## Results and Discussion
[46] \\ Wratislavia 1.81 \({}^{*}\) & 170.0 & 12.0 & - & 182.0 & 0.60 & Fed-batch reactor & [PERSON] et al. [46] \\ CCY-29-26-3 \({}^{k}\) & 23.0 & 2.6 & 2.3 & 27.9 & 0.40 & Batch flasks & [PERSON] et al. [29] \\ CCY-29-26-4 \({}^{k}\) & 26.7 & 1.0 & 2.2 & 29.9 & 0.40 & Batch flasks & [PERSON] et al. [29] \\ A-15 \({}^{k}\) & 71.0 & 8.0 & 1.8 & 80.8 & 0.50 & Batch reactor & [PERSON] et al. [29] \\ A UV1 \({}^{*}\) & 63.0 & 8.8 & 9.2 & 81.0 & 0.50 & Batch reactor & [PERSON] et al. [29] \\ Wratislavia Ki1 \({}^{*}\) & 80.0 & 2.6 & 0.3 & 82.9 & 0.51 & Batch reactor & [PERSON] et al. [29] \\ Wratislavia Ki1 \({}^{*}\) & 135.5 & 3.9 & 0.1 & 139.5 & 0.58 & Repeated-batch reactor & [PERSON]�  
especially concerning its physiological behavior. Moreover, for almost all of the reports indicated in Table 2, trials had been performed in pH values \(\approx\)3.0-3.5, whereas in the current investigation the pH value was \(\geq\)4.5, therefore, it is attainable to obtain higher _Pol_ quantities with the use of the LMBF Y-46 strain after further culture optimization, specifically as regards growth in lower pH values. Metabolic Characterization of Yarrowia lipolytica LMBF Y-46: Scale-Up in Laboratory-Scale bioreactor  
In the next step of this investigation, the bioprocess of glycerol fermentation by _Y. lipolytica_ LMBF Y-46 was scaled-up in a bench-top laboratory-scale bioreactor (active process volume = 2.0 L) which allowed fine pH control and dissolved oxygen measurement. Trials with \(Gly_{0}\) concentration adjusted to \(\approx\)100 g/L were performed ((NH4)\({}_{2}\)SO\({}_{4}\) at 2.0 g/L and yeast extract at 3.0 g/L were set into the medium). The choice of \(Gly_{0}\approx 100\) g/L was based on the results indicated in Table 1; precisely, in flask cultures with this \(Gly_{0}\) concentration, glycerol was almost completely consumed by the microorganism in a not excessively high incubation time (_c._ 180 h), while equally, DCW\({}_{\rm max}\) concentration was substantially high not being seriously influenced by the inhibition exerted due to high \(Gly_{0}\) concentrations into the medium (see Table 1). The obtained results in the equivalent trials between the shake-flask and the bioreactor culture are depicted in Table 3, while the evolution of DCW and glycerol in the two experiments is presented in Figure 3a,b. From the obtained results it can be indicated that drastically different kinetic and physiological profiles were recorded between the two experiments; in the bioreactor trial, much higher total biomass production occurred. This biomass value was obtained significantly more rapidly than the flask culture. On the other hand, the \(\mu_{\rm max}\) value between the shake-flask and the bioreactor trial (for the calculation see Section 2.2) was not substantially different between the two experiments (\(\mu_{\rm max}\approx 0.16\) h\({}^{-1}\) for both performed cultures). In contrast, the biomass production rate r\({}_{X}\) (= \(\frac{\Delta X}{\Delta t}\), in g/L/h; calculation performed when \(X\) obtained its maximum value), was drastically higher in the bioreactor experiment compared with the shake-flask one (_viz._ 0.506 vs. 0.08 g/L/h). Moreover, glycerol consumption was drastically higher in the bioreactor trial compared with the flask culture (see Table 3 and Figure 3b). As previously, fitting of the experimental data through linear regression of the remaining glycerol concentration \(f\) (fermentation time) demonstrated linear glycerol consumption rate r\({}_{\rm Gly}\) (although, \(r^{2}\) value was only 0.90 for the bioreactor experiment vs. 0.99 for the shake-flask trial; see Figure 3b) that was 0.52 g/L/h for the flask experiment and \(>\)3-fold time greater for the bioreactor culture (the r\({}_{\rm Gly}\) value for the latter case was = 1.85 g/L/h).