No abstract

Estrogen-dependent transcriptional activation by estrogen receptor (ER ) depends on the conformation of helices 3 and 12 in the ligand-binding domain. To better understand the function of helix 3 in ER , we examined the role of charged residues, which are conserved in most steroid receptors in helix 3, in estrogen-dependent transactivation. The replacement of Asp-351 with lysine (D351K) or leucine (D351 L) completely abolished estrogen-dependent transactivation without affecting estrogen-binding, DNA-binding and homodimerization activities in ER . The mutations dramatically reduced the ligand-dependent activation function 2 activity and impaired the ability of ER to bind p160 coactivators. In addition, the D351K mutant effectively inhibited the transcriptional activation activity of wild-type ER . Furthermore Asp-351 was required not only for the estrogen-dependent conformational change of wild-type ER but also for the constitutive transcriptional activity and ligand-independent active conformation of ER mutant Y537N. Similarly, in the orphan nuclear receptor called estrogen-related receptor 3 (ERR3), the replacement of Asp-273 (the corresponding amino acid to Asp-351 in ER ) with lysine abolished constitutive transcriptional activity of ERR3 without affecting DNA-binding activity and impaired the ability of the receptor to interact with p160 coactivators. These data suggest a role of Asp-351 in inducing and stabilizing the active conformation of ER , and our results experimentally confirm the concept that Asp-351 in helix 3 interacts with the amide hydrogen of L540 in helix 12 to form a transcriptionally competent surface for binding p160 coactivators.

We carried out the first simulation on multi-stage continuous high cell density culture (MSC-HCDC) to show that the MSC-HCDC can achieve batch/fed-batch product titer with much higher productivity to the fed-batch productivity using published fermentation kinetics of lactic acid, penicillin and ethanol. The system under consideration consists of n-serially connected continuous stirred-tank reactors (CSTRs) with either hollow fiber cell recycling or cell immobilization for high cell-density culture. In each CSTR substrate supply and product removal are possible. Penicillin production is severely limited by glucose metabolite repression that requires multi-CSTR glucose feeding. An 8-stage C-HCDC lactic acid fermentation resulted in 212.9 g/L of titer and 10.6 g/L/h of productivity, corresponding to 101 and 429% of the comparable lactic acid fed-batch, respectively. The penicillin production model predicted 149% (0.085 g/L/h) of productivity in 8-stage C-HCDC with 40 g/L of cell density and 289% of productivity (0.165 g/L/h) in 7-stage C-HCDC with 60 g/L of cell density compared with referring batch cultivations. A 2-stage C-HCDC ethanol experimental run showed 107% titer and 257% productivity of the batch system having 88.8 g/L of titer and 3.7 g/L/h of productivity. MSC-HCDC can give much higher productivity than batch/fed-batch system, and yield a several percentage higher titer as well. The productivity ratio of MSC-HCDC over batch/fed-batch system is given as a multiplication of system dilution rate of MSC-HCDC and cycle time of batch/fed-batch system. We suggest MSC-HCDC as a new production platform for various fermentation products including monoclonal antibody.

Perfusion cultures of recombinant Chinese hamster ovary cells, producing recombinant antibody against the S surface antigen of Hepatitis B virus, were carried out in continuous and intermittent mode using a Centritech Lab II Centrifuge. In the continuous perfusion process, despite the absence of shear stress from the pump head, long-term operation was not possible because of continuously repeated exposure to oxygen limitation and low temperature, as well as shear stress from centrifugal force. In the intermittent perfusion processes, the frequency of cell-passage through the centrifuge was substantially reduced, compared with the continuous perfusion mode; however, the degree of reduction could not guarantee stable long-term operation. Although various operating parameters were applied in the intermittent perfusion cultures, high cell densities could not be maintained stably. In a single bioreactor culture system, a specific cell that is returned from the centrifuge to the bioreactor could be transferred from the bioreactor to the centrifuge again in the next cycle. These repetitive damages, caused by shear stress from the pump head and centrifugal force, as well as exposure to suboptimal conditions such as oxygen limitation and low temperature below 37°C, were more serious at higher perfusion rates. Subsequently, damaged cells and dead cells were continuously accumulated in the bioreactor. Culture temperature shift from 37 to 33°C increased antibody concentrations but showed inhibitory effects on cell growth. The negative effects of lowering culture temperature on cell growth overwhelmed the positive effects on antibody production. To protect cells from shear stress, Pluronic F-68 was 2-fold concentrated in the culture medium; nevertheless, a significantly higher concentration of Pluronic F-68 (2 g/L) may have inhibitory effects on cell growth.