Development of a microchannel emulsification process for pancreatic beta cell encapsulation

In this study, we developed a high-throughput microchannel emulsification process to encapsulate pancreatic beta cells in monodisperse alginate beads. The process builds on a stirred emulsification and internal gelation method previously adapted to pancreatic cell encapsulation. Alginate bead production was achieved by flowing a 0.5–2.5% alginate solution with cells and CaCO₃ across a 1-mm thick polytetrafluoroethylene plate with 700 × 200 μm rectangular straight-through channels. Alginate beads ranging from 1.5–3 mm in diameter were obtained at production rates exceeding 140 mL/hr per microchannel. Compared to the stirred emulsification process, the microchannel emulsification beads had a narrower size distribution and demonstrated enhanced compressive burst strength. Both microchannel and stirred emulsification beads exhibited homogeneous profiles of 0.7% alginate concentration using an initial alginate solution concentration of 1.5%. Encapsulated beta cell viability of 89 ± 2% based on live/dead staining was achieved by minimizing the bead residence time in the acidified organic phase fluid. Microchannel emulsification is a promising method for clinical-scale pancreatic beta cell encapsulation as well as other applications in the pharmaceutical, food, and cosmetic industries.     

Comparison of spectroscopy technologies for improved monitoring of cell culture processes in miniature bioreactors

Cell culture process development requires the screening of large numbers of cell lines and process conditions. The development of miniature bioreactor systems has increased the throughput of such studies; however, there are limitations with their use. One important constraint is the limited number of offline samples that can be taken compared to those taken for monitoring cultures in large‐scale bioreactors. The small volume of miniature bioreactor cultures (15 mL) is incompatible with the large sample volume (600 µL) required for bioanalysers routinely used. Spectroscopy technologies may be used to resolve this limitation. The purpose of this study was to compare the use of NIR, Raman, and 2D‐fluorescence to measure multiple analytes simultaneously in volumes suitable for daily monitoring of a miniature bioreactor system. A novel design‐of‐experiment approach is described that utilizes previously analyzed cell culture supernatant to assess metabolite concentrations under various conditions while providing optimal coverage of the desired design space. Multivariate data analysis techniques were used to develop predictive models. Model performance was compared to determine which technology is more suitable for this application. 2D‐fluorescence could more accurately measure ammonium concentration (RMSE_CV 0.031 g L^?1) than Raman and NIR. Raman spectroscopy, however, was more robust at measuring lactate and glucose concentrations (RMSE_CV 1.11 and 0.92 g L^?1, respectively) than the other two techniques. The findings suggest that Raman spectroscopy is more suited for this application than NIR and 2D‐fluorescence. The implementation of Raman spectroscopy increases at‐line measuring capabilities, enabling daily monitoring of key cell culture components within miniature bioreactor cultures. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:337–346, 2017     

Modified CelliGen-packed bed bioreactors for hybridoma cell cultures

This study describes two packed bed bioreactor configurations which were used to culture a mouse-mouse hybridoma cell line (ATCC HB-57) which produces an IgG₁ monoclonal antibody. The first configuration consists of a packed column which is continuously perfused by recirculating oxygenated media through the column. In the second configuration, the packed bed is contained within a stationary basket which is suspended in the vessel of a CelliGen^™ bioreactor. In this configuration, recirculation of the oxygenated media is provided by the CelliGen Cell Lift impeller. Both configurations are packed with disk carriers made from a non-woven polyester fabric. During the steady-state phase of continuous operation, a cell density of 10⁸ cells per cm³ of bed volume was obtained in both bioreactor configurations. The high levels of productivity (0.5 gram MAb per 1 of packed bed per day) obtained in these systems demonstrates that the culture conditions achieved in these packed bed bioreactors are excellent for the continuous propagation of hybridomas using media which contains low levels (1 %) of serum as well as serum-free media. These packed bed bioreactors allow good control of pH, dissolved oxygen and temperature. The media flows evenly over the cells and produces very low shear forces. These systems are easy to set up and operate for prolonged periods of time. The potential for scale-up using Fibra-cel carriers is enhanced due to the low pressure drop and low mass transfer resistance, which creates high void fraction approaching 90% in the packed bed.     

Agitation,aeration and perfusion modules for cell culture bioreactors

For an optimized bioreactor design which is adapted to the cultivation of sensitive animal cells different modular bioreactor components for gentle agitation, sufficient aeration and long-term perfusion were developed and investigated with respect to their suitability from laboratory to production scale. Aeration systems have been designed for both shear sensitive cells and cells which tolerate bubbles. The systems are based on either membranes for bubble-free aeration or stainless steel sparger systems. They were characterized by determination of their oxygen transfer capacity and optimized in cultivation processes of different cell lines under process conditions such as batch and perfusion mode.Different impellers for suspension cells and cells grown on carriers were investigated for their suitability to ensure homogeneous gentle mixing. A large pitch blade impeller as well as a novel 3-blade segment impeller are appropriate for homogeneous mixing at low shear rates. Especially with the 3-blade segment impeller fluid mechanical stress can be reduced at a given stirrer speed which is advantageous for the cultivation of cells attached to microcarriers or extremely shear sensitive suspension cells. However, our results indicate that shear sensitivity of animal cells has been generally overestimated.Continuous perfusion of both suspension cell cultures and cells cultivated on microcarriers could be successfully performed over extended periods of time using stainless steel spinfilters with appropriate pore sizes and systems based on microporous hydrophilic membranes. Spinfilters are suitable cell retention systems for technical scale bioreactors allowing continuous perfusion cultures of suspension cells (pore size 10 to 20 m) as well as anchorage dependent cells grown on microcarriers (pore size 75 m) over six weeks to 3 months.Applying the developed modules for agitation, aeration and perfusion process adapted bioreactor set-ups can be realized which ensure optimum growth and product formation conditions in order to maximize cell and product yields.     

Enzymatic synthesis of β‐glucosylglycerol using a continuous‐flow microreactor containing thermostable β‐glycoside hydrolase CelB immobilized on coated microchannel walls

β‐Glucosylglycerol (βGG) has potential applications as a moisturizing agent in cosmetic products. A stereochemically selective method of its synthesis is kinetically controlled enzymatic transglucosylation from a suitable donor substrate to glycerol as acceptor. Here, the thermostable β‐glycosidase CelB from Pyrococcus furiosus was used to develop a microstructured immobilized enzyme reactor for production of βGG under conditions of continuous flow at 70°C. Using CelB covalently attached onto coated microchannel walls to give an effective enzyme activity of 30 U per total reactor working volume of 25 µL, substrate conversion and formation of transglucosylation product was monitored in dependence of glucosyl donor (2‐nitrophenyl‐β‐D ‐glucoside (oNPGlc), 3.0 or 15 mM; cellobiose, 250 mM), the concentration of glycerol (0.25–1.0 M), and the average residence time (0.2–90 s). Glycerol caused a concentration‐dependent decrease in the conversion of the glucosyl donor via hydrolysis and strongly suppressed participation of the substrate in the reaction as glucosyl acceptor. The yields of βGG were ≥80% and ≈60% based on oNPGlc and cellobiose converted, respectively, and maintained up to near exhaustion of substrate (≥80%), giving about 120 mM (30 g/L) of βGG from the reaction of cellobiose and 1 M glycerol. The structure of the transglucosylation products, 1‐O‐β‐D ‐glucopyranosyl‐rac‐glycerol (79%) and 2‐O‐β‐D ‐glucopyranosyl‐sn‐glycerol (21%), was derived from NMR analysis of the product mixture of cellobiose conversion. The microstructured reactor showed conversion characteristics similar to those for a batchwise operated stirred reactor employing soluble CelB. The advantage of miniaturization to the microfluidic format lies in the fast characterization of full reaction time courses for a range of process conditions using only a minimum amount of enzyme. Biotechnol. Bioeng. 2009;103: 865–872. © 2009 Wiley Periodicals, Inc.     

Packed-bed bioreactors for mammalian cell culture: bioprocess and biomedical applications

This article describes the development history of packed-bed bioreactors (PBRs) used for the culture of mammalian cells. It further reviews the current applications of PBRs and discusses the steps forward in the development of these systems for bioprocess and biomedical applications. The latest generation of PBRs used in bioprocess applications achieve very high cell densities (>10(8) cells ml(-1)) leading to outstandingly high volumetric productivity. However, a major bottleneck of such PBRs is their relatively small volume. The current maximal volume appears to be in the range of 10 to 30 l. A scale-up of more than 10-fold would be necessary for these PBRs to be used in production processes. In biomedical applications, PBRs have proved themselves as compact bioartificial organs, but their metabolic activity declines frequently within 1 to 2 weeks of operation. A main challenge in this field is to develop cell lines that grow consistently to high cell density in vitro and maintain a stable phenotype for a minimum of 1 to 2 months. Achieving this will greatly enhance the usefulness of PBR technology in clinical practice.     

Modeling fluid flow through irregular scaffolds for perfusion bioreactors

Direct perfusion of 3D tissue engineered constructs is known to enhance osteogenesis, which can be partly attributed to enhanced nutrient and waste transport. In addition flow mediated shear stresses are known to upregulate osteogenic differentiation and mineralization. A quantification of the hydrodynamic environment is therefore crucial to interpret and compare results of in vitro bioreactor experiments. This study aims to deal with the pitfalls of numerical model preparation of highly complex 3D bone scaffold structures and aims to provide more accurate wall shear stress (WSS) estimates. µCT imaging techniques were used to reconstruct the geometry of both a titanium (Ti) and a hydroxyapatite scaffold, starting from 430 images with a resolution of 8 µm. To tackle the tradeoff between model size and mesh resolution we selected two concentric regions of interest (cubes with a volume of 1 and 3.375 mm³, respectively) for both scaffolds. A flow guidance in front of the real inlet surface of the scaffold was designed to mimic realistic inlet conditions. With a flow rate of 0.04 mL/min perfused through a 5 mm diameter scaffold at an inlet velocity of 33.95 µm/s we obtained average WSSs of 1.10 and 1.46 mPa for the 1 mm³ and the 3.375 mm³ model of the hydroxyapatite scaffold compared to 1.40 and 1.95 mPa for the 1 mm³ model and the 3.375 mm³ model of the Ti scaffold, showing the important influence of the scaffold micro‐architecture heterogeneity and the proximity of boundaries. To assess that influence we selected cubic portions, of which the WSS data were analyzed, with the same size and the same location within both 1 and 3.375 mm³ cubic models. Varying the size of the inner portions simultaneously in both model selections gives a quantification of the sensitivity to boundary neighborhood. This methodology allows to get more insight in the complex concept of tissue engineering and will likely help to understand and eventually improve the fluid‐mechanical aspects. Biotechnol. Bioeng. 2009;103: 621–630. © 2009 Wiley Periodicals, Inc.     

In situ Raman spectroscopy for simultaneous monitoring of multiple process parameters in mammalian cell culture bioreactors

In this study, the application of Raman spectroscopy to the simultaneous quantitative determination of glucose, glutamine, lactate, ammonia, glutamate, total cell density (TCD), and viable cell density (VCD) in a CHO fed‐batch process was demonstrated in situ in 3 L and 15 L bioreactors. Spectral preprocessing and partial least squares (PLS) regression were used to correlate spectral data with off‐line reference data. Separate PLS calibration models were developed for each analyte at the 3 L laboratory bioreactor scale before assessing its transferability to the same bioprocess conducted at the 15 L pilot scale. PLS calibration models were successfully developed for all analytes bar VCD and transferred to the 15 L scale. © 2012 American Institute of Chemical Engineers Biotechnol. Prog., 2012     

Design of bioreactors suitable for plant cell and tissue cultures

Plant cell suspension cultures and hairy roots are potential sources of secondary metabolites and recombinant proteins. In contrast to traditionally grown “whole wild plants” or “whole transgenic plants”, their production in bioreactors guarantees defined controlled process conditions and therefore minimizes or even prevents variations in product yield and quality, which simplifies process validation and product registration. Moreover, bioreactors and their configuration significantly affect cultivation results by accomplishing and controlling the optimum environment for effective cell growth and production of bioactive substances. This review highlights the main design criteria of the most widely used bioreactor types, both for plant cell suspension cultures and for hairy roots, and outlines suitable low-cost disposable bioreactors which have found increasing acceptance over the last 10 years. Plants for human health in the post-genome era, PSE congress 26.8.2007–29.8.2007, Helsinki.     

Scale‐up analysis for a CHO cell culture process in large‐scale bioreactors

Bioprocess scale‐up is a fundamental component of process development in the biotechnology industry. When scaling up a mammalian cell culture process, it is important to consider factors such as mixing time, oxygen transfer, and carbon dioxide removal. In this study, cell‐free mixing studies were performed in production scale 5,000‐L bioreactors to evaluate scale‐up issues. Using the current bioreactor configuration, the 5,000‐L bioreactor had a lower oxygen transfer coefficient, longer mixing time, and lower carbon dioxide removal rate than that was observed in bench scale 5‐ and 20‐L bioreactors. The oxygen transfer threshold analysis indicates that the current 5,000‐L configuration can only support a maximum viable cell density of 7 × 10⁶ cells mL^?1. Moreover, experiments using a dual probe technique demonstrated that pH and dissolved oxygen gradients may exist in 5,000‐L bioreactors using the current configuration. Empirical equations were developed to predict mixing time, oxygen transfer coefficient, and carbon dioxide removal rate under different mixing‐related engineering parameters in the 5,000‐L bioreactors. These equations indicate that increasing bottom air sparging rate is more efficient than increasing power input in improving oxygen transfer and carbon dioxide removal. Furthermore, as the liquid volume increases in a production bioreactor operated in fed‐batch mode, bulk mixing becomes a challenge. The mixing studies suggest that the engineering parameters related to bulk mixing and carbon dioxide removal in the 5,000‐L bioreactors may need optimizing to mitigate the risk of different performance upon process scale‐up. Biotechnol. Bioeng. 2009;103: 733–746. © 2009 Wiley Periodicals, Inc.     

Monitoring of haploid maize cell suspension culture conditions in bioreactors

Maize (Zea mays L.) haploid cells were cultivated in a 1500 ml aerated and stirred batch bioreactor using modified BM medium. Cell growth was highly affected by pH and dissolved oxygen, and we observed two fairly distinct growth phases. During the first two days after inoculation at pH 5.8, oxygen consumption was high and the cells lowered the pH to a value around 4.3. After this period the pH stabilized at 4.5 and the dissolved oxygen reached a steady level. Decreasing dissolved oxygen concentration leads to lower growth rate and to higher pH. Both events mean stress conditions for the cell culture and probably result in increased genetic variability, and the loss of regeneration capacity. The stress condition during the adaptation phase can be eliminated by decreasing the pH of the medium to 4.7 before inoculation and by keeping dissolved oxygen above 40%. These conditions provide prolonged exponential growth dynamics and the cell suspensions could be the basis of large scale cultures also.Abbreviations 2,4-d 2,4-dichlorophenoxyacetitc acid - NAA naphthalene acetic acid     

Perfusion enhanced polydimethylsiloxane based scaffold cell culturing system for multi‐well drug screening platform

Conventional two‐dimensional cultures in monolayer and sandwich configuration have been used as a model for in vitro drug testing. However, these culture configurations do not present the actual in vivo liver cytoarchitecture for the hepatocytes cultures and thus they may compromise the cells liver‐specific functions and their cuboidal morphology over longer term culture. In this study, we present a three‐dimensional polydimethylsiloxane (PDMS) scaffold with interconnected spherical macropores for the culturing of rat liver cells (hepatocytes). The scaffolds were integrated into our perfusion enhanced bioreactor to improve the nutrients and gas supply for cell cultures. The liver‐specific functions of the cell culture were assessed by their albumin and urea production, and the changes in the cell morphology were tracked by immunofluorescence staining over 9 days of culture period. N‐Acetyl‐Para‐Amino‐Phenol (acetaminophen) was used as drug model to investigate the response of cells to drug in our scaffold‐bioreactor system. Our experimental results revealed that the perfusion enhanced PDMS‐based scaffold system provides a more conducive microenvironment with better cell‐to‐cell contacts among the hepatocytes that maintains the culture specific enzymatic functions and their cuboidal morphology during the culturing period. The numerical simulation results further showed improved oxygen distribution within the culturing chamber with the scaffold providing an additional function of shielding the cell cultures from the potentially detrimental fluid induced shear stresses. In conclusion, this study could serve a crucial role as a platform for future preclinical hepatotoxicity testing. © 2014 American Institute of Chemical Engineers Biotechnol. Prog., 30:418–428, 2014     

Scale‐down simulators for mammalian cell culture as tools to access the impact of inhomogeneities occurring in large‐scale bioreactors

During the scale‐up of a bioprocess, not all characteristics of the process can be kept constant throughout the different scales. This typically results in increased mixing times with increasing reactor volumes. The poor mixing leads in turn to the formation of concentration gradients throughout the reactor and exposes cells to varying external conditions based on their location in the bioreactor. This can affect process performance and complicate process scale‐up. Scale‐down simulators, which aim at replicating the large‐scale environment, expose the cells to changing environmental conditions. This has the potential to reveal adaptation mechanisms, which cells are using to adjust to rapidly fluctuating environmental conditions and can identify possible root causes for difficulties maintaining similar process performance at different scales. This understanding is of utmost importance in process validation. Additionally, these simulators also have the potential to be used for selecting cells, which are most robust when encountering changing extracellular conditions. The aim of this review is to summarize recent work in this interesting and promising area with the focus on mammalian bioprocesses, since microbial processes have been extensively reviewed.     

Protein adsorption in polysulfone hollow fiber bioreactors used for serum-free mammalian cell culture

The recovery of serum-free medium proteins from poly-sulfone hollow fiber bioreactors (HFBRs) was investigated. More than 99% of the initial transferrin was adsorbed to the hydrophobic hollow fibers within 2 h of HFBR operation. A methodology to minimize transferrin adsorption by pre-adsorption of bovine serum albumin (BSA) was developed. BSA adsorption on suspended cut fibers was virtually complete within 1 h. BSA-coated fibers adsorbed only 5% of the transferrin within 10 days, whereas uncoated cut fibers adsorbed more than 99% of the transferrin within 1 h. An improved HFBR startup procedure, using a BSA-coating step before inoculation, resulted in substantially higher transferrin recovery. Additional factors influenced extracapillary space (ECS) transferrin concentrations. Pronounced downstream polarization of transferrin was observed in the ECS. In addition, the 30-kDa nominal molecular weight cutoff ultrafiltration membranes rapidly leaked transferrin from the ECS to the lumen. (c) 1993 John Wiley & Sons, Inc.     

Design principles of photo‐bioreactors for cultivation of microalgae

The present hype in microalgae biotechnology has shown that the topic of photo‐bioreactors has to be revisited with respect to availability in really large scale measured in hectars footprint area, minimization of cost, auxiliary energy demand as well as maintenance and life span. This review gives an overview about present designs and the basic limiting factors which include light distribution to avoid saturation kinetics, mixing along the light gradient to make use of light/dark cycles, aeration and mass transfer along the vertical or horizontal main axis for carbon dioxide supply and oxygen removal and last but not least the energy demand necessary to fulfil these tasks. To make comparison of the performance of different designs easier, a commented list of performance parameters is given. Based on these critical points recent developments in the areas of membranes for gas transfer and optical structures for light transfer are discussed. The fundamental starting point for the optimization of photo‐bioprocesses is a detailed understanding of the interaction between the bioreactor in terms of mass and light transfer as well as the microalgae physiology in terms of light and carbon uptake kinetics and dynamics.     

Novel micro‐bioreactor high throughput technology for cell culture process development: Reproducibility and scalability assessment of fed‐batch CHO cultures

With increasing timeline pressures to get therapeutic and vaccine candidates into the clinic, resource intensive approaches such as the use of shake flasks and bench‐top bioreactors may limit the design space for experimentation to yield highly productive processes. The need to conduct large numbers of experiments has resulted in the use of miniaturized high‐throughput (HT) technology for process development. One such high‐throughput system is the SimCell? platform, a robotically driven, cell culture bioreactor system developed by BioProcessors Corp. This study describes the use of the SimCell? micro‐bioreactor technology for fed‐batch cultivation of a GS‐CHO transfectant expressing a model IgG4 monoclonal antibody. Cultivations were conducted in gas‐permeable chambers based on a micro‐fluidic design, with six micro‐bioreactors (MBs) per micro‐bioreactor array (MBA). Online, non‐invasive measurement of total cell density, pH and dissolved oxygen (DO) was performed. One hundred fourteen parallel MBs (19 MBAs) were employed to examine process reproducibility and scalability at shake flask, 3‐ and 100‐L bioreactor scales. The results of the study demonstrate that the SimCell? platform operated under fed‐batch conditions could support viable cell concentrations up to least 12 × 10⁶ cells/mL. In addition, both intra‐MB (MB to MB) as well as intra‐MBA (MBA to MBA) culture performance was found to be highly reproducible. The intra‐MB and ‐MBA variability was calculated for each measurement as the coefficient of variation defined as CV (%) = (standard deviation/mean) × 100. The % CV values for most intra‐MB and intra‐MBA measurements were generally under 10% and the intra‐MBA values were slightly lower than those for intra‐MB. Cell growth, process parameters, metabolic and protein titer profiles were also compared to those from shake flask, bench‐top, and pilot scale bioreactor cultivations and found to be within ±20% of the historical averages. Biotechnol. Bioeng. 2010; 106: 57–67. © 2010 Wiley Periodicals, Inc.     

三种细胞共培养微流控芯片的设计和制作

设计一种具有“微坝”和“微缝”结构的微流控芯片,能够物理隔离不同细胞,而且培养基中小分子营养物质可以自由流通。实验结果表明在芯片上可以共培养人肺腺癌细胞(A549)、人胚肺成纤维细胞(HLF-1)和人内皮细胞(HUVECs)三种细胞,在72 h培养后三种细胞生长状态良好,具有细胞图形化的特点和功能,为下一步开展多种细胞相互作用等相关研究提供重要的技术平台。