Modeling and simulation of liquid–solid circulating fluidized bed ion exchange system for continuous protein recovery

Liquid–solid circulating fluidized bed (LSCFB) is an integrated two‐column (downcomer and riser) system which can accommodate two separate processes (adsorption and desorption) in the same unit with continuous circulation of the solid particles between the two columns. In this study, a mathematical model based on the assumption of homogeneous fluidization was developed considering hydrodynamics, adsorption‐desorption kinetics and liquid–solid mass transfer. The simulation results showed good agreement with the available experimental results for continuous protein recovery. A parametric sensitivity study was performed to better understand the influence of different operating parameters on the BSA adsorption and desorption capacity of the system. The model developed can easily be extended to other applications of LSCFB. Biotechnol. Bioeng. 2009; 104: 111–126 © 2009 Wiley Periodicals, Inc.     

Soy protein recovery in a solvent-free process using continuous liquid-solid circulating fluidized bed ion exchanger

Soy protein concentrates and soy protein isolates act as ingredients in bakery, meat and dairy products, baby formulas, starting materials for spun textured vegetable products, and other nutritional supplements. In this study, the effectiveness of a liquid-solid circulating fluidized bed (LSCFB) ion exchanger is demonstrated for the recovery of soluble soy proteins from full fat and defatted soy flour. Under steady-state operating conditions, about 50% of the proteins could be recovered from the feed streams entering the ion exchanger. The LSCFB was shown to be a promising system for the recovery of soy protein from both defatted and full fat soy flour solutions. As the ion exchange process captures dissolved proteins, the system may offer a less damaging form of processing compared with the acid precipitation process where soy protein aggregates form and functionality is affected. In addition, the LSCFB allows simultaneous adsorption and desorption of the proteins allowing for a continuous operation. No prefiltration of feed containing suspended particles is required as well, because fluidization is used in place of packed bed technology to improve on current ion exchange processes.     

Continuous protein recovery from whey using liquid-solid circulating fluidized bed ion-exchange extraction

A liquid-solid circulating fluidized bed (LSCFB) continuous ion-exchange extraction system has been investigated for total protein recovery from whey solutions under various operating conditions. The effectiveness of a dynamic seal was evaluated between the riser and the downcomer, and the best conditions for the establishment of this seal were established. Start-up studies indicated that the system is robust and stable. Under optimal conditions, a productivity of 8.2 g of total protein removed per hour per kilogram of resin was achieved with a protein removal efficiency of 78.4%. However, higher overall protein recovery of up to 90% was also achieved under other conditions, with lower protein concentration in the effluent and a lower overall productivity.     

Bioproduction of the aroma compound 2‐Phenylethanol in a solid–liquid two‐phase partitioning bioreactor system by Kluyveromyces marxianus

The rose‐like aroma compound 2‐phenylethanol (2‐PE) is an important fragrance and flavor ingredient. Several yeast strains are able to convert l ‐phenylalanine (l ‐phe) to 2‐PE among which Kluyveromyces marxianus has shown promising results. The limitation of this process is the low product concentration and productivity primarily due to end product inhibition. This study explored the possibility and benefits of using a solid–liquid Two‐Phase Partition Bioreactor (TPPB) system as an in situ product removal technique. The system applies polymer beads as the sequestering immiscible phase to partition 2‐PE and reduce the aqueous 2‐PE concentration to non‐inhibitory levels. Among six polymers screened for extracting 2‐PE, Hytrel® 8206 performed best with a partition coefficient of 79. The desired product stored in the polymer was ultimately extracted using methanol. A 3 L working volume solid–liquid batch mode TPPB using 500 g Hytrel® as the sequestering phase generated a final overall 2‐PE concentration of 13.7 g/L, the highest reported in the current literature. This was based on a polymer phase concentration of 88.74 g/L and aqueous phase concentration of 1.2 g/L. Even better results were achieved via contact with more polymers (approximately 900 g) with the aqueous phase applying a semi‐continuous reactor configuration. In this system, a final 2‐PE concentration (overall) of 20.4 g/L was achieved with 1.4 g/L in the aqueous and 97 g/L in the polymer phase. The overall productivities of these two reactor systems were 0.38 and 0.43 g/L h, respectively. This is the first report in the literature of the use of a polymer sequestering phase to enhance the bioproduction of 2‐PE, and exceeds the performance of two‐liquid phase systems in terms of productivity as well as ease of operation (no emulsions) and ultimate product recovery. Biotechnol. Bioeng. 2009; 104: 332–339 © 2009 Wiley Periodicals, Inc.     

Identification of optimal flow rate for culture media,cell density,and oxygen toward maximization of virus production in a fed-batch baculovirus-insect cell system

In recent times, it has been realized that novel vaccines are required to combat emerging disease outbreaks, and faster optimization is required to respond to global vaccine demands. Although, fed-batch operations offer better productivity, experiment-based optimization of a new fed-batch process remains expensive and time-consuming. In this context, we propose a novel computational framework that can be used for process optimization and control of a fed-batch baculovirus-insect cell system. Since the baculovirus expression vector system (BEVS) is known to be widely used platforms for recombinant protein/vaccine production, we chose this system to demonstrate the identification of optimal profile. Toward this, first, we constructed a mathematical model that captures the time course of cell and virus growth in a baculovirus-insect cell system. Second, the proposed model was used for numerical analysis to determine the optimal operating profiles of control variables such as culture media, cell density, and oxygen based on a multiobjective optimal control formulation. Third, a detailed comparison between batch and fed-batch culture was perfromed along with a comparison between various alternatives of fed-batch operation. Finally, we demonstrate that a model-based quantification of controlled feed addition in fed-batch culture is capable of providing better productivity as compared to a batch culture. The proposed framework can be utilized for the estimation of optimal operating regions of different control variables to achieve maximum infected cell density and virus yield while minimizing the substrate/media, uninfected cell, and oxygen consumption.     

Optimization of elastin‐like polypeptide fusions for expression and purification of recombinant proteins in plants

The demand for recombinant proteins for medical and industrial use is expanding rapidly and plants are now recognized as an efficient, inexpensive means of production. Although the accumulation of recombinant proteins in transgenic plants can be low, we have previously demonstrated that fusions with an elastin‐like polypeptide (ELP) tag can significantly enhance the production yield of a range of different recombinant proteins in plant leaves. ELPs are biopolymers with a repeating pentapeptide sequence (VGVPG)_n that are valuable for bioseparation, acting as thermally responsive tags for the non‐chromatographic purification of recombinant proteins. To determine the optimal ELP size for the accumulation of recombinant proteins and their subsequent purification, various ELP tags were fused to green fluorescent protein, interleukin‐10, erythropoietin and a single chain antibody fragment and then transiently expressed in tobacco leaves. Our results indicated that ELP tags with 30 pentapeptide repeats provided the best compromise between the positive effects of small ELP tags (n = 5–40) on recombinant protein accumulation and the beneficial effects of larger ELP tags (n = 80–160) on recombinant protein recovery during inverse transition cycling (ITC) purification. In addition, the C‐terminal orientation of ELP fusion tags produced higher levels of target proteins, relative to N‐terminal ELP fusions. Importantly, the ELP tags had no adverse effect on the receptor binding affinity of erythropoietin, demonstrating the inert nature of these tags. The use of ELP fusion tags provides an approach for enhancing the production of recombinant proteins in plants, while simultaneously assisting in their purification. Biotechnol. Bioeng. 2009;103: 562–573. © 2009 Wiley Periodicals, Inc.     

Soft constraints-based multiobjective framework for flux balance analysis

The current state of the art for linear optimization in Flux Balance Analysis has been limited to single objective functions. Since mammalian systems perform various functions, a multiobjective approach is needed when seeking optimal flux distributions in these systems. In most of the available multiobjective optimization methods, there is a lack of understanding of when to use a particular objective, and how to combine and/or prioritize mutually competing objectives to achieve a truly optimal solution. To address these limitations we developed a soft constraints based linear physical programming-based flux balance analysis (LPPFBA) framework to obtain a multiobjective optimal solutions. The developed framework was first applied to compute a set of multiobjective optimal solutions for various pairs of objectives relevant to hepatocyte function (urea secretion, albumin, NADPH, and glutathione syntheses) in bioartificial liver systems. Next, simultaneous analysis of the optimal solutions for three objectives was carried out. Further, this framework was utilized to obtain true optimal conditions to improve the hepatic functions in a simulated bioartificial liver system. The combined quantitative and visualization framework of LPPFBA is applicable to any large-scale metabolic network system, including those derived by genomic analyses.     

A simplified and robust protocol for immunoglobulin expression in Escherichia coli cell‐free protein synthesis systems

Cell‐free protein synthesis (CFPS) systems allow for robust protein expression with easy manipulation of conditions to improve protein yield and folding. Recent technological developments have significantly increased the productivity and reduced the operating costs of CFPS systems, such that they can compete with conventional in vivo protein production platforms, while also offering new routes for the discovery and production of biotherapeutics. As cell‐free systems have evolved, productivity increases have commonly been obtained by addition of components to previously designed reaction mixtures without careful re‐examination of the essentiality of reagents from previous generations. Here we present a systematic sensitivity analysis of the components in a conventional Escherichia coli CFPS reaction mixture to evaluate their optimal concentrations for production of the immunoglobulin G trastuzumab. We identify eight changes to the system, which result in optimal expression of trastuzumab. We find that doubling the potassium glutamate concentration, while entirely eliminating pyruvate, coenzyme A, NAD, total tRNA, folinic acid, putrescine and ammonium glutamate, results in a highly productive cell‐free system with a 95% reduction in reagent costs (excluding cell‐extract, plasmid, and T7 RNA polymerase made in‐house). A larger panel of other proteins was also tested and all show equivalent or improved yields with our simplified system. Furthermore, we demonstrate that all of the reagents for CFPS can be combined in a single freeze‐thaw stable master mix to improve reliability and ease of use. These improvements are important for the application of the CFPS system in fields such as protein engineering, high‐throughput screening, and biotherapeutics. © 2015 American Institute of Chemical Engineers Biotechnol. Prog., 31:823–831, 2015     

A DNA replicon system for rapid high‐level production of virus‐like particles in plants

Recombinant virus‐like particles (VLPs) represent a safe and effective vaccine strategy. We previously described a stable transgenic plant system for inexpensive production and oral delivery of VLP vaccines. However, the relatively low‐level antigen accumulation and long‐time frame to produce transgenic plants are the two major roadblocks in the practical development of plant‐based VLP production. In this article, we describe the optimization of geminivirus‐derived DNA replicon vectors for rapid, high‐yield plant‐based production of VLPs. Co‐delivery of bean yellow dwarf virus (BeYDV)‐derived vector and Rep/RepA‐supplying vector by agroinfiltration of Nicotiana benthamiana leaves resulted in efficient replicon amplification and robust protein production within 5 days. Co‐expression of the P19 protein of tomato bush stunt virus, a gene silencing inhibitor, further enhanced VLP accumulation by stabilizing the mRNA. With this system, hepatitis B core antigen (HBc) and Norwalk virus capsid protein (NVCP) were produced at 0.80 and 0.34 mg/g leaf fresh weight, respectively. Sedimentation analysis and electron microscopy of transiently expressed antigens verified the efficient assembly of VLPs. Furthermore, a single replicon vector containing a built‐in Rep/RepA cassette without P19 drove protein expression at similar levels as the three‐component system. These results demonstrate the advantages of fast and high‐level production of VLP‐based vaccines using the BeYDV‐derived DNA replicon system for transient expression in plants. Biotechnol. Bioeng. 2009;103: 706–714. © 2009 Wiley Periodicals, Inc.     

Optimizing performance of semi‐continuous cell culture in an ambr15™ microbioreactor using dynamic flux balance modeling

The ambr bioreactors are single‐use microbioreactors for cell line development and process optimization. With operating conditions for large‐scale biopharmaceutical production properly scaled down, microbioreactors such as the ambr15? can potentially be used to predict the effect of process changes such as modified media or different cell lines. While there have been some recent studies evaluating the ambr15? technology as a scale‐down model for fed‐batch operations, little has been reported for semi‐continuous or continuous operation. Gassing rates and dilution rates in the ambr15? were varied in this study to attempt to replicate performance of a perfusion process at the 5 L scale. At both scales, changes to metabolite production and consumption, and cell growth rate and therapeutic protein production were measured. Conditions were identified in the ambr15? bioreactor that produced metabolic shifts and specific metabolic and protein production rates that are characteristic of the corresponding 5 L perfusion process. A dynamic flux balance (DFB) model was employed to understand and predict the metabolic changes observed. The DFB model predicted trends observed experimentally, including lower specific glucose consumption and a switch from lactate production to consumption when dissolved CO₂ was maintained at higher levels in the broth. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 34:420–431, 2018     

Optimization of chimeric HIV‐1 virus‐like particle production in a baculovirus‐insect cell expression system

A baculovirus‐insect cell expression system potentially provides the means to produce prophylactic HIV‐1 virus‐like particle (VLP) vaccines inexpensively and in large quantities. However, the system must be optimized to maximize yields and increase process efficiency. In this study, we optimized the production of two novel, chimeric HIV‐1 VLP vaccine candidates (GagRT and GagTN) in insect cells. This was done by monitoring the effects of four specific factors on VLP expression: these were insect cell line, cell density, multiplicity of infection (MOI), and infection time. The use of western blots, Gag p24 ELISA, and four‐factorial ANOVA allowed the determination of the most favorable conditions for chimeric VLP production, as well as which factors affected VLP expression most significantly. Both VLP vaccine candidates favored similar optimal conditions, demonstrating higher yields of VLPs when produced in the Trichoplusia ni Pro? insect cell line, at a cell density of 1 × 10⁶ cells/mL, and an infection time of 96 h post infection. It was found that cell density and infection time were major influencing factors, but that MOI did not affect VLP expression significantly. This work provides a potentially valuable guideline for HIV‐1 protein vaccine optimization, as well as for general optimization of a baculovirus‐based expression system to produce complex recombinant proteins. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2009     

Integrated two‐liquid phase bioconversion and product‐recovery processes for the oxidation of alkanes: Process design and economic evaluation

Pseudomonas oleovorans and recombinant strains containing the alkane oxidation genes can produce alkane oxidation products in two‐liquid phase bioreactor systems. In these bioprocesses the cells, which grow in the aqueous phase, oxidize apolar, non‐water soluble substrates. The apolar products typically accumulate in the emulsified apolar phase. We have studied both the bioconversion systems and several downstream processing systems to separate and purify alkanols from these two‐liquid phase media. Based on the information generated in these studies, we have now designed bioconversion and downstream processing systems for the production of 1‐alkanols from n‐alkanes on a 10 kiloton/yr scale, taking the conversion of n‐octane to 1‐octanol as a model system. Here, we describe overall designs of fed‐batch and continuous‐fermentation processes for the oxidation of octane to 1‐octanol by Pseudomonas oleovorans, and we discuss the economics of these processes. In both systems the two‐liquid phase system consists of an apolar phase with hexadecene as the apolar carrier solvent into which n‐octane is dissolved, while the cells are present in the aqueous phase. In one system, multiple‐batch fermentations are followed by continuous processing of the product from the separated apolar phase. The second system is based on alkane oxidation by continuously growing cultures, again followed by continuous processing of the product. Fewer fermentors were required and a higher space‐time‐yield was possible for production of 1‐octanol in a continuous process. The overall performance of each of these two systems has been modeled with Aspen software. Investment and operating costs were estimated with input from equipment manufacturers and bulk‐material suppliers. Based on this study, the production cost of 1‐octanol is about 7 US$kg⁻¹ when produced in the fed‐batch process, and 8 US$kg⁻¹ when produced continuously. The comparison of upstream and downstream capital costs and production costs showed significantly higher upstream costs for the fed‐batch process and slightly higher upstream costs for continuous fermentation. The largest cost contribution was due to variable production costs, mainly resulting from media costs. The organisms used in these systems are P. putida alk+ recombinants which oxidize alkanes, but cannot oxidize the resulting alkanols further. Hence, such cells need a second carbon source, which in these systems is glucose. Although the continuous process is about 10% more expensive than the fed‐batch process, improvements to reduce overall cost can be achieved more easily for continuous than for fed‐batch fermentation by decreasing the dilution rate while maintaining near constant productivity. Improvements relevant to both processes can be achieved by increasing the biocatalyst performance, which results in improved overall efficiency, decreased capital investment, and hence, decreased production cost. © 1999 John Wiley & Sons, Inc. Biotechnol Bioeng 84: 459–477, 1999.     

Quantification of non‐specific binding of magnetic micro‐ and nanoparticles using cell tracking velocimetry: Implication for magnetic cell separation and detection

The maturation of magnetic cell separation technology places increasing demands on magnetic cell separation performance. While a number of factors can cause sub‐optimal performance, one of the major challenges can be non‐specific binding of magnetic nano‐ or microparticles to non‐targeted cells. Depending on the type of separation, this non‐specific binding can have a negative effect on the final purity, the recovery of the targeted cells, or both. In this work, we quantitatively demonstrate that non‐specific binding of magnetic nanoparticles can impart a magnetization to cells such that these cells can be retained in a separation column and thus negatively impact the purity of the final product and the recovery of the desired cells. Through experimental data and theoretical arguments, we demonstrate that the number of MACS magnetic particles needed to impart a magnetization that is sufficient to cause non‐targeted cells to be retained in the column to be on the order of 500–1,000 nanoparticles. This number of non‐specifically bound particles was demonstrated experimentally with an instrument, cell tracking velocimeter, CTV, and it is demonstrated that the sensitivity of the CTV instrument for Fe atoms contained in magnetic nanoparticles on the order of 1 × 10^?15 g/mL of Fe. Biotechnol. Bioeng. 2010;105: 1078–1093. © 2009 Wiley Periodicals, Inc.     

Bioproduction and characterization of a pH responsive self‐assembling peptide

Peptide P₁₁‐4 (QQRFEWEFEQQ) was designed to self‐assemble to form β‐sheets and nematic gels in the pH range 5–7 at concentrations ≥12.6 mM in water. This self‐assembly is reversibly controlled by adjusting the pH of the solvent. It can also self‐assemble into gels in biological media. This together with its biocompatibility and biodegradability make P₁₁‐4 an attractive building block for the fabrication of nanoscale materials with uses in, for example, tissue engineering. A limitation to large‐scale production of such peptides is the high cost of solid phase chemical synthesis. We describe expression of peptide P₁₁‐4 in the bacterium Escherichia coli from constructs carrying tandem repeats of the peptide coding sequence. The vector pET31b+ was used to express P₁₁‐4 repeats fused to the ketosteroid isomerase protein which accumulates in easily recoverable inclusion bodies. Importantly, the use of auto‐induction growth medium to enhance cell density and protein expression levels resulted in recovery of 2.5 g fusion protein/L culture in both shake flask and batch fermentation. Whole cell detergent lysis allowed recovery of inclusion bodies largely composed of the fusion protein. Cyanogen bromide cleavage followed by reverse phase HPLC allowed purification of the recombinant peptide with a C‐terminal homoserine lactone (rP₁₁‐4(hsl)). This recombinant peptide formed pH dependent hydrogels, displayed β‐structure measured by circular dichroism and fibril formation observed by transmission electron microscopy. Biotechnol. Bioeng. 2009;103: 241–251. © 2009 Wiley Periodicals, Inc.     

Modeling and multi-criteria optimization of an industrial process for continuous lactic acid production

The key feature of this paper is the optimization of an industrial process for continuous production of lactic acid. For this, a two-stage fermentor process integrated with cell recycling has been mathematically modeled and optimized for overall productivity, conversion, and yield simultaneously. Non-dominated sorting genetic algorithm (NSGA-II) was applied to solve the constrained multi-objective optimization problem as it is capable of finding multiple Pareto-optimal solutions in a single run, thereby avoiding the need to use a single-objective optimization several times. Compared with traditional methods, NSGA-II could find most of the solutions in the true Pareto-front and its simulation is also very direct and convenient. The effects of operating variables on the optimal solutions are discussed in detail. It was observed that we can make higher profit with an acceptable compromise in a two-stage system with greater efficiency.     

Ultra scale‐down approaches for clarification of mammalian cell culture broths in disc‐stack centrifuges

Ultra‐scale down (USD) methodology developed by University College London for cell broth clarification with industrial centrifuges was applied to two common cell lines (NS0 and GS‐CHO) expressing various therapeutic monoclonal antibodies. A number of centrifuges at various scales were used with shear devices operating either by high speed rotation or flow‐through narrow channels. The USD methodology was found effective in accounting for both gravitational and shear effects on clarification performance with three continuous centrifuges at pilot and manufacturing scales. Different shear responses were observed with the two different cell lines and even with the same cell line expressing different products. Separate particle size analysis of the treated broths seems consistent with the shear results. Filterability of the centrifuged solutions was also evaluated to assess the utility of the USD approach for this part of the clarification operation. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2009     

Integrated continuous production of recombinant therapeutic proteins

In the current environment of diverse product pipelines, rapidly fluctuating market demands and growing competition from biosimilars, biotechnology companies are increasingly driven to develop innovative solutions for highly flexible and cost‐effective manufacturing. To address these challenging demands, integrated continuous processing, comprised of high‐density perfusion cell culture and a directly coupled continuous capture step, can be used as a universal biomanufacturing platform. This study reports the first successful demonstration of the integration of a perfusion bioreactor and a four‐column periodic counter‐current chromatography (PCC) system for the continuous capture of candidate protein therapeutics. Two examples are presented: (1) a monoclonal antibody (model of a stable protein) and (2) a recombinant human enzyme (model of a highly complex, less stable protein). In both cases, high‐density perfusion CHO cell cultures were operated at a quasi‐steady state of 50–60 × 10⁶ cells/mL for more than 60 days, achieving volumetric productivities much higher than current perfusion or fed‐batch processes. The directly integrated and automated PCC system ran uninterrupted for 30 days without indications of time‐based performance decline. The product quality observed for the continuous capture process was comparable to that for a batch‐column operation. Furthermore, the integration of perfusion cell culture and PCC led to a dramatic decrease in the equipment footprint and elimination of several non‐value‐added unit operations, such as clarification and intermediate hold steps. These findings demonstrate the potential of integrated continuous bioprocessing as a universal platform for the manufacture of various kinds of therapeutic proteins. Biotechnol. Bioeng. 2012; 109: 3018–3029. © 2012 Wiley Periodicals, Inc.     

Economic analysis of pilot‐scale production of B‐phycoerythrin

β‐Phycoerythrin is a color protein with several applications, from food coloring to molecular labeling. Depending on the application, different purity is required, affecting production cost and price. Different production and purification strategies for B‐phycoerythrin have been developed, the most studied are based on the production using Porphyridium cruentum and purified using chromatographic techniques or aqueous two‐phase systems. The use of the latter can result in a less expensive and intensive recovery of the protein, but there is lack of a proper economic analysis to study the effect of using aqueous two‐phase systems in a scaled‐up process. This study analyzed the production of B‐Phycoerythrin using real data obtained during the scale‐up of a bioprocess using specialized software (BioSolve, Biopharm Services, UK). First, a sensitivity analysis was performed to identify critical parameters for the production cost, then a Monte Carlo analysis to emulate real processes by adding uncertainty to the identified parameters. Next, the bioprocess was analyzed to determine its financial attractiveness and possible optimization strategies were tested and discussed. Results show that aqueous two‐phase systems retain their advantages of low cost and intensive recovery (54.56%); the costs of production per gram calculated (before titer optimization: US$15,709 and after optimization: US$2,374) allowed to obtain profit (in the range of US$millions in a 10‐year period) for a potential company taking this production method by comparing the production cost against commercial prices. The bioprocess analyzed is a promising and profitable method for the generation of a highly purified B‐phycoerythrin. © 2016 American Institute of Chemical Engineers Biotechnol. Prog., 32:1472–1479, 2016     

Directed evolution of a secretory leader for the improved expression of heterologous proteins and full‐length antibodies in Saccharomyces cerevisiae

Because of its eukaryotic nature, simple fermentation requirements, and pliable genetics, there have been many attempts at improving recombinant protein production in Saccharomyces cerevisiae. These strategies typically involve altering the expression of a native protein thought to be involved in heterologous protein trafficking. Usually, these approaches yield three‐ to tenfold improvements over wild‐type strains and are almost always specific to one type of protein. In this study, a library of mutant alpha mating factor 1 leader peptides (MFα1pp) is screened for the enhanced secretion of a single‐chain antibody. One of the isolated mutants is shown to enhance the secretion of the scFv up to 16‐fold over wild type. These leaders also confer a secretory improvement to two other scFvs as well as two additional, structurally unrelated proteins. Moreover, the improved leader sequences, combined with strain engineering, allow for a 180‐fold improvement over previous reports in the secretion of full‐length, functional, glycosylated human IgG₁. The production of full‐length IgG₁ at milligram per liter titers in a simple, laboratory‐scale system will significantly expedite drug discovery and reagent synthesis while reducing antibody cloning, production, and characterization costs. Biotechnol. Bioeng. 2009;103: 1192–1201. © 2009 Wiley Periodicals, Inc.     

Maximizing power production in a stack of microbial fuel cells using multiunit optimization method

This study demonstrates real‐time maximization of power production in a stack of two continuous flow microbial fuel cells (MFCs). To maximize power output, external resistances of two air–cathode membraneless MFCs were controlled by a multiunit optimization algorithm. Multiunit optimization is a recently proposed method that uses multiple similar units to optimize process performance. The experiment demonstrated fast convergence toward optimal external resistance and algorithm stability during external perturbations (e.g., temperature variations). Rate of the algorithm convergence was much faster than in traditional maximum power point tracking algorithms (MPPT), which are based on temporal perturbations. A power output of 81–84 mW/L_A (A = anode volume) was achieved in each MFC. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2009