Large-scale Bioreactors Research Articles

Protein-protein-interaction network organization of the hypusine modification system.

Hypusine modification of eukaryotic initiation factor 5A (eIF-5A) represents a unique and highly specific post-translational modification with regulatory functions in cancer, diabetes, and infectious diseases. However, the specific cellular pathways that are influenced by the hypusine modification remain largely unknown. To globally characterize eIF-5A and hypusine-dependent pathways, we used an approach that combines large-scale bioreactor cell culture with tandem affinity purification and mass spectrometry: “bioreactor-TAP-MS/MS.” By applying this approach systematically to all four components of the hypusine modification system (eIF-5A1, eIF-5A2, DHS, and DOHH), we identified 248 interacting proteins as components of the cellular hypusine network, with diverse functions including regulation of translation, mRNA processing, DNA replication, and cell cycle regulation. Network analysis of this data set enabled us to provide a comprehensive overview of the protein-protein interaction landscape of the hypusine modification system. In addition, we validated the interaction of eIF-5A with some of the newly identified associated proteins in more detail. Our analysis has revealed numerous novel interactions, and thus provides a valuable resource for understanding how this crucial homeostatic signaling pathway affects different cellular functions.

Characterization of soluble microbial products in 10 large-scale membrane bioreactors for municipal wastewater treatment in China

In order to fill the knowledge gaps between lab/pilot-scale and full-scale operations and contribute basic information to long-term and stable operation of large-scale membrane bioreactors (MBRs), a systematic investigation was first conducted focused on soluble microbial products (SMPs) in 10 large-scale MBRs (capacity over 10,000 m3/d) for municipal wastewater treatment distributed in 4 different areas of China from fall to winter. The majority of these MBR plants had been operated stably for at least 1 year. Fundamental properties of SMPs were investigated, including composition, molecular weight distribution, hydrophobicity, fluorescent characteristics and fouling potential. The results showed that the concentration of SMPs ranged roughly from 5 to 25 mg TOC/L, with the major component being polysaccharides (ca. 3–18 mg/L) followed by humic substances (ca. 2–10 mg/L); while the protein concentration was relatively low (<5 mg/L). The SMPs presented a broad molecular weight distribution from smaller than 1 kDa to over 100 kDa. About half of the SMPs were hydrophilic substances mainly contributed by polysaccharides; humic substances were concentrated in hydrophobic fractions while proteins showed a relatively wide distribution. The fluorescent properties were found to be affected appreciably by the influent quality. The batch fouling tests indicated that the initial fouling rate correlated significantly with SMPs concentrations, which was particularly the case for hydrophilic and large-molecular-weight fractions. These findings may contribute to better understanding of membrane fouling in engineering conditions and assist in long-term and stable operation of full-scale MBRs.

Limitations for transferring lab-scale microfiltration results to large-scale membrane bioreactor (MBR) processes

Membrane bioreactor (MBR) processes for the treatment of municipal and industrial wastewater have been extensively investigated in the past years. For this purpose, synthetic model feeds containing dissolved macromolecules and/or suspended solids were used to allow for a stable and reproducible feed composition. Lab-scale setups equipped with single membrane filaments and pilot plants containing single-bundle configurations were applied. Despite the fact that numerous of the corresponding findings were successfully transferred to large-scale MBR processes, it is expected that the filterability of activated sludge differs significantly from that of common model substances. Moreover, phenomena linked to the highly complex multi-phase flow of liquid, suspended solids and dispersed air bubbles which physically interacts with the membrane filaments make downsizing difficult. Therefore, the overall objective of this study was to evaluate the transferability of lab-scale microfiltration results to large-scale MBR processes. Our investigations have shown that the rheology of a model feed containing silica particles is similar to that of activated sludge with MLSS⩽3.5g/L. A noticeable sub-critical fouling was observed, but was removable by an intensive chemical cleaning using sodium hypochlorite. Lower fouling rates when increasing the aeration frequency with the same net aeration rate were found for both single-fibre and single-bundle tests, but are more pronounced on the larger scale. A macroscopic circulation flow affects the filtration performance of full-scale MBRs, but is difficult to mimic on a smaller scale. Fibre motion enhances the filtration performance, but is insensitive to packing density variations for bundles of up to four filaments.

KLa as a predictor for probe-independent mammalian cell bioprocesses in orbitally shaken bioreactors

Background Orbitally shaken flasks are commonly used at an early stage of bioprocess development with mammalian cells. In contrast to large-scale stirred-tank bioreactors, shaken flasks are usually operated in probe-independent bioprocesses, i.e. without strictly controlling the pH or dissolved oxygen concentration (DO). As a consequence, gas transfer issues are thought to limit the effectiveness of orbitally shaken flasks and bioreactors (OSRs). To define optimal operating conditions for probe-independent bioprocesses in OSRs, we tested the effects of the mass transfer coefficient of oxygen (kLa) on mammalian cell growth, recombinant protein production, and environmental conditions of the culture (pH, DO).

Effect of post-induction substrate oscillation on recombinant alkaline phosphatase production expressed in Escherichia coli

Microorganisms are exposed to fast changes in microenvironment in large scale bioreactors. Because of their fast response to the changes, overall performance of biological system in small scale differs from large scale. Hence the variations in the environment that microorganisms are living in are mimicked in small scale. For this purpose one way is to feed substrate into the bioreactor in an oscillatory profile. In this work two different types of triangular oscillatory feeding profiles were applied as the post induction feeding strategy in intracellular recombinant alkaline phosphatase production expressed in Escherichia coli to find out if this biological system behaves in inhomogeneous environment differently. On line and offline measurements provide evaluation of product quality and quantity. Then the results of the experiments were compared with those of the control run at which constant feeding rate was executed. The results showed that oscillatory feeding at which cells were not starved led to higher yield of protein per substrate (0.027C-mol/C-mol) and higher activity per protein (0.79U/mg) when compared to a constant feeding rate (0.011C-mol/C-mol and 0.11U/mg).

Insights into large‐scale cell‐culture reactors: I. Liquid mixing and oxygen supply

In the pharmaceutical industry, it is state of the art to produce recombinant proteins and antibodies with animal-cell cultures using bioreactors with volumes of up to 20 m(3) . Recent guidelines and position papers for the industry by the US FDA and the European Medicines Agency stress the necessity of mechanistic insights into large-scale bioreactors. A detailed mechanistic view of their practically relevant subsystems is required as well as their mutual interactions, i.e., mixing or homogenization of the culture broth and sufficient mass and heat transfer. In large-scale bioreactors for animal-cell cultures, different agitation systems are employed. Here, we discuss details of the flows induced in stirred tank reactors relevant for animal-cell cultures. In addition, solutions of the governing fluid dynamic equations obtained with the so-called computational fluid dynamics are presented. Experimental data obtained with improved measurement techniques are shown. The results are compared to previous studies and it is found that they support current hypotheses or models. Progress in improving insights requires continuous interactions between more accurate measurements and physical models. The paper aims at promoting the basic mechanistic understanding of transport phenomena that are crucial for large-scale animal-cell culture reactors.

Determination of the stoichiometry and critical oxygen tension in the production culture of bacterial cellulose using saccharified food wastes

The stoichiometry of the entire reaction in a 50 L scaled-up production culture of bacterial cellulose (BC), using saccharified food wastes (SFW), was analyzed in this study. The stoichiometric analysis was carried out using the chemical formula, yield, degrees of reduction of the major components, and the respiratory quotient (RQ). Based on the stoichiometric analysis, the amounts of substrate, oxygen supply and BC production etc., were able to be predicted. In addition, the amount of energy generated in the culture was predicted based on the oxygen consumption via the stoichiometric analysis. The stoichiometry of BC production using SFW in a 50 L large scale reactor will be useful as a standard for mass production of the culture. The stoichiometric analysis can also help the designers of reactors decide on the boiler capacity and oxygen supply for a large scale bioreactor system. The OUR (oxygen uptake rate) of Acetobacter xylinum KJ1 in a 12 hour-age cultivation was 0.21 mg DO/L·min, from which the critical DO concentration was suggested to be maintained above 3.10 ppm to prevent oxygen limitation during the BC production culture. The results indicated that pure oxygen should be supplied during the exponential phase, where DO depletion was observed. An ascertainment experiment, with the addition of pure oxygen into the culture system, showed BC production of 7.37 g/L, which was considerable productivity.

A Review of Bioreactor Protocols for Human Neural Precursor Cell Expansion in Preparation for Clinical Trials

Tissue-specific human neural precursor cells (hNPCs) can be isolated from various regions of the developing or adult central nervous system and may serve as a viable source of cells in cell replacement therapies for the treatment of neurodegenerative disorders. However, in order for cell replacement strategies to become a routine therapeutic option for the treatment of neurodegenerative disorders, hNPCs should be generated under standardized and controlled conditions. Studies over the last two decades have focused on developing cell growth media and cell handling protocols for expansion and differentiation of hNPCs in culture. Key studies have reported the development of serum-free growth media and large-scale computer-controlled suspension bioreactors that can support high cell proliferation rates (doubling times < 3 days), multipotentiality, and potential neurogenic differentiation (more than 60% neurons). Moreover, bioengineering studies have focused on controlling culture conditions in suspension bioreactors including inoculation, hydrodynamics of culture, oxygen and nutrients transfer to the cells, monitoring in situ physiological parameters using process control techniques, and expansion for extended periods of time. In addition, in vitro and in vivo characterization of hNPCs have been performed, providing information on stem/progenitor cell characteristics, cell surface analysis, and appropriate type of cells to use in transplantation studies.

Detection and determination of hydrodynamic properties in a bio-hydrogen production reactor

The Bed Pressure Fluctuation Analysis (PFA) and dual electrical resistivity probe methods were used to investigate the hydrodynamic properties in a bioreactor. It was found that the dominant frequency and side frequency signals were not obvious from Hydraulic Retention Time (HRT) 4 to 0.5 h on the power spectrum diagram when using condensed molasses fermentation soluble (CMS) as the substrate in a biohydrogen production reactor. The start-up testing and online monitoring of the bed pressure fluctuation in a pilot system with HRT 12 h was also investigated. The pressure fluctuation analysis method established a hydrodynamic behavior diagram that was effective in determining flow regime of biogas in large-scale bioreactors. Finally, the study found that a mathematical model built using MATLAB to calculate and simulate the dynamic behavior of bubbles in a biological hydrogen production reactor satisfactorily. The bubble rise velocity and bubble size increased from 0.7 to 1.5 cm/s and 0.2 to 1.9 × 10 −6 cm respectively when the biogas production rate was increased from 30 to 70 mL/min in the biohydrogen production reactor.

A two‐compartment bioreactor system made of commercial parts for bioprocess scale‐down studies: Impact of oscillations on Bacillus subtilis fed‐batch cultivations

This study describes an advanced version of a two-compartment scale-down bioreactor that simulates inhomogeneities present in large-scale industrial bioreactors on the laboratory scale. The system is made of commercially available parts and is suitable for sterilization with steam. The scale-down bioreactor consists of a usual stirred tank bioreactor (STR) and a plug flow reactor (PFR) equipped with static mixer modules. The PFR module with a working volume of 1.2 L is equipped with five sample ports, and pH and dissolved oxygen (DO) sensors. The concept was applied using the non-sporulating Bacillus subtilis mutant strain AS3, characterized by a SpoIIGA gene knockout. In a fed-batch process with a constant feed rate, it is found that oscillating substrate and DO concentration led to diminished glucose uptake, ethanol formation and an altered amino acid synthesis. Sampling at the PFR module allowed the detection of dynamics at different concentrations of intermediates, such as pyruvic acid, lactic acid and amino acids. Results indicate that the carbon flux at excess glucose and low DO concentrations is shifted towards ethanol formation. As a result, the reduced carbon flux entering the tricarboxylic acid cycle is not sufficient to support amino acid synthesis following the oxaloacetic acid branch point.

Glycerol utilisation for the production of chemicals: Conversion to succinic acid, a combined experimental and computational study

An effective method for the valorisation of the main by-product of biodiesel production, i.e. glycerol is investigated in this work. It involves the biological conversion of glycerol to succinic acid, a top added-value material, which can be used as a building block for the production of various commodity and specialty chemicals. Our aim is to give new insights into this bioprocess, which has so far received little attention and is open for further investigation, through a combination of experimental and computational studies. The microorganism employed here was Actinobacillus succinogenes in batch bioreactors where glycerol was used as the sole carbon source. The highest obtained product yield, final succinate concentration and productivity were found to be equal to 1.23 g-succinate/g-glycerol, 29.3 g-succinate/L and 0.27 g-succinate/L/h, respectively. Furthermore, an unstructured model of the batch experiments was developed by considering both substrate and product inhibition. Kinetic parameters of the model were estimated by minimising the difference between experimental and predicted values. The corresponding optimisation problem was solved by using a combination of stochastic and deterministic methodologies, with the goal to probabilistically compute global minima and the resulting parameter values. The model developed can be utilised to successfully predict the concentration profiles of the five most important state variables (biomass, glycerol, succinic acid, formic acid, and acetic acid) with different initial glycerol concentrations. Scaled-up experiments in larger-scale bioreactors were used for further validation purposes. Our model can be further used to compute optimal operating/parametric conditions, which maximise yield, productivity and/or the final succinic acid concentration.

The potential of hydrodynamic damage to animal cells of industrial relevance: current understanding.

Suspension animal cell culture is now routinely scaled up to bioreactors on the order of 10,000L, and greater, to meet commercial demand. However, the concern of the 'shear sensitivity' of animal cells still remains, not only within the bioreactor, but also in the downstream processing. As the productivities continue to increase, titer of ~10g/L are now reported with cell densities greater than 2×10(7)cells/mL. Such high, and potentially higher cell densities will inevitably translate to increased demand in mass transfer and mixing. In addition, achieving productivity gains in both the upstream stage and downstream processes can subject the cells to aggressive environments such as those involving hydrodynamic stresses. The perception of 'shear sensitivity' has historically put an arbitrary upper limit on agitation and aeration in bioreactor operation; however, as cell densities and productivities continue to increase, mass transfer requirements can exceed those imposed by these arbitrary low limits. Therefore, a better understanding of how animal cells, used to produce therapeutic products, respond to hydrodynamic forces in both qualitative and quantitative ways will allow an experimentally based, higher, "upper limit" to be created to guide the design and operation of future commercial, large scale bioreactors. With respect to downstream hydrodynamic conditions, situations have already been achieved in which practical limits with respect to hydrodynamic forces have been experienced. This review mainly focuses on publications from both the academy and industry regarding the effect of hydrodynamic forces on industrially relevant animal cells, and not on the actual scale-up of bioreactors. A summary of implications and remaining challenges will also be presented.

Simulation of dissolved CO2 gradients in a scale‐down system: A metabolic and transcriptional study of recombinant Escherichia coli

Deficient mixing in industrial-scale bioreactors is an important concern as it results in a heterogeneous environment that may affect microbial cell physiology. Dissolved carbon dioxide (dCO(2) ) fluctuations, which can occur in large-scale bioreactors, were simulated for the first time and their effects were evaluated on Escherichia coli expressing recombinant green fluorescent protein (GFP). The dCO(2) gradients were simulated by continuously circulating the medium between two vessels of a scale-down system to mimic mean circulation times (t(c) ) of 50, 170, and 375 s. Specific growth rate (μ) decreased by 11% and acetate concentration increased by 23% at the highest t(c) compared to reference cultures. An increase in the time needed for attaining maximum GFP concentration was also observed. The effect of dCO(2) fluctuations on the transcriptional levels of genes involved in the glutamate decarboxylase (gadA and gadC) and α-ketoglutarate dehydrogenase (sucA and sucB) were analyzed by quantitative real time PCR. Such genes are known to be highly over- or underexpressed at elevated constant dCO(2) . Expression levels of gadA and gadC increased up to 60% and 72%, and sucA decreased 1.8-fold in the culture performed at the highest t(c) . Only a minor decrease of sucB expression was observed at t(c) of 170 and 375 s. Although exposure to continuous high dCO(2) can affect culture performance, in this work it was shown that E. coli is able to rescue its metabolism in very short times when cells are intermittently returned to low dCO(2) conditions after being exposed to high dCO(2) .

Phenotypic and functional characterization of human bone marrow stromal cells in hollow-fibre bioreactors

The transplantation of human bone marrow stromal cells (BMSCs) is a novel immunotherapeutic approach that is currently being explored in many clinical settings. Evidence suggests that the efficacy of cell transplantation is directly associated with soluble factors released by human BMSCs. In order to harness these secreted factors, we integrated BMSCs into large-scale hollow-fibre bioreactor devices in which the cells, separated by a semipermeable polyethersulphone (PES) membrane, can directly and continuously release therapeutic factors into the blood stream. BMSCs were found to be rapidly adherent and exhibited long-term viability on PES fibres. The cells also preserved their immunophenotype under physiological fluid flow rates in the bioreactor, and exhibited no signs of differentiation during device operation, but still retained the capacity to differentiate into osteoblastic lineages. BMSC devices released growth factors and cytokines at comparable levels on a per-cell basis to conventional cell culture platforms. Finally, we utilized a potency assay to demonstrate the therapeutic potential of the collected secreted factors from the BMSC devices. In summary, we have shown that culturing BMSCs in a large-scale hollow-fibre bioreactor is feasible without deleterious effects on phenotype, thus providing a platform for collecting and delivering the paracrine secretions of these cells.

Time‐resolved selected ion flow tube mass spectrometric quantification of the volatile compounds generated by E. coli JM109 cultured in two different media

Preliminary measurements have been made of the volatile compounds emitted by the bacterium E. coli JM109 cultured in the commonly used media Dulbecco's modified Eagle's medium (DMEM) and lysogeny broth (LB) using selected ion flow tube mass spectrometry, SIFT-MS, as a step towards the real time, non-invasive monitoring of accidental infections of mammalian cell cultures. In one procedure, the culture medium alone and the E. coli cells/medium combination were held at 37 °C in bottles sealed with septa for a given time period, usually overnight, to allow the bacterium to proliferate, after which the captured headspace was analysed directly by SIFT-MS. Several compounds were seen to be produced by the E. coli cells that depended on the liquid medium used: when cultured in DMEM, copious amounts of ethanol, acetaldehyde and hydrogen sulphide were produced; in LB ammonia is the major volatile product. In a second procedure, to ensure aerobic conditions prevailed in the cell culture, selected volatile compounds were monitored by SIFT-MS in real time for several hours above the open-to-air E. coli/DMEM culture held at close to 37 °C. The temporal variations in the concentrations of some compounds, which reflect their production rates in the culture, indicate maxima. Thus, the maxima in the ethanol and acetaldehyde production are a reflection of the reduction of glucose from the DMEM by the vigorous E. coli cells and the maximum in the hydrogen sulphide level is an indication of the loss of the sulphur-bearing amino acids from the DMEM. Serendipitously, emissions from DMEM inadvertently infected with the bacterium C. testosteroni were observed when large quantities of ammonia were seen to be produced. The results of this preliminary study suggest that monitoring volatile compounds might assist in the early detection of bacterial infection in large-scale bioreactors.

Clinical-Grade Generation of Active NK Cells from Cord Blood Hematopoietic Progenitor Cells for Immunotherapy Using a Closed-System Culture Process

Natural killer (NK) cell-based adoptive immunotherapy is a promising treatment approach for many cancers. However, development of protocols that provide large numbers of functional NK cells produced under GMP conditions are required to facilitate clinical studies. In this study, we translated our cytokine-based culture protocol for ex vivo expansion of NK cells from umbilical cord blood (UCB) hematopoietic stem cells into a fully closed, large-scale, cell culture bioprocess. We optimized enrichment of CD34+ cells from cryopreserved UCB units using the CliniMACS system followed by efficient expansion for 14 days in gas-permeable cell culture bags. Thereafter, expanded CD34+ UCB cells could be reproducibly amplified and differentiated into CD56+CD3− NK cell products using bioreactors with a mean expansion of more than 2,000 fold and a purity of >90%. Moreover, expansion in the bioreactor yielded a clinically relevant dose of NK cells (mean: 2×109 NK cells), which display high expression of activating NK receptors and cytolytic activity against K562. Finally, we established a versatile closed washing procedure resulting in optimal reduction of medium, serum and cytokines used in the cell culture process without changes in phenotype and cytotoxic activity. These results demonstrate that large numbers of UCB stem cell-derived NK cell products for adoptive immunotherapy can be produced in closed, large-scale bioreactors for the use in clinical trials.

Production of leucine amino peptidase in lab scale bioreactors using Streptomyces gedanensis

Studies were conducted on the production of leucine amino peptidase (LAP) by Streptomyces gedanensis to ascertain the performance of the process in shake flask, parallel fermenter and 5-L fermenter utilizing soy bean meal as the carbon source. Experiments were conducted to analyze the effects of aeration and agitation rate on cell growth and LAP production. The results unveiled that an agitation rate of 300rpm, 50% dissolved oxygen (DO) upholding and 0.15vvm strategies were the optimal for the enzyme production, yielding 22.72±0.11IU/mL LAP in parallel fermenter which was comparable to flask level (24.65±0.12IU/mL LAP) fermentation. Further scale-up, in 5-L fermenter showed 50% DO and 1vvm aeration rate was the best, producing optimum and the production was 20.09±0.06IU/mL LAP. The information obtained could be useful to design a strategy to improve a large-scale bioreactor cultivation of cells and production of LAP.

Perfusion Circuit Concepts for Hollow-Fiber Bioreactors Used as in Vitro Cell Production Systems or Ex Vivo Bioartificial Organs

For the development and implementation of primary human cell- and stem cell-based applications in regenerative medicine, large amounts of cells with well-defined characteristics are needed. Such cell quantities can be obtained with the use of hollow fiber-based bioreactors. While the use of such bioreactors generally requires a perfusion circuit, the configuration and complexity of such circuits is still in debate. We evaluated various circuit configurations to investigate potential perfusate volume shifts in the arterial and venous sides of the perfusion circuit, as well as in the feed and waste lines. Volume shifts with changes in flow conditions were measured with graduated bubble traps in the circuit, and perfusion pressures were measured at three points in the circuits. The results of this study demonstrate that the bioreactor perfusion circuit configuration has an effect on system pressures and volume shifts in the circuit. During operation, spikes in post-bioreactor pressures caused detrimental, potentially dangerous volume shifts in the feed and waste lines for configurations that lacked feed pumps and/or waste line check valves. Our results indicate that a more complex tubing circuit adds to safety of operation and avoids technical challenges associated with the use of large-scale hollow fiber bioreactors (e.g., for extracorporeal liver support or erythrocyte production from hematopoietic stem cells), including volume shifts and the need for a large reservoir. Finally, to ensure safe use of bioreactors, measuring pre-, intra-, and post-bioreactor pressures, and pump operation control is also advisable, which suggests the use of specifically developed bioreactor perfusion devices.

A simplified polyethylenimine-mediated transfection process for large-scale and high-throughput applications

Transient gene expression in mammalian cells is a valuable alternative to stable cell lines for the rapid production of large amounts of recombinant proteins. While the establishment of stable cell lines takes 2–6months, milligram amounts of protein can be obtained within a week following transfection. The polycation polyethylenimine (PEI) is one of the most utilized reagents for small- to large-scale transfections as it is simple to use and, when combined with optimized expression vectors and cell lines, provides high transfection efficiency and titers. As with most transfection reagents, PEI-mediated transfection involves the formation of nanoparticles (polyplexes) which are obtained by its mixing with plasmid DNA. A short incubation period that allows polyplexes to reach their optimal size is performed prior to their addition to the culture. As the quality of polyplexes directly impacts transfection efficiency and productivity, their formation complicates scalability and automation of the process, especially when performed in large-scale bioreactors or small-scale high-throughput formats. To avoid variations in transfection efficiency and productivity that arise from polyplexes formation step, we have optimized the conditions for their creation directly in the culture by the consecutive addition of DNA and PEI. This simplified approach is directly transferable from suspension cultures grown in 6-well plates to shaker flasks and 5-L WAVE bioreactors. As it minimizes the number of steps and does not require an incubation period for polyplex formation, it is also suitable for automation using static cultures in 96-well plates. This “direct” transfection method thus provides a robust platform for both high-throughput expression and large-scale production of recombinant proteins.

A test facility for fritted spargers of production-scale-bioreactors

The production of therapeutic proteins requires qualification of equipment components and appropriate validation procedures for all operations. Since protein productions are typically performed in bioreactors using aerobic cultivation processes air sparging is an essential factor. As recorded in literature, besides ring spargers and open pipe, sinter frits are often used as sparging elements in large scale bioreactors. Due to the manufacturing process these frits have a high lot-to-lot product variability. Experience shows this is a practical problem for use in production processes of therapeutic proteins, hence frits must be tested before they can be employed. The circumstance of checking quality and performance of frits as sparging elements was investigated and various possibilities have been compared. Criteria have been developed in order to evaluate the sparging performance under conditions comparable to those in production bioreactors. The oxygen mass transfer coefficient (k ( L ) a) was chosen as the evaluation criterion. It is well known as an essential performance measure for fermenters in the monoclonal antibody production. Therefore a test rig was constructed able to automatically test frit-spargers with respect to their k ( L ) a-values at various gas throughputs. Performance differences in the percent range could be detected.