Serum-free suspension cultivation of PER.C6(R) cells and recombinant adenovirus production under different pH conditions

PER.C6(R) cell growth, metabolism, and adenovirus production were studied in head-to-head comparisons in stirred bioreactors under different pH conditions. Cell growth rate was found to be similar in the pH range of 7.1-7.6, while a long lag phase and a slower growth rate were observed at pH 6.8. The specific consumption rates of glucose and glutamine decreased rapidly over time during batch cell growth, as did the specific lactate and ammonium production rates. Cell metabolism in both infected and uninfected cultures was very sensitive to culture pH, resulting in dramatic differences in glucose/glutamine consumption and lactate/ammonium production under different pH conditions. It appeared that glucose metabolism was suppressed at low pH but the efficiency of energy production from glucose was enhanced. Adenovirus infection resulted in profound changes in cell growth and metabolism. Cell growth was largely arrested under all pH conditions, while glucose consumption and lactate production were elevated post virus infection. Virus infection induced a reduction in glutamine consumption at low pH but an increase at high pH. The optimal pH for adenovirus production was found to be 7.3 under the experimental conditions used in the study. Deviations from this optimum resulted in significant reductions of virus productivity. The results indicate that culture pH is a very critical process parameter in PER.C6(R) cell culture and adenovirus production.     

Enhancement of a two-phase partitioning bioreactor system by modification of the microbial catalyst: demonstration of concept

Application of two-phase partitioning bioreactors (TPPB) to the degradation of phenol and xenobiotics has been limited by the fact that many organic compounds that would otherwise be desirable delivery solvents can be utilized by the microorganisms employed. The ability to metabolize the solvent itself could interfere with xenobiotic degradation, limiting remediation efficiency, and hence represents a microbial characteristic incompatible with process goals. To avoid the issue of bioavailability, previous TPPB applications have relied on complex and often expensive delivery solvents or suboptimal catalyst-solvent pairings. In an effort to enhance TPPB activity and applicability, a genetically engineered derivative of Pseudomonas putida ATCC 11172 mutated in its ability to utilize medium-chain-length alcohols was generated (AVP2) and applied as the catalyst within a TPPB system with decanol as the delivery solvent. Kinetic analysis verified that the genetic alteration had not negatively affected phenol degradation. The volumetric productivity of AVP2 (0.48 g/L x h(-1)) was equivalent to that seen for wild-type ATCC 11172 (0.51 g/L x h(-1)), but a comparison of initial cell concentrations and yields revealed an improved phenol-degrading efficiency for the mutant under process conditions. Yield coefficients, cell dry weight, and viable count determinations all confirmed the stability of the modified phenotype. This work illustrates the possibilities for TPPB process enhancement through a careful combination of genetic modification and solvent selection.     

Protein NMR structure determination with automated NOE-identification in the NOESY spectra using the new software ATNOS

Novel algorithms are presented for automated NOESY peak picking and NOE signal identification in homonuclear 2D and heteronuclear-resolved 3D [¹H,¹H]-NOESY spectra during de novoprotein structure determination by NMR, which have been implemented in the new software ATNOS (automated NOESY peak picking). The input for ATNOS consists of the amino acid sequence of the protein, chemical shift lists from the sequence-specific resonance assignment, and one or several 2D or 3D NOESY spectra. In the present implementation, ATNOS performs multiple cycles of NOE peak identification in concert with automated NOE assignment with the software CANDID and protein structure calculation with the program DYANA. In the second and subsequent cycles, the intermediate protein structures are used as an additional guide for the interpretation of the NOESY spectra. By incorporating the analysis of the raw NMR data into the process of automated de novoprotein NMR structure determination, ATNOS enables direct feedback between the protein structure, the NOE assignments and the experimental NOESY spectra. The main elements of the algorithms for NOESY spectral analysis are techniques for local baseline correction and evaluation of local noise level amplitudes, automated determination of spectrum-specific threshold parameters, the use of symmetry relations, and the inclusion of the chemical shift information and the intermediate protein structures in the process of distinguishing between NOE peaks and artifacts. The ATNOS procedure has been validated with experimental NMR data sets of three proteins, for which high-quality NMR structures had previously been obtained by interactive interpretation of the NOESY spectra. The ATNOS-based structures coincide closely with those obtained with interactive peak picking. Overall, we present the algorithms used in this paper as a further important step towards objective and efficient de novoprotein structure determination by NMR.     

Solution structure and dynamics of melanoma inhibitory activity protein

Melanoma inhibitory activity (MIA) is a small secreted protein that is implicated in cartilage cell maintenance and melanoma metastasis. It is representative of a recently discovered family of proteins that contain a Src Homologous 3 (SH3) subdomain. While SH3 domains are normally found in intracellular proteins and mediate protein-protein interactions via recognition of polyproline helices, MIA is single-domain extracellular protein, and it probably binds to a different class of ligands.Here we report the assignments, solution structure, and dynamics of human MIA determined by heteronuclear NMR methods. The structures were calculated in a semi-automated manner without manual assignment of NOE crosspeaks, and have a backbone rmsd of 0.38 Å over the ordered regions of the protein. The structure consists of an SH3-like subdomain with N- and C-terminal extensions of approximately 20 amino acids each that together form a novel fold. The rmsd between the solution structure and our recently reported crystal structure is 0.86 Å over the ordered regions of the backbone, and the main differences are localized to the most dynamic regions of the protein. The similarity between the NMR and crystal structures supports the use of automated NOE assignments and ambiguous restraints to accelerate the calculation of NMR structures.     

Influence of the completeness of chemical shift assignments on NMR structures obtained with automated NOE assignment

Reliable automated NOE assignment and structure calculation on the basis of a largely complete, assigned input chemical shift list and a list of unassigned NOESY cross peaks has recently become feasible for routine NMR protein structure calculation and has been shown to yield results that are equivalent to those of the conventional, manual approach. However, these algorithms rely on the availability of a virtually complete list of the chemical shifts. This paper investigates the influence of incomplete chemical shift assignments on the reliability of NMR structures obtained with automated NOESY cross peak assignment. The program CYANA was used for combined automated NOESY assignment with the CANDID algorithm and structure calculations with torsion angle dynamics at various degrees of completeness of the chemical shift assignment which was simulated by random omission of entries in the experimental ¹H chemical shift lists that had been used for the earlier, conventional structure determinations of two proteins. Sets of structure calculations were performed choosing the omitted chemical shifts randomly among all assigned hydrogen atoms, or among aromatic hydrogen atoms. For comparison, automated NOESY assignment and structure calculations were performed with the complete experimental chemical shift but under random omission of NOESY cross peaks. When heteronuclear-resolved three-dimensional NOESY spectra are available the current CANDID algorithm yields in the absence of up to about 10% of the experimental ¹H chemical shifts reliable NOE assignments and three-dimensional structures that deviate by less than 2 Å from the reference structure obtained using all experimental chemical shift assignments. In contrast, the algorithm can accommodate the omission of up to 50% of the cross peaks in heteronuclear- resolved NOESY spectra without producing structures with a RMSD of more than 2 Å to the reference structure. When only homonuclear NOESY spectra are available, the algorithm is slightly more susceptible to missing data and can tolerate the absence of up to about 7% of the experimental ¹H chemical shifts or of up to 30% of the NOESY peaks.Abbreviations: BmPBP^A – Bombyx mori pheromone binding protein form A; CYANA – combined assignment and dynamics algorithm for NMR applications; NMR – nuclear magnetic resonance; NOE – nuclear Overhauser effect; NOESY – NOE spectroscopy; RMSD – root-mean-square deviation; WmKT – Williopsis mrakii killer toxin     

Automated multi-dimensional purification of tagged proteins

The capacity for high throughput purification (HTP) is essential in fields such as structural genomics where large numbers of protein samples are routinely characterized in, for example, studies of structural determination, functionality and drug development. Proteins required for such analysis must be pure and homogenous and available in relatively large amounts. ÄKTAT 3D system is a powerful automated protein purification system, which minimizes preparation, run-time and repetitive manual tasks. It has the capacity to purify up to 6 different His₆- or GST-tagged proteins per day and can produce 1–50 mg protein per run at >90% purity. The success of automated protein purification increases with careful experimental planning. Protocol, columns and buffers need to be chosen with the final application area for the purified protein in mind.     

Xylitol production from high xylose concentration: evaluation of the fermentation in bioreactor under different stirring rates

AIMS: To investigate the production of xylitol by the yeast Candida guilliermondii FTI 20037, in a bioreactor, from rice straw hemicellulosic hydrolysate with a high xylose concentration. METHODS AND RESULTS: Batch fermentation was carried out with rice straw hemicellulosic hydrolysate containing about 85 g xylose l(-1), in a stirred-tank bioreactor at 30 degrees C, under aeration of 1.3 vvm (volume of air per volume of medium per min) and different stirring rates (200, 300 and 500 rev min(-1)). The bioconversion of xylose into xylitol by the yeast depended on the stirring rate, the maximum xylitol yield (YP/S = 0.84 g g(-1)) being achieved at 300 rev min-1, with no need to pretreat the hydrolysate for purification. CONCLUSIONS: To determine the most adequate oxygen transfer rate is fundamental to improving the xylose-to-xylitol bioconversion by C. guilliermondii. SIGNIFICANCE AND IMPACT OF THE STUDY: For the microbial production of xylitol to be economically viable, the initial concentration of xylose in the lignocellulosic hydrolysate should be as high as possible, as with high substrate concentrations it is possible to increase the final product concentration. Nevertheless, there are few reports on the use of high xylose concentrations. Considering a process in bioreactor, from rice straw hemicellulosic hydrolysate, this is an innovator work.     

Replacement of immobilised cell bioreactors by smaller immobilised enzyme bioreactors: unique-outcome predictability for cytochromes P450 isoforms?

Both immobilized enzymes (IME) and immobilized cells (IMC) are acceptable as the biocatalysts essential for the attainment of rapid rates of bioconversion in bioreactors. IMC can display higher than expected cellular permeability whilst IME can exhibit high catalytic constant (k_cat/K_m) despite limitations on substrate utilisation due to an unstired diffusion layer of solvent. Scale-down switching from IMC to IME involves the replacement of high-volume biotechnology by low-volume biotechnology, sometimes using IME mimics in partially non-aqueous solvent systems. Highly purified IME systems covalently immobilised to particles of, for instance, microcrystalline cellulose or porous glass, can retain both the hydrophilic and hydrophobic intermediate products in situ of the chosen sequence of enzyme reactions. These bioconversions, therefore, are as efficient as those with IMC where enzymes are often particle- or membrane-bound so that even hydrophilic intermediates are not released rapidly into solution. This mimicry of in vivo biosynthetic pathways that are compartmentalised in vivo (e.g. of lysosomes, mitochondria and endoplasmic reticulum) can replace larger IMC by IME especially in application of up to 2700 cytochromes P450 isoforms in bioprocessing. In silico investigation of appropriate model IME systems, in comparison with IMC systems, will be needed to define the optimal bioreactor configuration and parameters of operation, such as pH, T and oxygen mass transfer rate (OTR). The application solely of hazop (applied hazard and operability concepts) may, nevertheless, not be recommended to replace fully the in silico and real-lab pilot-scale and scale studies. Here, food-safe bioprocessing has to be achieved without incorporation of recognised biohazards; especially in the form of unacceptable levels of toxic metals that promote a risk-analysis uncertainty.     

Biooxidation of ferrous iron by immobilized Acidithiobacillus ferrooxidans in poly(vinyl alcohol) cryogel carriers

PVA-cryogels entrapping about 10⁹ cells of Acidithiobacillus ferrooxidans per ml of gel were prepared by freezing-thawing procedure, and the biooxidation of Fe²⁺ by immobilized cells was investigated in a 0.365 l packed-bed bioreactor. Fe²⁺ oxidation fits a plug-flow reaction model well. A maximum oxidation rate of 3.1 g Fe²⁺ l^–1 h^–1 was achieved at the dilution rate of 0.4 h^–1 or higher, while no obvious precipitate was determined at this time. In addition, cell-immobilized PVA-cryogels packed in bioreactor maintained their oxidative ability for more than two months under non-sterile conditions. Nomenclature: C _A0 – Concentration of Fe²⁺ in feed stream (g l^–1) C _A – Concentration of Fe^{2 +} in outlet stream (g l^{– 1}) D – Dilution rate of the packed-bed bioreactor (h^–1) F – Volumetric flow rate of iron solution (l h^–1) F _A0 – Mass flow rate of Fe²⁺ in the feed stream (g h^–1) K – Kinetic constant (l l^–1 h^–1) r _A – Oxidation rate of Fe²⁺ (g l^–1 h^–1) V – Volume of packed-bed bioreactor (l) X _A – Conversion ratio of Fe²⁺ (%)     

Removal and destruction of high concentrations of gaseous toluene in a two-phase partitioning bioreactor by Alcaligenes xylosoxidans

A two-phase bioreactor consisting of hexadecane dispersed in an aqueous, cell-containing medium (organic fraction = 0.33) was used to trap toluene vapours from an air stream. The affinity for toluene by the solvent resulted in high efficiency of removal and transfer to the aqueous phase based on equilibrium transfer. The system was readily able to handle a loading capacity of 748 mg l^–1 h^–1 at a toluene degradation efficiency of greater than 98%.