Enhanced chitosan production and modeling hyphal growth of Mucor rouxii interpreting the dependence of chitosan yields on processing and cultivation time

Chitosan is a major structural component of fungal cell walls and has diverse medical and other applications. However, cost‐effective culture and extraction methods for fungi need to be developed. Therefore, Mucor rouxii was grown on YPG‐media in both submerged batch and semi‐continuous cultures. Chitosan was extracted from the mycelia to explore strategies to enhance yields and production rates. As observed in earlier studies, M. rouxii is able to adapt to shear stress when cultured semi‐continuously. Modeling the hyphal growth of batch experiments shows that the mycelia were ruptured by shear forces within a short cultivation time shown by a decreased hyphal length. However, an increasing chitosan content was observed with an increasing cultivation period in semi‐continuous cultures, which is an indication for the adaption to shear stress. Semi‐continuous culture resulted in the highest contents of extractable chitosan. The results and models of hyphal growth, including tip extension and branching, suggest that repeated batch cultures may be optimal for chitosan production.     

Comparison of a quadroma and its parent hybridomas in fed batch culture

A quadroma (#22 × 63), formed by the fusion of two hybridomas, and its parent hybridomas (#22 and FMC 63) were each grown in fed batch cultures in order to examine the change in antibody productivity over time of the quadroma compared to its parent hybridomas. The growth rate, glucose uptake rate and lactate production rate of the quadroma were found to be intermediate between those of its parent cells of origin. The specific antibody productivity and internal antibody content of the quadroma followed the same decreasing trends over time as those seen in both parent hybridomas. Losses in specific antibody production rate and antibody content, however, occurred at a faster rate for the quadroma than for either of its parent hybridomas. Although the growth of a non-producing subpopulation is presumed to account for the drop in antibody production, there was no direct correlation between the percentage of high antibody containing cells, as determined by flow cytometry, and the specific antibody production rate.     

大肠杆菌发酵生产重组人源抗-HBs Fab

在KLF2000发酵罐中利用补料分批培养技术培养表达含重组质粒pBAD/HBs Fab的TOP10大肠杆菌,生产人源抗-HBs Fab,为批量生产作准备,在发酵过程中,控制溶氧30%以上,温度37℃,在基础培养基内生长4h后,补加以甘油为碳源的补料,继续生长到9h,加入阿拉伯糖,至终浓度为0.02%,30℃诱导表达5h,收集菌体,纯化制备目的蛋白。利用Western blot方法检测Fab抗原性,Dot blot方法检测生物学活性。14h发酵结束后,菌体密度最终达96g/L,纯化所得蛋白大约占菌体总蛋白的6%,含量为80mg/L,以重组质粒pBAD/HBs Fab,大肠杆菌TOP10表达表达比率与摇瓶相比没有降低,表达量达80mg/L左右,为大批量生产作了准备。     

Synthesis of the Human Insulin Gene: Protein Expression,Scaling Up and Bioactivity

Abstract

Optimized Synthetic human insulin gene was preferred to easy of cloning, plasmid stability, and protein expression away from the native sequence and its rare codons. Two steps to obtain the insulin, so we assembled the gene of 293 bp using a battery of overlapped synthetic oligos, then cloned into pET101directional TOPO expression vector downstream to the T7 promoter. The proinsulin products were produced as inclusion bodies in E. coli at a level of 10%. The batch cultivation of the strain yielded 6 g/L, while the high cell density of fed‐batch cultivation yielded 46 g/L. The proinsulin purification yielded 110 mg/gram cell weight, and 1.3 mg/gram of a bioactive insulin. The native insulin was generated by enzymatic conversion of chemically processed proinsulin. The produced insulin was matched with that of a commercial aqueous version at a level of enzyme immunoassys, SDS‐PAGE, RP‐HPLC, and bioactivity. The present results showed that the produced insulin has a comparable biochemical and potency similar to that of commercial one.     

Integrated continuous bioprocessing: Economic,operational, and environmental feasibility for clinical and commercial antibody manufacture

This paper presents a systems approach to evaluating the potential of integrated continuous bioprocessing for monoclonal antibody (mAb) manufacture across a product's lifecycle from preclinical to commercial manufacture. The economic, operational, and environmental feasibility of alternative continuous manufacturing strategies were evaluated holistically using a prototype UCL decisional tool that integrated process economics, discrete‐event simulation, environmental impact analysis, operational risk analysis, and multiattribute decision‐making. The case study focused on comparing whole bioprocesses that used either batch, continuous or a hybrid combination of batch and continuous technologies for cell culture, capture chromatography, and polishing chromatography steps. The cost of goods per gram (COG/g), E‐factor, and operational risk scores of each strategy were established across a matrix of scenarios with differing combinations of clinical development phase and company portfolio size. The tool outputs predict that the optimal strategy for early phase production and small/medium‐sized companies is the integrated continuous strategy (alternating tangential flow filtration (ATF) perfusion, continuous capture, continuous polishing). However, the top ranking strategy changes for commercial production and companies with large portfolios to the hybrid strategy with fed‐batch culture, continuous capture and batch polishing from a COG/g perspective. The multiattribute decision‐making analysis highlighted that if the operational feasibility was considered more important than the economic benefits, the hybrid strategy would be preferred for all company scales. Further considerations outside the scope of this work include the process development costs required to adopt continuous processing. © 2017 The Authors Biotechnology Progress published by Wiley Periodicals, Inc. on behalf of American Institute of Chemical Engineers Biotechnol. Prog., 33:854–866, 2017     

Heterotrophic production of Chlorella sp. TISTR 8990—biomass growth and composition under various production conditions

The green microalga Chlorella sp. TISTR 8990 was grown heterotrophically in the dark using various concentrations of a basal glucose medium with a carbon‐to‐nitrogen mass ratio of 29:1. The final biomass concentration and the rate of growth were highest in the fivefold concentrated basal glucose medium (25 g L^?1 glucose, 2.5 g L^?1 KNO₃) in batch operations. Improving oxygen transfer in the culture by increasing the agitation rate and decreasing the culture volume in 500‐mL shake flasks improved growth and glucose utilization. A maximum biomass concentration of nearly 12 g L^?1 was obtained within 4 days at 300 rpm, 30°C, with a glucose utilization of nearly 76% in batch culture. The total fatty acid (TFA) content of the biomass and the TFA productivity were 102 mg g^?1 and 305 mg L^?1 day^?1, respectively. A repeated fed‐batch culture with four cycles of feeding with the fivefold concentrated medium in a 3‐L bioreactor was evaluated for biomass production. The total culture period was 11 days. A maximum biomass concentration of nearly 26 g L^?1 was obtained with a TFA productivity of 223 mg L^?1 day^?1. The final biomass contained (w/w) 13.5% lipids, 20.8% protein and 17.2% starch. Of the fatty acids produced, 52% (w/w) were saturated, 41% were monounsaturated and 7% were polyunsaturated (PUFA). A low content of PUFA in TFA feedstock is required for producing high quality biodiesel. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:1589–1600, 2017     

Process development for production of human granulocyte-colony stimulating factor by high cell density cultivation of recombinant <Emphasis Type="Italic">Escherichia coli</Emphasis>

The fed-batch process using glucose as the sole source of carbon and energy with exponential feeding rate was carried out for high cell density cultivation of recombinant Escherichia coli BL21 (DE3) expressing human granulocyte-colony stimulating factor (hG-CSF). IPTG was used to induce the expression of hG-CSF at 48 g dry cell wt l⁻¹ during high cell density culture of recombinant E. coli BL21 (DE3) [pET23a-g-csf]. The final cell density, specific yield and overall productivity of hG-CSF were obtained as ~64 g dry cell wt l⁻¹, 223 mg hG-CSF g⁻¹ dry cell wt and 775 mg hG-CSF l⁻¹ h⁻¹, respectively. The resulting purification process used cell lysis, inclusion body (IB) preparation, refolding, DEAE and Butyl-Sepharose. Effects of different process conditions such as cell lysis and washing of IB were evaluated. The results reveal that the cells lyzed at 1,200 bar, 99.9% and Triton removed about 64% of the LPS but sarcosyl had no effect on removal of nucleic acids and LPS. Further analysis show that DEAE column removes DNA about 84%. Cupper concentration was identified as parameter that could have a significant impact on aggregation, as an unacceptable pharmaceutical form that decrease process yields. The purity of purified hG-CSF was more than 99%. Also the comparison of activity between purified hG-CSF and commercial form do not show valuable decrease in activity in purified form.     

Industrial production of heterologous proteins by fed-batch cultures of the yeast Saccharomyces cereuisiae

Abstract: This review concerns the issues involved in the industrial development of fed-batch culture processes with Saccharomyces cereriviae strains producing heterologous proteins. Most of process development considerations with fed-batch recombinant cultures are linked to the reliability and reproducibility of the process for manufacturing environments where quality assurance and quality control aspects are paramount. In this respect, the quality, safety and efficacy of complex biologically active molecules produced by recombinant techniques are strongly influenced by the genetic background of the host strain, genetic stability of the transformed strain and production process factors. An overview of the recent literature of these culture-related factors is coupled with our experience in yeast fed-batch process development for producing various therapeutic grade proteins. The discussion is based around three principal topics: genetics, microbial physiology and fed-batch process design. It includes the fundamental aspects of yeast strain physiology, the nature of the recombinant product, quality control aspects of the biological product, features of yeast expression vectors, expression and localization of recombinant products in transformed cells and fed-batch process considerations for the industrial production of Saccharomyces cerevisiae recombinant proteins. It is our purpose that this review will provide a comprehensive understanding of the fed-batch recombinant production processes and challenges commonly encountered during process development.