Enhanced production of total flavones from Inonotus baumii by multiple strategies

As one kind of important secondary metabolites produced by Inonotus baumii, flavones can be applied in food, medicine, and other industries due to their biological activities such as antioxidant, anticancer, and antibacterial activity. To enhance total flavone production in submerged fermentation of I. baumii, three different strategies, optimization of fermentation parameters by statistical designs including Plackett–Burman design and response surface methodology, addition of precursors and elicitors, and two-phase culture, were used. The production of total flavones (PTF) reached 1532.83?mg/L when the optimized medium was used. All precursors and elicitors can increase the PTF. The maximum PTF (2184.06?mg/L, up to 1.57-fold) was obtained with the addition of both AgNO₃ and glutathione in fermentation media. Interestingly, when 0.5% (w/v) DM130 macroporous resin as adsorbent was added to fermentation broth on day 4 of culture, the highest production reached 2407.79?mg/L with this two-phase culture strategy. These methods can be further applied to large-scale industrial production and broaden the application of flavones.     

IN SITU SEPARATION OF ETHANOL WITH AQUEOUS TWO-PHASE SYSTEM AND ASSESSMENT OF KLa FOR YEAST GROWTH IN BATCH CULTIVATION

In the fermentation process, the separation of product and its purification is the most difficult and exigent task in the ground of biochemical engineering. Another major problem that is encountered in the fermentation is product inhibition, which leads to low conversion and low productivities. Extractive fermentation is a technique that helps in the in situ removal of product and better performance of the fermentation. An aqueous two-phase system was employed for in situ ethanol separation since the technique was biofriendly to the Saccharomyces cerevisiae and the ethanol produced. The two-phase system was obtained with polyethylene glycol 4000 (PEG 4000) and ammonium sulfate in water above critical concentrations, with the desire that the ethanol moves to the top phase while cells rest at the bottom. The overall mass transfer coefficient (K_La) was also estimated for the yeast growth at different rpm. The concentration and yield of ethanol were determined for conventional fermentation to be around 81.3% and for extractive fermentation around 87.5% at the end of the fermentation. Based on observation of both processes, extractive fermentation was found to be the best.     

Recovery of endo-polygalacturonase using polyethylene glycol-salt aqueous two-phase extraction with polymer recycling

The partitioning behaviour of endo-polygalacturonase (endo-PG) and total protein from a clarified Kluyveromyces marxianus fermentation broth in polyethylene glycol (PEG)-ammonium sulfate and PEG-potassium phosphate (pH=7) aqueous two-phase systems was experimentally investigated. Both the enzyme and total protein partitioned in the bottom phase for these two kinds of systems. The enzyme partitioning coefficient can be lower than 0.01 in PEG8000-(NH₄)₂SO₄ ATPS with a large phase volume ratio and a moderate tie-line length, which implies the possibility of concentration operation using aqueous two phase partitioning. An ion-exchange separation of high purification efficiency was applied to analyze the clarified and dialyzed fermentation broth. A total purification factor of only 2.3 was obtained, which indicated the high enzyme protein content in the total protein of the fermentation broth. Consequently, the main purpose for separating endo-PG is concentration rather than purification. A separation scheme using an aqueous two-phase extraction process with polymer recycling and a dialysis was proposed to recover endo-PG from the fermentation supernatant of K. marxianus for commercial purpose. A high enzyme recovery up to 95% and a concentration factor of 5 to 8 with a purification factor of about 1.25 were obtained using the single aqueous two-phase extraction process. More than 95% polymer recycled will not affect the enzyme recovery and purification factor. Dialysis was used mainly to remove salts in the bottom phase. The dialysis step has no enzyme loss and can further remove small bulk proteins. The total purification factor for the scheme is about 1.7.     

Protein body-inducing fusions for high-level production and purification of recombinant proteins in plants

For the past two decades, therapeutic and industrially important proteins have been expressed in plants with varying levels of success. The two major challenges hindering the economical production of plant-made recombinant proteins include inadequate accumulation levels and the lack of efficient purification methods. To address these limitations, several fusion protein strategies have been recently developed to significantly enhance the production yield of plant-made recombinant proteins, while simultaneously assisting in their subsequent purification. Elastin-like polypeptides are thermally responsive biopolymers composed of a repeating pentapeptide 'VPGXG' sequence that are valuable for the purification of recombinant proteins. Hydrophobins are small fungal proteins capable of altering the hydrophobicity of their respective fusion partner, thus enabling efficient purification by surfactant-based aqueous two-phase systems. Zera, a domain of the maize seed storage protein γ-zein, can induce the formation of protein storage bodies, thus facilitating the recovery of fused proteins using density-based separation methods. These three novel protein fusion systems have also been shown to enhance the accumulation of a range of different recombinant proteins, while concurrently inducing the formation of protein bodies. The packing of these fusion proteins into protein bodies may exclude the recombinant protein from normal physiological turnover. Furthermore, these systems allow for quick, simple and inexpensive nonchromatographic purification of the recombinant protein, which can be scaled up to industrial levels of protein production. This review will focus on the similarities and differences of these artificial storage organelles, their biogenesis and their implication for the production of recombinant proteins in plants and their subsequent purification.     

An automated small-scale protein expression and purification screening provides beneficial information for protein production

One of the first key steps in structural genomics is high-throughput expression and rapid screening to select highly soluble proteins, the preferred candidates for crystal production. Here we describe the methodology used at the Berkeley Structural Genomics Center (BSGC) for automated parallel expression and small-scale purification of fusion proteins using a 96-well format. Our robotic method includes cell lysis, soluble fraction separation and purification with affinity resins. For detection of His-tagged proteins in the soluble fractions and after affinity resin elution, a dot-blot procedure with an anti-His-antibody is used. The expression level and molecular mass of recombinant proteins are checked by SDS-PAGE. With this approach, we are able to obtain beneficial information to be used for large-scale protein expression and purification.     

Solid-state fermentation for Trichokonins production from Trichoderma koningii SMF2 and preparative purification of Trichokonin VI by a simple protocol

Trichokonins are peptaibols produced by Trichoderma koningii SMF2. The main isoforms are Trichokonin VI, Trichokonin VII and Trichokonin VIII. The solid-state fermentation (SSF) was applied for the production of Trichokonin VI. The fermentation factors, which included inoculum size, incubation temperature, initial moisture content and initial pH, were investigated and optimized by response surface methodology. The maximum Trichokonin VI production (4.07mg/g dry substrate) was achieved by employing inoculum size of 18%, incubation temperature at 24.3 degrees C, initial moisture content of 77.5% and initial pH at 5.0. Furthermore, gel filtration and preparative HPLC were used for separation of Trichokonin VI from a crude extract of the T. koningii SMF2 culture. With this preparative purification protocol under optimized fermentation conditions, 146.20mg Trichokonin VI was obtained from 1kg solid cultures. It has been shown that the obtained Trichokonin VI is more than 95% in purity. This is the first report on optimization of peptaibols production in SSF with high content. An efficient method for the preparative purification of Trichokonin VI is also proposed.     

Pilot-and production-scale containment of cytotoxic and oncogenic fermentation processes

Proper design of fermentation facilities and equipment modification can control the risks associated with largescale production and purification of microbially produced cytotoxic agents and oncogenic viruses. The primary biohazard risks to operators and the environment are generation of aerosols and accidental spills. Fermentation and recovery facilities can be constructed to contain these agents by installing fermentation equipment within a HEPA-filter-exhausted biological barrier. Within this barrier system, large-scale processing that generates potentially hazaradous areosols (filtration, centrifugation of transformed cells or crystal slurries, and banding of viruses) should be isolated from other operations. Isolation of equipment is often required, with provision for both chemical and biological decontamination of process wastes. Failsafe fermentor over-pressure sensors, parallel exhaust gas filtration, welded transfer lines, and modified sampling systems for elimination of aerosols can be installed on most fermentation equipment. Aerosol and spill containment by proper equipment design, coupled with appropriate personnel protective equipment and medical monitoring, make possible safe production of experimental growth factors and viruses from large-scale culture of transformed mammalian cells and production of cytotoxic antitumor antibiotics.     

重组质粒pVAX1-PENK大规模制备研究

目的：建立质粒pVAX1-PENK的大规模制备2--艺。方法：对大肠杆菌工程菌DH5α-pVAX1-PENK进行补料发酵,利用自行发明的连续碱裂解过程对菌体进行裂解,经超滤浓缩后,用Sepharnse 6 Fast Flow层析柱分离DNA与RNA,再经Plasmidselect Xtra层析柱分离超螺旋质粒DNA与开环或线性质粒DNA,最后经Source 15Q层析柱精制质粒DNA。结果：发酵获得质粒pVAX1-PENK的产率为182mg／L,经碱裂解及层析分离后,最终制备的质粒DNA超螺旋比例大于98％,总回收率为60.5％,纯度（D260nm／D280nm）为1.8～2.0。结论：建立的质粒DNA生产工艺可以制备大量高纯度的质粒DNA,并避免了使用动物源性的酶及有毒试剂。     

Extraction of protease from Aspergillus tamarii URM 4634 in aqueous two-phase system under continuous and discontinuous process

Abstract

Aqueous two-phase systems have been studied for almost a century to separate biomolecules in harmless conditions. Proteases produced by Aspergillus tamarii URM 4634 were extracted in polyethylene glycol (PEG)/phosphate aqueous two-phase system under discontinuous and continuous (perforated rotative discs column) process. On the discontinuous process, it was evaluated the effect of operational conditions (PEG molar mass and its concentration, phosphate concentration and pH) over the partition coefficient, activity yield and purification factor. Protease partitioned to PEG-phase with partition coefficients up to 55.73. The best process parameters were 17.5% of PEG, with molar mass 8000?g·mol^?1, 15% of phosphate salt at pH 6, with 113.15% of activity yield and purification factor of 2.62. Under continuous extraction, hold up data showed that 57.1% of the discontinuous phase was available for protein extraction. Further, separation achieved 90.0% of efficiency. The yields surpassed 100% in almost all runs, and the best purification factor was 1.84, with both flows of 2?mL·min^?1. Thus, the best operational conditions reached an activity yield of 95.3% and 90.0% of separation efficiency. Hence, aqueous two-phase system PEG/phosphate extraction is an efficient process for separation of proteases produced by Aspergillus tamarii URM 4634, under continuous extraction likewise under discontinuous process.     

Evaluation of different primary recovery methods for E. coli-derived recombinant human growth hormone and compatibility with further down-stream purification

Due to advances in fermentation technology, it is now possible to obtain fermentation broth with over 30% solids. The high solid content makes the clarification step difficult, especially at large scale. The primary protein recovery step is challenging due to the heterogeneous solution of soluble and insoluble material. In this study, we compare different primary recovery routes and the compatibility with the initial capture chromatography step. The primary recovery routes studied are standard clarification by centrifugation and extraction in aqueous two-phase systems. The compatibility of the feed streams from the different primary recovery steps with the first chromatography step is addressed. An anion-exchange column was used as the first capture column in the purification process. The aqueous two-phase system was composed of a random copolymer of ethylene oxide and propylene oxide (EOPO) in combination with a waxy starch. The target protein in this study was human growth hormone (hGH) produced in recombinant Escherichia coli. The purity of hGH in the top phase after aqueous two-phase extraction was found to be significantly higher than in clarified homogenate supernatant and increased as the EOPO polymer concentration in the aqueous two-phase system increased. Stability of the supernatant and EOPO top phases and hGH were determined by turbidity measurements and LC-MS assay. All of the feed-streams from the primary recovery steps were compatible with the anion-exchange chromatography step; however, the capacity of the resin was strongly dependent on the purity of the load. Different process aspects, e.g., resin capacity, viscosity, purification, and yield of hGH and scalability are compared.     

Fermentation process development for the production of medium-chain-length poly-3-hyroxyalkanoates

This paper presents a review of the existing fermentation processes for the production of medium-chain-length poly-3-hydroxyalkanoates (MCL-PHAs). These biodegradable polymers are usually produced most efficiently from structurally related carbon sources such as alkanes and alkanoic acids. Unlike alkanoic acids, alkanes exhibit little toxicity but their low aqueous solubility limits their use in high density culture. Alkanoic acids pose little mass transfer difficulty, but their toxicity requires that their concentration be well controlled. Using presently available technology, large-scale production of MCL-PHA from octane has been reported to cost from US $5 to 10 per kilogram, with expenditures almost evenly divided between carbon source, fermentation process, and the separation process. However, MCL-PHAs, even some with functional groups in their subunits, can also be produced from cheaper unrelated carbon sources, such as glucose. Metabolic engineering and other approaches should also allow increased PHA cellular content to be achieved. These approaches, as well as a better understanding of fermentation kinetics, will likely result in increased productivity and lower production costs.     

Aqueous two-phase systems

Biphasic systems formed by mixing of two polymers or a polymer and a salt in water can be used for separation of cells, membranes, viruses, proteins, nucleic acids, and other biomolecules. The partitioning between the two phases is dependent on the surface properties and conformation of the materials, and also on the composition of the two-phase system. The mechanism of partitioning is, however, complex and not easily predicted. Aqueous two-phase systems (ATPS) have proven to be a useful tool for analysis of biomolecular and cellular surfaces and their interactions, fractionation of cell populations, product recovery in biotechnology, and so forth. Potential for environmental remediation has also been suggested. Because ATPS are easily scalable and are also able to hold high biomass load in comparison with other separation techniques, the application that has attracted most interest so far has been the large-scale recovery of proteins from crude feedstocks. As chemicals constitute the major cost factor for large-scale systems, use of easily recyclable phase components and the phase systems generated by a single-phase chemical in water are being studied.     

Large scale protein separations: engineering aspects of chromatography

The engineering considerations common to large scale chromatographic purification of proteins are reviewed. A discussion of the industrial chromatography fundamentals is followed by aspects which affect the scale of separation. The separation column geometry, the effect of the main operational parameters on separation performance, and the physical characteristics of column packing are treated. Throughout, the emphasis is on ion exchange and size exclusion techniques which together constitute the major portion of commercial chromatographic protein purifications. In all cases, the state of current technology is examined and areas in need of further development are noted.

The physico-chemical advances now underway in chromatographic separation of biopolymers would ensure a substantially enhanced role for these techniques in industrial production of products of new biotechnology.     

Recombinant aprotinin produced in transgenic corn seed: extraction and purification studies

Expression in transgenic plants is potentially one of the most economical systems for large-scale production of valuable peptide and protein products. However, the downstream processing of recombinant proteins produced in plants has not been extensively studied. In this work, we studied the extraction and purification of recombinant aprotinin, a protease inhibitor used as a therapeutic compound, produced in transgenic corn seed. Conditions for extraction from transgenic corn meal that maximize aprotinin concentration and its fraction of the total soluble protein in the extract were found: pH 3.0 and 200 mM NaCl. Aprotinin, together with a native corn trypsin inhibitor (CTI), was captured using a tryspin-agarose column. These two inhibitors were separated using an agarose-IDA-Cu2+ column that proved to efficiently absorb the CTI while the recombinant aprotinin was collected in the flowthrough with purity of at least 79%. The high purity of the recombinant aprotinin was verified by SDS-PAGE and N-terminal sequencing. The overall recombinant aprotinin recovery yield and purification factor were 49% and 280, respectively. Because CTI was also purified, the recovery and purification process studied has the advantage of possible CTI co-production. Finally, the work presented here introduces additional information on the recovery and purification of recombinant proteins produced in plants and corroborates with past research on the potential use of plants as biorreactors.     

An efficient strategy for high-throughput expression screening of recombinant integral membrane proteins

The recombinant expression of integral membrane proteins is considered a major challenge, and together with the crystallization step, the major hurdle toward routine structure determination of membrane proteins. Basic methodologies for high-throughput (HTP) expression optimization of soluble proteins have recently emerged, providing statistically significant success rates for producing such proteins. Experimental procedures for handling integral membrane proteins are generally more challenging, and there have been no previous comprehensive reports of HTP technology for membrane protein production. Here, we present a generic and integrated parallel HTP strategy for cloning and expression screening of membrane proteins in their detergent solubilized form. Based on this strategy, we provide overall success rates for membrane protein production in Escherichia coli, as well as initial benchmarking statistics of parameters such as expression vectors, strains, and solubilizing detergents. The technologies were applied to 49 E. coli integral membrane proteins with human homologs and revealed that 71% of these proteins could be produced at sufficient levels to allow milligram amounts of protein to be relatively easily purified, which is a significantly higher success rate than anticipated. We attribute the high success rate to the quality and robustness of the methodology used, and to introducing multiple parameters such as different vectors, strains, and detergents. The presented strategy demonstrates the usefulness of HTP technologies for membrane protein production, and the feasibility of large-scale programs for elucidation of structure and function of bacterial integral membrane proteins.     

Efficient purification of recombinant proteins using hydrophobins as tags in surfactant-based two-phase systems

In this work we describe the new concept of using fungal hydrophobins as efficient tags for purification of recombinant fusion proteins by aqueous two-phase separation. Hydrophobins are a group of small surface-active proteins produced by filamentous fungi. Some characteristics of hydrophobins are that they are relatively small (approximately 100 amino acids), they contain eight disulfide-forming Cys residues in a conserved pattern, and they self-assemble on interfaces. The aqueous two-phase systems studied were based on nonionic surfactants that phase-separate at certain temperatures. We show that the use of hydrophobins as tags has many advantages such as high selectivity and good yield and is technically very simple to perform. Fusion proteins with target proteins of different molecular size were compared to the corresponding free proteins using a set of different surfactants. This gave an understanding on which factors influence the separation and what rationale should be used for optimization. This unusually strong and specific interaction between polymeric surfactants and a soluble protein shows promise for new developments in interfacing proteins and nonbiological materials for other applications as well.     

Isolation of proteins by gel filtration in 6M guanidinium chloride: application to RNA tumor viruses

Separation of RNA tumor virus proteins by gel filtration in 6m guanidinium chloride indicates that this method will effectively separate polypeptides in milligram amounts whose molecular weights differ by as little as 15 percent. Such separations are achieved because proteins in 6m guanidinium chloride have a random coil conformation with diffusion coefficients considerably smaller than the corresponding native proteins. Consequently, protein bands that emerge from a gel filtration column in 6m guanidinium chloride are remarkably sharp. A 60–70% yield of renatured RNA tumor virus proteins could be obtained following dialysis against a dilute solution of mercaptoethanol. The major proteins of avian RNA tumor viruses were obtained as pure components by gel filtration in 6m guanidinium chloride. Mammalian RNA tumor viruses appear to have a more complex protein structure, since, in some cases, additional purification was required to obtain the pure proteins. This method of protein separation might be used as the initial stop in the isolation of components from other biological macrostructures.     

Large-scale separation and production of engineered proteins,designed for facilitated recovery in detergent-based aqueous two-phase extraction systems

The feasibility and scalability of extraction in detergent-based aqueous two-phase systems for the separation of proteins from culture broth is demonstrated. At the same time the large-scale production of a fusion protein and the influence of cultivation scale on the efficiency of separation were investigated. An amphiphilic fusion protein EGIcore-HFBI was chosen, consisting of the catalytic core of the cellulase endoglucanase I and the small protein hydrophobin I, expressed homologously in Trichoderma reesei. Using the technical nonionic detergent Agrimul NRE 1205 the separation was successfully scaled up to 1200 l. No differences in yield or in partition coefficient were observed at 10 ml and 1200 l scale. Changes in the fermentation temperature and scale, however, can influence the properties of the protein and thus alter partition coefficient and yield. The decreased separation efficiency appears to be correlated with changes in glycosylation at lower cultivation temperatures.     

Present state and perspective of downstream processing of biologically produced 1,3-propanediol and 2,3-butanediol

1,3-Propanediol and 2,3-butanediol are two promising chemicals which have a wide range of applications and can be biologically produced. The separation of these diols from fermentation broth makes more than 50% of the total costs in their microbial production. This review summarizes the present state of methods studied for the recovery and purification of biologically produced diols, with particular emphasis on 1,3-propoanediol. Previous studies on the separation of 1,3-propanediol primarily include evaporation, distillation, membrane filtration, pervaporation, ion exchange chromatography, liquid–liquid extraction, and reactive extraction. Main methods for the recovery of 2,3-butanediol include steam stripping, pervaporation, and solvent extraction. No single method has proved to be simple and efficient, and improvements are especially needed with regard to yield, purity, and energy consumption. Perspectives for an improved downstream processing of biologically produced diols, especially 1,3-propanediol are discussed based on our own experience and recent work. It is argued that separation technologies such as aqueous two-phase extraction with short chain alcohols, pervaporation, reverse osmosis, and in situ extractive or pervaporative fermentations deserve more attention in the future.     

Efficient FLPe recombinase enables scalable production of helper-dependent adenoviral vectors with negligible helper-virus contamination

Helper-dependent (HD), high-capacity adenoviruses are one of the most efficient and safe gene therapy vectors, capable of mediating long-term expression. Currently, the most widely used system for HD vector production avoids significant contamination with helper virus by using producer cells stably expressing a nuclear-targeted Cre recombinase and an engineered first-generation helper virus with parallel loxP sites flanking its packaging signal. The system requires a final, density-based separation of HD and residual helper viruses by ultracentrifugation to reduce contaminating helper virus to low levels. This separation step hinders large-scale production of clinical-grade HD virus. By using a very efficient recombinase, in vitro-evolved FLPe (ref. 14), to excise the helper virus packaging signal in the producer cells, we have developed a scalable HD vector production method. FLP has previously been shown to mediate maximum levels of excision close to 100% compared to 80% for Cre (ref. 15). Utilizing a common HD plasmid backbone, the FLPe-based system reproducibly yielded HD virus with the same low levels of helper virus contamination before any density-based separation by ultracentrifugation. This should allow large-scale production of HD vectors using column chromatography-based virus purification.