Abstract
Keywords
Introduction
The methylotrophic yeast Pichia pastoris is a well-established expression host which is often used in the production of protein pharmaceuticals (1-3). It can produce high levels of recombinant proteins using a strong and tightly regulated methanol-inducible alcohol oxidase promoter (AOX1) (4, 5). The most widely utilized fermentation process of P. pastoris consists of a three steps approach (6). During the first step, cells are cultured in batches using a defined medium with glycerol as the carbon source to rapidly achieve high cell densities. As the AOX1 promoter is repressed by unlimited growth on glycerol (7, 8) recombinant protein expression is repressed at this stage. During the second step, in order to increase biomass production and de-repress the methanol metabolic machinery, a glycerol-limited fed-batch procedure is initiated. This phase leads to gradual de-repression of the enzymes necessary for the dissimilation of methanol and reduces the time necessary for the cells to adapt to growth on methanol (9). Finally, recombinant protein expression is usually induced by feeding methanol as the sole carbon source.
A fermentation guideline for both Mut+ and Muts strains of P. pastoris is available from Invitrogen (10). Stratton et al. devised a protocol for P. pastoris high cell-density fermentation, in which detailed procedures are provided (6). Using this protocol, in our laboratory, recombinant human growth hormone (rhGH) was produced with P. pastoris Mut+ in which AOX1 promoter was induced with methanol for 30 h.
However, the methanol feed rate profiles described by Stratton et al. are fixed and may be inapplicable for those strains whose ability to utilize methanol has changed as a result of the expression of heterologous genes. For a fed-batch fermentation process, the substrate feed rate usually needs to be optimized to maximize productivity. Various methods for such optimization have been reported in other production systems (11).
Methanol can act as both the carbon source and the inducer of the expression of recombinant proteins. However, in the presence of high concentrations of methanol, which has a high substrate affinity for alcohol oxidase, P. pastoris tends to intoxicate itself with metabolites (formaldehyde, formic acid) (12). Hence, at high concentrations, methanol inhibits the organism’s growth. Therefore, in order to keep methanol concentration below the toxic limit, fed-batch operation has been utilized as the standard protocol for recombinant protein production by P. pastoris through AOX1 promoter (13).
Since accumulation of methanol leads to cytotoxic effects, so methanol mixed feeding strategies have been studied to partially replace or at least complement methanol with other carbon sources such as glycerol (14-16) glucose (17-19) or sorbitol (20-24). Moreover, the use of a less repressing carbon source may result in higher specific production rates, improving overall productivity and eliminating the need for the tight control of residual substrate levels (25). Among them, sorbitol is a widely accepted non-repressive carbon source for P. pastoris (26). The advantages of mixed feeds of sorbitol and methanol for the production of different recombinant proteins with P. pastoris have been reported (20-25, 27and 28).
As a follow-up to other studies, this work aimed to compare the effect of various concentrations of sorbitol in mixed feeding strategy with stepwise addition of methanol to develop a new experimental method that would maximize the production of hGH in P. pastoris. In this study sorbitol was added batch-wise to the medium at the beginning of the induction phase, continuing with methanol feeding for 30 h. In order to understand the effects of various feeding strategies, based on different co-substrate concentrations, on production of hGH in P. pastoris, cell density, total protein, hGH expression level and hGH concentration were analyzed and the results compared with the basic protocol of methanol feeding using one-way analysis of variance (ANOVA).
Experimental
Microorganism, inoculum and media preparation
P. pastoris GS 115 strain Mut+ carrying hGH cDNA under the control of AOX1 which secrets the target protein into the fermentation broth was streaked from glycerol stock onto YPD-agar containing (g/L): yeast extract (10), peptone (20), dextrose (20) and agar (20) and incubated for 48 h at 30 °C (30). A single colony was inoculated into BMGY medium containing 10 g/L yeast extract, 20 g/L peptone, 13.4 g/L YNB, 4 × 10−5 g/L biotin, 10 g/L glycerol and 0.1 M potassium phosphate buffer (29) and incubated at 30 °C in a shaker incubator at 150 rpm, until the culture reached an optical density (OD600) of 1-2.
Fermentation conditions
The culture obtained was used as inoculum for a 13 L fermenter containing 3 L of basal salts medium which consisted of (g/L): glycerol (40); K2SO4 (18); MgSO4.7H2O (14.9); KOH (4.13); CaSO4 (0.9) and 27 mL H3PO4, plus 4.0 mL of a trace metal stock solution that consisted of (g/L): CuSO4.5H2O (6); KI (0.09); MnSO4.H2O (3); H3BO3 (0.02); MoNa2O4.2H2O (0.20); CoCl2 (0.5); ZnCl2 (20); FeSO4·7H2O (65); biotin (0.2) and H2SO4, 5.0 (mL/L) (30).
The 13 L bioreactor (Infors, Switzerland), had a working volume of 9.0–10.0 L and included temperature, pH, foam, stirring rate, feed inlet rate and dissolved oxygen control systems. Dissolved oxygen (DO) concentration was maintained above 20% air saturation at 400-700 rpm, using air and, when needed, enriching the inlet air with pure oxygen passing through a digital mass flow controller. Temperature was maintained constant at 30.0 ± 0.1 °C throughout the entire bioprocess. In the first two phases, the pH was held at 5.0 ± 0.2 and then in the production phase was lowered to 3.0 ± 0.2. The pH was maintained at the relevant values, by adding 25% ammonia solution.
Induction Phase
According to the basic protocol, the induction phase was performed with methanol feed containing 12 PTM1 trace salts per liter of methanol. The feed rate was set to 3.65 mL/h/L initial fermentation volume for six h. Then, the feed rate was doubled to 7.3 mL/h/L initial fermentation volume. After 6 h, feed rate was further increased to 10.9 mL/h/L initial fermentation volume and maintained throughout the remainder of the fermentation up to 30 h.
To conduct a mixed feed strategy, sorbitol at concentrations of 30, 40, 50 and 60 g/L were added to the fermenter in a batch-wise mode and methanol fed-batch was continued based on the basic protocol in which the rate of methanol addition was increased stepwise during the first 12 h of production and then kept constant. To determine the optimal sorbitol concentration for the yeast growth profile and rhGH production, cell density, total protein concentration and expression level of cultures grown using different concentrations of sorbitol were studied.
Analytical procedures
Cell density measurement
Optical density (OD) of cell suspensions was measured at 600 nm. The wet cell weight (WCW, g/L) was used as a measure of cell density within the bioreactor. A 1.0 mL sample was centrifuged at 13,000 rpm for 5 min. The pellet was weighed and the supernatant was stored at 4 °C for further analysis. The dry cell weight (DCW, g/L) was calculated using the following equation DCW = 0.35 × WCW which was obtained from a calibration curve prepared using 20 samples that were dried for 24 h at 105 °C.
Determination of total protein:
Cell suspension was centrifuged at 13,000 rpm for 10 min (Labnet, USA). Since rhGH was secreted into the culture media, the supernatant was used for the determination of total protein concentration by the Bradford assay using a UV/V is spectrophotometer (PerkinElmer, USA), at 595 nm (31). Bovine serum albumin (BSA) was used as the standard protein for this measurement. The total protein concentration of each sample was then estimated from the constructed standard curve.
SDS–PAGE and densitometric analysis
To determine the expression level of rhGH, SDS–PAGE was performed in a Mini-Protean® 3 cell gel apparatus (Bio-Rad, USA) according to the method of Laemmli (32). The samples were dissolved in 10 X sample buffer and incubated at 100 °C for 5 min. About 25 μL of each sample was loaded in the gel of 15% resolving and 5% stacking gel with 0.75 mm thickness at a constant voltage of 100 V. After running, the gel was stained with Coomassie Brilliant Blue R250. Densitometric analysis of the SDS–PAGE gel was performed using TotalLab software (Nonlinear dynamics, USA).
Determination of rhGH Concentration by ELISA
Concentration of rhGH in the samples was measured by an enzyme-linked immunosorbent assay (ELISA) using a commercially available test kit (hGH ELISA, Roche) according to the manufacturer’s protocols. hGH standards were prepared in 1:2 dilution steps from 400 to 12.5 pg/mL. Test samples were diluted in the range of standard concentrations. Two-hundred μL of each standard and sample was added to the pre-coated wells and incubated for 1 h at 37 °C. Then the solution was removed thoroughly and the well rinsed 5 times with 250 μL of washing buffer for 30 s each. Following the washing step, 200 μL of anti-hGH-DIG was added to each well and incubated for 1 h at 37 °C. The washing step was repeated again and 200 μL of anti-hGH-POD was added to each well and incubated for 1 h at 37 °C. Two-hundred μL of POD substrate was added into each well and incubated at 20 °C until color development. The absorbance of the sample was measured at 405 nm with a reference wavelength at 490 nm, using an ELISA reader (Spectrostar Nano, BMG, Germany). The standard curve was constructed by plotting the absorbance for the hGH standards on the y-axis versus the hGH standard concentrations on the x-axis.
Statistical tests
Statistical analysis was performed by GraphPad Prism 6.01 software (GraphPad software, La Jolla, USA). Data were analyzed by one-way ANOVA followed by Tukey›s post-hoc. Differences with p-values of < 0.05 were regarded as significant.
Results
Cell density measurement
The effect of sorbitol concentration combined with stepwise methanol addition in mixed-feed strategy on cell density was investigated during 30 h induction phase. In the methanol fed-batch strategy (basic protocol) cell density, as DCW, was 94.38 g/L. In the presence of sorbitol, cell density was found to be 94.73, 96.83, 108.5 and 108.38 g/L at a concentration of 30, 40, 50 and 60 g/L sorbitol respectively. The effect of sorbitol substrate concentration on cell density was shown in Figure 1.
It has been reported that adding sorbitol to the medium enhances biomass production, achieving higher recombinant protein (20-25, 27 and 28). By increasing the concentration of sorbitol to 50% at the beginning of methanol induction phase (MIP), a significant increase in cell density was observed. Since, there was no significant difference between sorbitol co-substrate at concentrations of 50 g/L and 60 g/L, so, in terms of cell density a mixed feed containing 50 g/L sorbitol was considered as the optimal concentration.
Furthermore, dry cell weight was calculated using the afore-mentioned equation. Results obtained from comparison of different concentrations of sorbitol in mixed feed strategy indicate that there is an increase in dry cell weight with an increase in sorbitol concentration. However, the maximum dry cell weight was observed in the presence of 50 g/L of sorbitol and, again, beyond this concentration no significance increase was observed.
Determination of total protein
The effect of sorbitol-methanol mixed feeding strategy on total protein concentration was also investigated. Addition of different concentrations of sorbitol resulted in significant (p-value = 0.05) increase in total protein concentration in culture medium. According to the obtained results total protein concentration at 30, 40, 50 and 60 g/L of sorbitol was 0.423, 0.490, 0.530, 0.807, 0.844 mg/mL respectively. Statistical analysis using ANOVA revealed a significant difference (p-value = 0.05) between sorbitol mixed-feed at concentrations of 30, 40 and 50 g/L on total protein concentration. However, 50 g/L sorbitol co-substrate was found to be the optimal concentration for induction, as increasing the concentration of sorbitol beyond that did not lead to a significant increase in protein concentration. Total protein concentration under optimal condition reached 0.844 mg/mL which was approximately 2-folds higher than the concentration obtained with the basic protocol (Figure 2).
Expression level
The effect of induction with different concentrations of sorbitol on rhGH expression level showed a similar pattern of increase to that of total protein (Figure 2). However, although at 30 and 40 g/L concentrations of sorbitol, an increase in the expression level was seen, the difference with the basic protocol was not significant, partly due to the high standard deviation of the results of the basic protocol. However, at 50 g/L concentration of sorbitol, the increase in the expression level was large enough to be significantly higher than the basic protocol about 1.2-folds. Again, no significant difference was found between the result of sorbitol concentration of 50 and 60 g/L (Figure 3). The expression level under optimal conditions was 82.66%. Figure 4 shows protein expression and densitometric analysis of three fermentation runs at concentration of 50 g/L.
Measurement of rhGH production
The effect of sorbitol concentration in mixed feed strategy with stepwise addition of methanol on the production of rhGH is shown in Figure 5. The rhGH concentration in the basic protocol was 0.345 g/L but the amount was increased about 2-fold when concentration of sorbitol used was 50 g/L. Statistical analysis of different concentrations of rhGH secreted into the culture medium at different concentrations of sorbitol, in comparison with the basic protocol, showed significant difference in rhGH concentration produced. However, similar to the above results, no statistical significant difference was observed between the effect of sorbitol concentrations of 50 and 60 g/L. So, once again, 50 g/L was found to be the optimal amount of sorbitol with an rhGH production of 0.688 g/L.
Discussion
The feeding rate in MIP is one of the key factors for maximizing protein production (33, 34), because protein production is directly or indirectly associated with cell growth (35). So, different approaches have been proposed to optimize MIP. One strategy to increase the productivity of Pichia expression is the use of a multicarbon substrate in addition to methanol. Accordingly, mixed feeding strategies have been studied to partially replace or at least complement methanol with other carbon sources such as glycerol (14-16) glucose (17-19) or sorbitol (20-25). Among these, sorbitol as a non-repressive carbon source was found the most promising one (27). The benefits of methanol/sorbitol co-feeding with various strategies have been reported by other researchers (20-25, 28 and 29). In the mixed-feed strategy reported by Celik et al. the highest rhGH production and cell concentration achieved was 0.64 g/L and 105 g/L, respectively. In the strategy used, methanol was fed to the system at a predetermined rate of 0.03/h and sorbitol concentration was kept at 50 g/L at t = 0-15 h of rhGH production phase. These results were obtained following 42 h induction time (28).
In the present study, not only the effect of different concentrations of sorbitol was examined but also induction was performed with a continuous feed containing increasing concentration of methanol. The results obtained indicated that addition of sorbitol at a concentration of 50 g/L at the beginning of the induction phase and continuing the induction with methanol for 30 h resulted in maximum biomass and rhGH production. Under these optimal conditions the cell biomass achieved was 108 g/L (DCW), total protein 0.807 g/L, rhGH expression level 83.1% and rhGH concentration was 0.688 g/L. These results were obtained following an induction time of 30 h which is considerably shorter in comparison to the previous studies.
Moreover, the productivity of mixed-feed strategy at optimal conditions within 24 h was comparable with 30 h induction with the basic protocol.
The shorter induction phase required by the strategy developed in this study has advantages other than simply lower costs. It was reported that during fermentative production of extracellular recombinant proteins, the product was degraded increasingly after 48 h of induction and the rate of degradation increased towards 72 h (36). So, by using shorter induction times, the risk of degradation of the recombinant protein could be reduced and hence product yield may improve. Furthermore the longer the induction time, the higher the amount, and even possibly the variety, of the impurities produced. On the other hand, the control of the product-related impurities during the upstream processes by using a shorter induction phase, leads to an increase in the efficiency of purification processes, and/or reduction of purification steps required, to remove such impurities to an acceptable level in the downstream stage. It is worth noting that in this study heat production and oxygen consumption rates was reduced during the induction phase without affecting rhGH production. This leads to reduced production costs especially in large scale manufacturing processes.
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