potential to confer partial or complete resistance to TbYDV, and possibly heterologous viruses as motif III is conserved between geminiviruses. Studies were first undertaken to determine the levels of TbYDV Rep and TbYDV replication-associated protein A (RepA) required for optimal transgene expression from a TbYDV-based InPAct vector. Transient assays in a non-regenerable Nicotiana tabacum (NT-1) cell line were undertaken using a TbYDV-based InPAct vector containing the uidA reporter gene (encoding GUS) in combination with TbYDV Rep and RepA under the control of promoters with high (CaMV 35S) or low (Banana bunchy top virus DNA-R, BT1) activity. The replication enhancer protein of Tomato leaf curl begomovirus (ToLCV), REn, was also used in some co-bombardment experiments to examine whether RepA could be substituted by a replication enhancer from another geminivirus genus. GUS expression was observed both quantitatively and qualitatively by fluorometric and histochemical assays, respectively. GUS expression from the TbYDV-based InPAct vector was found to be greater when Rep was expected to be expressed at low levels (BT1 promoter) rather than high levels (35S promoter). GUS expression was further enhanced when Rep and RepA were co-bombarded with a low ratio of Rep to RepA. Substituting TbYDV RepA with ToLCV REn also enhanced GUS expression but more importantly highest GUS expression was observed when cells were co-transformed with expression vectors directing low levels of Rep and high levels of RepA irrespective of the level of REn. In this case, GUS expression was approximately 74-fold higher than that from a non-replicating vector. The use of different terminators, namely CaMV 35S and Nos terminators, in InPAct vectors was found to influence GUS expression. In the presence of Rep, GUS expression was greater using pInPActGUS-Nos rather than pInPActGUS-35S. The only instance of GUS expression being greater from vectors containing the 35S terminator was when comparing expression from cells transformed with Rep, RepA and REnexpressing vectors and either non-replicating vectors, p35SGS-Nos or p35SGS-35S. This difference was most likely caused by an interaction of viral replication proteins with each other and the terminators. These results indicated that (i) the level of replication associated proteins is critical to high transgene expression, (ii) the choice of terminator within the InPAct vector may affect expression levels and (iii) very low levels of Rep can activate InPAct vectors hence controlling its activity is critical. Prior to generating recombinant scFvs, a recombinant TbYDV Rep was produced in E. coli to act as a control to enable the screening for Rep-specific antibodies. A bacterial expression vector was constructed to express recombinant TbYDV Rep with an Nterminal His-tag (N-His-Rep). Despite investigating several purification techniques including Ni-NTA, anion exchange, hydrophobic interaction and size exclusion chromatography, N-His-Rep could only be partially purified using a Ni-NTA column under native conditions. Although it was not certain that this recombinant N-His-Rep had the same conformation as the native TbYDV Rep and was functional, results from an electromobility shift assay (EMSA) showed that N-His-Rep was able to interact with the TbYDV LIR and was, therefore, possibly functional. Two hybridoma cell lines from mice, immunised with a synthetic peptide containing the TbYDV Rep motif III amino acid sequence, were generated by GenScript (USA). Monoclonal antibodies secreted by the two hybridoma cell lines were first screened against denatured N-His-Rep in Western analysis. After demonstrating their ability to bind N-His-Rep, two scFvs (scFv1 and scFv2) were generated using a PCR-based approach. Whereas the variable heavy chain (VH) from both cell lines could be amplified, only the variable light chain (VL) from cell line 2 was amplified. As a result, scFv1 contained VH and VL from cell line 1, whereas scFv2 contained VH from cell line 2 and VL from cell line 1. Both scFvs were first expressed in E. coli in order to evaluate their affinity to the recombinant TbYDV N-His-Rep. The preliminary results demonstrated that both scFvs were able to bind to the denatured N-His-Rep. However, EMSAs revealed that only scFv2 was able to bind to native N-His-Rep and prevent it from interacting with the TbYDV LIR. Each scFv was cloned into plant expression vectors and co-bombarded into NT-1 cells with the TbYDV-based InPAct GUS expression vector and pBT1-Rep to examine whether the scFvs could prevent Rep from mediating RCR. Although it was expected that the addition of the scFvs would result in decreased GUS expression, GUS expression was found to slightly increase. This increase was even more pronounced when the scFvs were targeted to the cell nucleus by the inclusion of the Simian virus 40 large T antigen (SV40) nuclear localisation signal (NLS). It was postulated that the scFvs were binding to a proportion of Rep, leaving a small amount available to mediate RCR. The outcomes of this project provide evidence that very high levels of recombinant protein can theoretically be expressed using InPAct vectors with judicious selection and control of viral replication proteins. However, the question of whether the scFvs generated in this project have sufficient affinity for TbYDV Rep to prevent its activity in a stably transformed plant remains unknown. It may be that other scFvs with different combinations of VH and VL may have greater affinity for TbYDV Rep. Such scFvs, when expressed at high levels in planta, might also confer resistance to TbYDV and possibly heterologous geminiviruses.

Abstract Replicative DNA polymerases (pols) synthesize chromosomal DNA with high accuracy and speed during cell division. In eukaryotes the process involves three family B pols (α, δ, ε), whereas in Archaea, two types of pols, families B and D, are involved. In this study the B-subunits of replicative pols were analysed at the DNA, RNA and protein levels. By cloning the cDNAs for the B-subunits of human and mouse pol ε we were able to show that the encoded proteins are not only homologous to budding yeast pol ε, but also to the second largest subunit of pol α. Later studies have revealed that the B-subunits are conserved from Archaea to human, and also that they belong to the large calcineurin-like phosphoesterase superfamily consisting of a wide variety of hydrolases. At the mRNA level, the expression of the human pol ε B-subunit was strongly dependent on cell proliferation as has been observed for the A-subunit of pol ε and also for other eukaryotic replicative pols. By analysing the promoter of the POLE2 gene encoding the human pol ε B-subunit we show that the gene is regulated by two E2F-pocket protein complexes associated with the Sp1 and NF-1 transcription factors. Comparison of the promoters of the human pol ε and the pol α B-subunit indicates that the genes for the B-subunits may be generally regulated through E2F-complexes whereas adjustment of the basal activity may be achieved by distinct transcription factors. To clarify the function of the B-subunits, we screened through the expression of 13 different recombinant B-subunits. Although they were mainly expressed as insoluble proteins in E. coli, we were able to optimize the expression and purification for the B-subunit (DP1) of Methanococcus jannaschii pol D (MjaDP1). We show that MjaDP1 alone was a manganese dependent 3'-5' exonuclease with a preference for mispaired nucleotides and single-stranded DNA, suggesting that MjaDP1 functions as the proofreader of archaeal pol D. So far, pol D is the only pol family utilising an enzyme of the calcineurin-like phosphoesterase superfamily as a proofreader.

Several expression systems for recombinant protein production, essentially cells or whole organisms are currently in use today. Recently, research into recombinant protein production revealed a more attractive expression system based on the microalgae, C. reinhardtii, for significant savings in cost and production of correctly folded recombinant proteins. However, protein yield in the microalgae remain very low, non-predictable and whether this was due to limitations in the system was unclear. Using the expression of E. coli β-glucuronidase (gus) in C. reinhardtii chloroplast, the overall aim of the project was to address if the low recombinant gus yield in C. reinhardtii was due to limitations that affect growth and protein production, and if the fluxes for recombinant gus production were suboptimal (limiting). The finding was used to implement a strategy for a more predictable recombinant protein yield in C. reinhardtii. The research involved a range of experiments, analysis, and Flux Balance Analysis (FBA) modelling. The growth of C. reinhardtii cultures were characterized in autotrophic, heterotrophic and mixotrophic conditions to identify factors that limit growth and recombinant gus yields. These factors were availability of light, carbon and nitrogen substrates, pH changes, protein burden and energetic limitation (ATP). The highest biomass was obtained in autotrophic and mixotrophic cultures (>1 g/litre), the lowest biomass was in heterotrophic cultures (~0.4 g/litre). The recombinant gus yields on the basis of dry cell weight were: mixotrophic cultures (0.038%), autotrophic cultures (0.032%), heterotrophic cultures (0.026%). No detectable protein burden was observed for expression of recombinant gus in autotrophic and mixotrophic conditions, but protein burden was significant in heterotrophic condition (15 – 18% reduction in growth rate). A strategy that significantly increased growth and cell productivity (>3 fold) in heterotrophic condition was identified. FBA was used to identify suboptimal amino acid steady state fluxes (bottlenecks) that limited the gus yield. Using FBA modelling, model verifications and corrections, a strategy that significantly increased the yield of recombinant gus in each cell (~2 fold) was identified. Put together, the total increase represents a 6 fold increase in recombinant gus yield. Furthermore, this research presented a framework for identifying, analysing and understanding the effect of the uptake of individual amino acid towards recombinant protein yield.

Thesis (MScEng)--Stellenbosch University, 2012. / ENGLISH ABSTRACT: Recombinant glycoproteins are important biopharmaceuticals, providing solutions for numerous previously untreatable illnesses, in everything from cancer to infertility. Most recombinant biopharmaceuticals are produced in mammalian cells due to their ability to provide the correct post-translational processing for use in humans. The post-translation processing influences many of the protein’s properties including pharmacokinetics, bioactivity, secretion, half-life, solubility, recognition and antigenicity. The aim of this thesis is to further study the upstream production of a glycosylated recombinant protein produced by Chinese hamster ovary (CHO) cells on production scale within the confines of an existing process. The process in question uses adherent CHO cells to produce a glycosylated recombinant hormone. As with most recombinant protein production processes, this process has two sections to the upstream production: a seed train to grow enough cells to inoculate production, and a production section, which focuses on the production of a recombinant protein. The seed train is predominantly conducted in roller bottles, while the production section takes place in perfusion bioreactors, where the cells are attached to microcarriers, with spin-filters for cell retention. The whole process uses medium with serum. There are two process challenges regarding an existing recombinant-protein production process: 1. The gradual increase, over the past several campaigns, of the final population doubling level of the cells (which must remain within certain specified limits) at the end of the seed train. 2. The low glycosylation levels of the product seen in certain campaigns, which meant that a certain number of final product batches were below the specified acceptable glycosylation limits. Following a literature survey several controlled process variables were chosen for investigation and hypotheses made on their effect on the seed train or glycosylation. To investigate their effect on the PDL and cell growth in the seed train: - Medium volume: decreasing the medium volume will yield a lower PDL due to slower cell growth caused by lower glucose availability. - Seeding density: if cells obtain confluence by the time they are harvested, decreasing the seeding density will yield a higher PDL. - Cultivation temperature: decreasing the temperature ought to decrease the growth rate. - Medium feed temperature: there will be no significant difference to the cell culture when pre-heated or cold medium is used. Aeration: using vent caps will increase the oxygen content of the medium in the roller bottles and the cell growth, yielding a higher PDL. To investigate their effect on glycosylation during production: - pH: better glycosylation will be seen at pH 6.9, than at pH 6.7. - Perfusion rate: a higher perfusion rate will lead to better glycosylation due to increased glucose and glutamine concentrations. In the seed train, the only factor that significantly influenced the final PDL was the seeding density. Cell growth was inhibited once cells reached confluence, so lowering the seeding density lead to a higher PDL. It is recommended to use a high seeding density to ensure a lower PDL. Historic data indicated that the seeding density was not the cause of the apparent increase of the final PDL, as all previous campaigns had been seeded with a high seeding density. What then became apparent was that the final PDL remained relatively constant during a campaign and that the increase in final PDL occurred between campaigns. It appears that the apparent increase in the final PDL is due to differences in cell counting between operators as each new campaign was managed by different operators. It is recommended that a mechanical cell counter be used to verify cells counts and to maintain a standard between campaigns. In the bioreactors, varying the pH proved to have no significant effect on the glycosylation levels. However, both the initial perfusion rate and the specific perfusion rate proved to be important from both historical data and the data generated during these experiments. Lower levels of the initial perfusion rate lead to better glycosylation and it is recommended that an initial perfusion rate of 1.0 volumes/day be used. The relationship between the specific perfusion rate and the glycosylation appears to be non-linear and requires further study, for now it is recommended that the specific perfusion rate be kept below 0.3 volumes/day/109 cells. Probable reasons for the unsatisfactory glycosylation seen in certain runs could also be proposed from these two factors: • RP33-133 : Very high specific perfusion rate • RP32-135 : High initial perfusion rate and very high specific perfusion rate • RP32-138 : High initial perfusion rate • RP33-139 : High initial perfusion rate Further research is recommended into the effect of the specific perfusion rate as well as the specific glucose consumption rate and the specific glutamine concentration on the glycosylation. / AFRIKAANSE OPSOMMING: Rekombinante glikoproteïene is baie belangrike biofarmaseutiese produkte wat oplossings bied vir talle voorheen ongeneeslike siektes in alles van kanker tot onvrugbaarheid. Meeste rekombinante farmaseutiese produkte word gemaak deur diere-selle as gevolg van hulle bevoegtheid om die korrekte na-translasie stappe te volg sodat die produkte in mense gebruik kan word. Die na-translasie stappe beïnvloed baie van die proteïene se karaktertreke insluitende die farmakokinetika, bioaktiwiteit, uitskeiding, half-leeftyd, oplosbaarheid, herkenbaarheid and antigeniciteit. Die doel van hierdie tesis is om die stroomop produksie van ‘n rekombinante glikoproteïene vervaardig deur Chinese hamster ovariale (CHO) selle verder te bestudeer binne die grense van ‘n bestaande proses op grootskaalse vlak. Die huidige proses gebruik CHO selle om ‘n rekombinante glikohormoon te produseer. Soos meeste prosesse wat rekombinante proteïene produseer bestaan die stroomop gedeelte van die proses uit twee dele: ‘n saad trein wat genoeg selle maak vir produksie en ‘n produksie gedeelte wat fokus op die vervaardiging van die glikoproteïen. Die saad trein bestaan hoofsaaklik uit roller bottels terwyl produksie plaasvind in perfusie bioreaktors waar die selle op “microcarriers” groei, met spin-filters om die selle binne die bioreaktors te hou; die hele proses gebruik medium met serum. Daar is twee probleme in die stroomop gedeelte van die bestaande proses: 1. Die geleidelike toename oor die afgelope paar jaar van die finale verdubbelingsvlak van die selle aan die einde van die saad trein 2. Die lae glukosilering van die eindproduk wat veroorsaak dat sekere lotnommers buite spesifikasie is Na ‘n literatuur studie, was seker beheerde proses parameters gekies om verder te bestudeer en hipotesisse gemaak oor hulle effek op die saad trein of die vlak van glukosilering. Die volgende faktore is bestudeer vir hulle effek op die finale verdubbelingsvlak van die selle in die saad trein: - Medium volume: ‘n laer medium volume sal lei tot a laer verdubbelingsvlak van die selle as gevolg van stadige groei - Konsentrasie van selle vir inokulasie: as die selle konfluent is teen die tyd wat hulle versamel word sal ‘n laer konsentrasie selle lei tot ’n hoër verdubellingsvlak. - Temperatuur: laer temperatuur behoort te lei tot ‘n stadiger groei koers van die selle - Medium voer-temperatuur: die voer-temperatuur van die medium sal geen beduidende verskil maak - Belugting: die gebruik van “vent-caps” sal die suurstof inhoud van die roller bottels verhoog Die volgende faktore is bestudeer vir hulle effek op die glukosilering tydens produksie: - pH: beter glukosilering word verwag by by pH 6.9 dan by pH 6.7 - Perfusie koers: ‘n hoër perfusie koers sal lei tot beter glukosilering as gevolg van hoër glukose en glutamien konsentrasies Die konsentrasie van die selle wat gebruik word vir inokulasie blyk die enigste faktor te wees wat die finale verdubbelingsvlak van die selle en die groei van die selle in die saad trein beïnvloed het. Die groei van die selle was beprek wanneer die selle konfluent geraak het en dus het ‘n laër sel konsentrasie by inokulasie gelei tot ‘n hoër sel verdubbelingsvlak. Dit word aanbeveel dat ‘n hoë sel konsentrasie by inokulasie gebruik word. Die geleidelike toename van die finale verdubbelingsvlak van die selle in die saad trein is waarskynlik as gevolg van die variasie in sel tellings tussen verskillende operateurs eerder as as gevolg van die beheerde proses parameters. Dit word aanbeveel dat ‘n meganiese sel-teller gebruik word om die verskil in sel tellings tussen operateurs te kontroleer en om ‘n standaard te handhaaf tussen produksie lotte. In die bioreaktors, het die pH geen beduidende invloed gehad op die glukosilering maar uit historiese data en die huidige data van hierdie eksperimente blyk albei die begin perfusie koers en die spesifieke perfusie koers ‘n belangrike invloed te hê op die glukosilering. Laër vlakke van die begin perfusie koers lei tot beter glikosilsie en dit word aanbeveel dat elke produksielot ‘n begin perfusie koers het van 1.0 volume/dag. Die verhouding tussen die glukosilering en die spesifieke perfusie koers blyk om nie-liniêr te wees nie. Nog navorsing hieroor word aanbeveel, maar vir nou word dit aanbeveel dat die spesifieke perfusie koers onder 0.3 volumes/dag/109 selle gehou word. Hierde twee faktore blyk die oorsaak te wees vir die lae glukosilering wat in sekere produksielopies gevind was: • RP33-133 : baie hoë spesifieke perfusie koers • RP32-135 : hoë begin perfusie koers en baie hoe spesifieke perfusie koers • RP32-138 : hoë begin perfusie koers • RP33-139 : hoë begin perfusie koers Dit word aanbeveel dat verdere navorsing gedoen word op die effek van die spesifieke perfusie koers asook die spesifieke koers van glukose verbruik en die spesifieke glutamien konsentrasie op die glukosilering van die produk.

Protéines difficiles à exprimer: un goulot d'étranglement pour la plupart des biologistes. J'ai choisi d'utiliser comme modèle d’étude Acanthamoeba polyphaga Mimivirus. Ce virus géant à ADN possède des protéines subissant des modifications post-traductionnelles, des structures multi-protéiques ou encore des voies enzymatiques jamais identifiées auparavant dans un virus, ce qui en font un modèle idéal pour l’étude de protéines récalcitrantes. Le but ultime de cette thèse, était de produire les protéines de capsides de Mimivirus. Le rôle de la protéine de capside dans l’assemblage de la particule virale, son infectivité et ses caractéristiques moléculaires sont d’une grande importance. Pour aller du gène à la protéine, J’ai participé à la compréhension de ce qui gouverne la terminaison de la transcription de Mimivirus et également participé à l'analyse globale du transcriptome au cours du cycle d'infection des amibes par Mimivirus. Nous avons montré que les transcrits de Mimivirus sont systématiquement polyadénylés dans des régions formant une structure secondaire en tige-boucle, même s’il n’existe pas de signal de polyadénylation canonique en amont. Nous en avons conclu que la polyadénylation de Mimivirus suit exclusivement une règle «épingle à cheveux». De plus, l’étude du transcriptome a révélé 3 phases temporelles distinctes dans le cycle infectieux: précoce, intermédiaire et tardive. Les transcrits de capsides sont tous exprimés durant la phase tardive mais leur profil d’expression ne sont pas superposables dans le temps. Les données de transcriptomique ont révélées la présence de plusieurs glycosyltransférases chez Mimivirus, dans la phase tardive du cycle, concomitant avec la production de la protéine de capside. Les informations recueillies sur l'expression des gènes à différents temps post-infection ont contribué à la conception de protocoles pour la production des protéines de capsides (la protéine majeure de capside (MCP) et ses paralogues) dans de systèmes eucaryote. / Difficult to express proteins: a bottleneck for most biologists. I have chosen to use Acanthamoeba polyphaga Mimivirus as my study model. This giant dsDNA virus possesses post-translationally modified proteins, multi-protein structures and enzyme pathways never before seen in a virus, which makes it ideal for refractory studies. The ultimate goal of my thesis was to produce the capsid proteins of Mimivirus. The role of the capsid protein in the assembly of the viral particle, its infectivity, and molecular features are of great importance. To go from gene to protein, I participated in the comprehension of what governs the post-transcriptional termination in Mimivirus and equally participated in the global analysis of the transcriptome during the infectious cycle of Acanthamoeba by Mimivirus. We have shown that the Mimivirus transcripts are systematically polyadenylated in the regions forming a stem-loop secondary structure; even when a canonical poyadenylation signal is absent We concluded that Mimivirus polyadenylation obeys a strict “Hairpin rule”. Moreover, the transcriptomic study revealed three distinct temporal phases: early, intermediate and late. The capsid transcripts are all expressed during the late phase but their expression profiles are not superimposable. The transcriptomic data also revealed the presence of several Mimivirus glycosyltransferases in the late temporal phase, concomitant with the capsid proteins. The expression data gathered throughout my thesis has contributed to the rational design of a protein production experiment to produce the major capsid protein and its three paralogs in eukaryotic systems.