Akademik Veri Yönetim Sistemi
Tezin Türü: Yüksek Lisans
Tezin Yürütüldüğü Kurum: Orta Doğu Teknik Üniversitesi, Türkiye
Tezin Onay Tarihi: 2013
Tezin Dili: İngilizce
Öğrenci: Şükran Melda Eskitoros
Danışman: PINAR ÇALIK
Özet:In this study, it was aimed to investigate the effects of different co-carbon sources on therapeutically important glycoprotein, recombinant human erythropoietin (rHuEPO) production by Pichia pastoris by designing feeding strategies which were applied in the production phase of the bioprocess. During the experiments, the cell growth, sorbitol, mannitol, and methanol consumptions, recombinant human EPO production, alcohol oxidase activity, total protease concentrations and the by-products organic acid concentrations were analyzed. In this context, firstly, laboratory scale air filtered shake bioreactor experiments were performed by P. pastoris Mut+ strain to investigate the effects of mannitol and sorbitol. 50 gL-1 initial concentration of co-substrates was found more affordable and appropriate for cell concentration and recombinant protein production. Thereafter, six pilot scale bioreactor operations were designed and performed. In the first designed strategy (named as SSM strategy), batch-wise 50 g L-1 sorbitol was fed at t=0 h of the production phase and then sorbitol concentration was kept constant at 50 g L-1 by fed-batch feeding with a pre-determined specific growth rate of μSrb0=0.025 h-1 within t=0-15 h of the production phase together with fed-batch methanol feeding with a pre-determined specific growth rate of μM0=0.03 h-1. In the following bioreactor experiments co-substrate mannitol was fed to the system with different feeding strategies together with fed-batch methanol feeding with a pre-determined specific growth rate of μM0=0.03 h-1. In the second strategy (MM), only 40 g L-1 mannitol was added to the system at t=0 h of the production phase. In the third strategy (MMM), after adding 50 g L-1 mannitol at t=0 h, mannitol concentration was kept constant at 50 g L-1 by fed-batch feeding with a pre-determined specific growth rate of μMan0=0.11 h-1 within t=0-9 h of the production phase when the same cell concentration was attained in SSM strategy. In the fourth one (MLM), limiting amount of mannitol, 3 g L-1, was added at t=0 h and then mannitol concentration was kept constant at 3 g L-1 by fed-batch feeding with a pre-determined specific growth rate of μMan0=0.005 h-1 within t=0-10 h of the production phase. After these strategies, several pulses, batch-wise, mannitol feeding strategies were performed. In the fifth strategy (MPM), besides 50 g L-1 initial mannitol feeding at t=0 h, adding second batch-wise mannitol at t=6 h, and third one at t=12 h were applied. In the last strategy (MPMG), four 50 g L-1 pulse feeding of mannitol were performed at t=0 h, 7 h, 14 h, and 24 h, containing glycerol, with an initial concentration in the fermentation medium being 8 g L-1. The highest extracellular rHuEPO production was achieved in the fifth strategy MPM as CrHuEPO=645 mg L-1 at t=9 h while the highest cell concentration was achieved in the first strategy SSM as Cx=109 gL-1 at t=48 h. The overall cell and product yields on total substrate were calculated as YX/St=0.22 g g-1 and YP/St=2.23 mg g-1 in the highest rHuEPO production case.