Production and scale‐up of a monoclonal antibody against 17‐hydroxyprogesterone

The hybridoma 192 was used to produce a monoclonal antibody (MAb) against 17‐hydroxyprogesterone (17‐OHP), for possible use in screening for congenital adrenal hyperplasia (CAH). The factors influencing the MAb production were screened and optimized in a 2 L stirred bioreactor. The production was then scaled up to a 20 L bioreactor. All of the screened factors (aeration rate, stirring speed, dissolved oxygen concentration, pH, and temperature) were found to significantly affect production. Optimization using the response surface methodology identified the following optimal production conditions: 36.8°C, pH 7.4, stirring speed of 100 rpm, 30% dissolved oxygen concentration, and an aeration rate of 0.09 vvm. Under these conditions, the maximum viable cell density achieved was 1.34 ± 0.21 × 10⁶ cells mL^?1 and the specific growth rate was 0.036 ± 0.004 h^?1. The maximum MAb titer was 11.94 ± 4.81 μg mL^?1 with an average specific MAb production rate of 0.273 ± 0.135 pg cell^?1 h^?1. A constant impeller tip speed criterion was used for the scale‐up. The specific growth rate (0.040 h^?1) and the maximum viable cell density (1.89 × 10⁶ cells mL^?1) at the larger scale were better than the values achieved at the small scale, but the MAb titer in the 20 L bioreactor was 18% lower than in the smaller bioreactor. A change in the culture environment from the static conditions of a T‐flask to the stirred bioreactor culture did not affect the specificity of the MAb toward its antigen (17‐OHP) and did not compromise the structural integrity of the MAb. © 2012 American Institute of Chemical Engineers Biotechnol. Prog., 2013     

Caveolin‐1 down‐regulation is required for Wnt5a‐Frizzled 2 signalling in Ha‐RasV12‐induced cell transformation

Caveolin‐1 (Cav1) is down‐regulated during MK4 (MDCK cells harbouring inducible Ha‐Ras^V12 gene) transformation by Ha‐Ras^V12. Cav1 overexpression abrogates the Ha‐Ras^V12‐driven transformation of MK4 cells; however, the targeted down‐regulation of Cav1 is not sufficient to mimic this transformation. Cav1‐silenced cells, including MK4/shCav1 cells and MDCK/shCav1 cells, showed an increased cell area and discontinuous junction‐related proteins staining. Cellular and mechanical transformations were completed when MDCK/shCav1 cells were treated with medium conditioned by MK4 cells treated with IPTG (MK4+I‐CM) but not with medium conditioned by MK4 cells. Nanoparticle tracking analysis showed that Ha‐Ras^V12‐inducing MK4 cells increased exosome‐like microvesicles release compared with their normal counterparts. The cellular and mechanical transformation activities of MK4+I‐CM were abolished after heat treatment and exosome depletion and were copied by exosomes derived from MK4+I‐CM (MK4+I‐EXs). Wnt5a, a downstream product of Ha‐Ras^V12, was markedly secreted by MK4+I‐CM and MK4+I‐EXs. Suppression of Wnt5a expression and secretion using the porcupine inhibitor C59 or Wnt5a siRNA inhibited the Ha‐Ras^V12‐ and MK4+I‐CM‐induced transformation of MK4 cells and MDCK/shCav1 cells, respectively. Cav1 down‐regulation, either by Ha‐Ras^V12 or targeted shRNA, increased frizzled‐2 (Fzd2) protein levels without affecting its mRNA levels, suggesting a novel role of Cav1 in negatively regulating Fzd2 expression. Additionally, silencing Cav1 facilitated the internalization of MK4+I‐EXs in MDCK cells. These data suggest that Cav1‐dependent repression of Fzd2 and exosome uptake is potentially relevant to its antitransformation activity, which hinders the activation of Ha‐Ras^V12‐Wnt5a‐Stat3 pathway. Altogether, these results suggest that both decreasing Cav1 and increasing exosomal Wnt5a must be implemented during Ha‐Ras^V12‐driven cell transformation.     

Microwell engineering characterization for mammalian cell culture process development

Experimentation in shaken microplate formats offers a potential platform technology for the rapid evaluation and optimization of cell culture conditions. Provided that cell growth and antibody production kinetics are comparable to those found in currently used shake flask systems then the microwell approach offers the possibility to obtain early process design data more cost effectively and with reduced material requirements. This work describes a detailed engineering characterization of liquid mixing and gas–liquid mass transfer in microwell systems and their impact on suspension cell cultures. For growth of murine hybridoma cells producing IgG1, 24‐well plates have been characterized in terms of energy dissipation (P/V) (via Computational Fluid Dynamics, CFD), fluid flow, mixing and oxygen transfer rate as a function of shaking frequency and liquid fill volume. Predicted k_La values varied between 1.3 and 29 h^?1; liquid‐phase mixing time, quantified using iodine decolorization experiments, varied from 1.7 s to 3.5 h; while the predicted P/V ranged from 5 to 35 W m^?3. CFD simulations of the shear rate predicted hydrodynamic forces will not be detrimental to cells. For hybridoma cultures however, high shaking speeds (>250 rpm) were shown to have a negative impact on cell growth, while a combination of low shaking speed and high well fill volume (120 rpm, 2,000 µL) resulted in oxygen limited conditions. Based on these findings a first engineering comparison of cell culture kinetics in microwell and shake flask formats was made at matched average energy dissipation rates. Cell growth kinetics and antibody titer were found to be similar in 24‐well microtiter plates and 250 mL shake flasks. Overall this work has demonstrated that cell culture performed in shaken microwell plates can provide data that is both reproducible and comparable to currently used shake flask systems while offering at least a 30‐fold decrease in scale of operation and material requirements. Linked with automation this provides a route towards the high throughput evaluation of robust cell lines under realistic suspension culture conditions. Biotechnol. Bioeng. 2010; 105: 260–275. © 2009 Wiley Periodicals, Inc.     

NaCS‐PDMDAAC immobilized cultivation of recombinant Dictyostelium discoideum for soluble human Fas ligand production

Dictyostelium discoideum is a promising eukaryotic host for the expression of heterologous proteins requiring post‐translational modifications. However, the dilute nature of D. discoideum cell culture limits applications for high value proteins production. D. discoideum cells, entrapped in sodium cellulose sulfate/poly‐dimethyl‐diallyl‐ammonium chloride (NaCS‐PDMDAAC) capsules were used for biosynthesis of the heterologous protein, soluble human Fas ligand (hFasL). Semi‐continuous cultivations with capsules recycling were carried out in shake flasks. Also, a scaled‐up cultivation of immobilized D. discoideum for hFasL production in a customized vitreous airlift bioreactor was conducted. The results show that NaCS‐PDMDAAC capsules have desirable biophysical properties including biocompatibility with the D. discoideum cells and good mechanical stability throughout the duration of cultivation. A maximum cell density of 2.02 × 10⁷ cells mL^?1 (equivalent to a maximum cell density of 2.22 × 10⁸ cells mL^?1 in capsules) and a hFasL concentration of 130.40 μg L^?1 (equivalent to a hFasL concentration of 1434.40 μg L^?1 in capsules) were obtained in shake flask cultivation with capsules recycling. Also, a maximum cell density of 1.72 × 10⁷cells mL^?1 (equivalent to a maximum cell density of 1.89 × 10⁸ cells mL^?1 in capsules) and a hFasL concentration of 106.10 μg L^?1 (equivalent to a hFasL concentration of 1167.10 μg L^?1 in capsules) were obtained after ～170 h cultivation in the airlift bioreactor (with a working volume of 200 mL in a 315 mL bioreactor). As the article presents a premier work in the application of NaCS‐PDMDAAC immobilized D. discoideum cells for the production of hFasL, more work is required to further optimize the system to generate higher cell densities and hFasL titers for large‐scale applications. © 2014 American Institute of Chemical Engineers Biotechnol. Prog., 31:424–430, 2015     

Demonstrating the Manufacture of Human CAR‐T Cells in an Automated Stirred‐Tank Bioreactor

Chimeric antigen receptor T‐cell (CAR‐T) therapies have proven clinical efficacy for the treatment of hematological malignancies. However, CAR‐T cell therapies are prohibitively expensive to manufacture. The authors demonstrate the manufacture of human CAR‐T cells from multiple donors in an automated stirred‐tank bioreactor. The authors successfully produced functional human CAR‐T cells from multiple donors under dynamic conditions in a stirred‐tank bioreactor, resulting in overall cell yields which were significantly better than in static T‐flask culture. At agitation speeds of 200 rpm and greater (up to 500 rpm), the CAR‐T cells are able to proliferate effectively, reaching viable cell densities of >5 × 10⁶ cells ml‐1 over 7 days. This is comparable with current expansion systems and significantly better than static expansion platforms (T‐flasks and gas‐permeable culture bags). Importantly, engineered T‐cells post‐expansion retained expression of the CAR gene and retained their cytolytic function even when grown at the highest agitation intensity. This proves that power inputs used in this study do not affect cell efficacy to target and kill the leukemia cells. This is the first demonstration of human CAR‐T cell manufacture in stirred‐tank bioreactors and the findings present significant implications and opportunities for larger‐scale allogeneic CAR‐T production.     

Epoxidation of 1,7‐octadiene by Pseudomonas oleovorans in a membrane bioreactor

A growing cell culture of Pseudomonas oleovorans was used to biotransform 1,7‐octadiene to 1,2‐epoxy‐7,8‐octene in a continuous‐flow bioreactor with an external membrane module. A dense silicone rubber membrane was used to contact an organic phase, containing both the reactant (1,7‐octadiene) and the growth substrate (heptane), with an aqueous biomedium phase containing the biocatalyst. Heptane and octadiene delivery to the aqueous phase, and epoxide extraction into the solvent, occurred by diffusion across the dense membrane under a concentration‐driving force. In addition, a liquid feed of heptane and octadiene was pumped directly into the bioreactor to increase the rate of delivery of these compounds to the aqueous phase. In this system 1,2‐epoxy‐7,8‐octene accumulated in a pure solvent phase, thus, product recovery problems associated with emulsion formation were avoided. Furthermore, no phase breakthrough of either liquid across the membrane was observed. In this system, the highest volumetric productivity obtained was 30 U.L⁻¹, and this was achieved at a dilution rate of 0.07 h⁻¹, 70 m².m⁻³ of membrane area, and a steady‐state biomass concentration of 2.5 g.L⁻¹. The system was stable for over 1250 h. Decreasing the dilution rate led to an increased biomass concentration, however, the specific activity was significantly reduced, and therefore, an optimal dilution rate was determined at 0.055 h⁻¹. © 1999 John Wiley & Sons, Inc. Biotechnol Bioeng 63: 601–611, 1999.     

Process optimization of the integrated synthesis and secretion of ectoine and hydroxyectoine under hyper/hypo‐osmotic stress

The synthesis and secretion of the industrial relevant compatible solutes ectoine and hydroxyectoine using the halophile bacterium Chromohalobacter salexigens were studied and optimized. For this purpose, a cascade of two continuously operated bioreactors was used. In the first bioreactor, cells were grown under constant hyperosmotic conditions and thermal stress driving the cells to accumulate large amounts of ectoines. To enhance the overall productivity, high cell densities up to 61 g L^?1 were achieved using a cross‐flow ultrafiltration connected to the first bioreactor. In the coupled second bioreactor the concentrated cell broth was subjected to an osmotic and thermal down‐shock by addition of fresh distilled water. Under these conditions, the cells are forced to secrete the accumulated intracellular ectoines into the medium to avoid bursting. The cultivation conditions in the first bioreactor were optimized with respect to growth temperature and medium salinity to reach the highest synthesis (productivity); the second bioreactor was optimized using a multi‐objective approach to attain maximal ectoine secretion with simultaneous minimization of cell death and product dilution caused by the osmotic and thermal down‐shock. Depending on the cultivation conditions, intracellular ectoine and hydroxyectoine contents up to 540 and 400 mg per g cell dry weight, respectively, were attained. With a maximum specific growth rate of 0.3 h^?1 in defined medium, productivities of approximately 2.1 g L^?1 h^?1 secreted ectoines in continuous operation were reached. Biotechnol. Bioeng. 2010;107: 124–133. © 2010 Wiley Periodicals, Inc.     

Strain engineering for high‐level 5‐aminolevulinic acid production in Escherichia coli

Herein, we report the development of a microbial bioprocess for high‐level production of 5‐aminolevulinic acid (5‐ALA), a valuable non‐proteinogenic amino acid with multiple applications in medical, agricultural, and food industries, using Escherichia coli as a cell factory. We first implemented the Shemin (i.e., C4) pathway for heterologous 5‐ALA biosynthesis in E. coli. To reduce, but not to abolish, the carbon flux toward essential tetrapyrrole/porphyrin biosynthesis, we applied clustered regularly interspersed short palindromic repeats interference (CRISPRi) to repress hemB expression, leading to extracellular 5‐ALA accumulation. We then applied metabolic engineering strategies to direct more dissimilated carbon flux toward the key precursor of succinyl‐CoA for enhanced 5‐ALA biosynthesis. Using these engineered E. coli strains for bioreactor cultivation, we successfully demonstrated high‐level 5‐ALA biosynthesis from glycerol (~30 g L^?1) under both microaerobic and aerobic conditions, achieving up to 5.95 g L^?1 (36.9% of the theoretical maximum yield) and 6.93 g L^?1 (50.9% of the theoretical maximum yield) 5‐ALA, respectively. This study represents one of the most effective bio‐based production of 5‐ALA from a structurally unrelated carbon to date, highlighting the importance of integrated strain engineering and bioprocessing strategies to enhance bio‐based production.     

Aerobic biodegradation of a mixture of sulfonated azo dyes by a bacterial consortium immobilized in a two‐stage sparged packed‐bed biofilm reactor

The biodegradation of the sulfonated azo dyes, Acid Orange 7 (AO7) and Acid Red 88 (AR88), by a bacterial consortium isolated from water and soil samples obtained from sites receiving discharges from textile industries, was evaluated. For a better removal of azo dyes and their biodegradation byproducts, an aerobically operated two‐stage rectangular packed‐bed biofilm reactor (2S‐RPBR) was constructed. Because the consortium's metabolic activity is affected by oxygen, the effect of the interstitial air flow rate Q_GI on 2S‐RPBR's zonal values of the oxygen mass transfer coefficient k_La was estimated. In the operational conditions probed in the bioreactor, the k_La values varied from 3 to 60 h^?1, which roughly correspond to volumetric oxygen transfer rates, dc_L/dt, ranging from 20 to 375 mg O₂ L^?1h^?1. Complete biodegradation of azo dyes was attained at loading rates B_V,AZ up to 40 mg L^?1d^?1. At higher B_V,AZ values (80 mg L^?1 d^?1), dye decolorization and biodegradation of the intermediaries 4‐amino‐naphthalenesulphonic acid (4‐ANS) and 1‐amino‐2‐naphthol (1‐A2N) was almost complete. However, a diminution in COD and TOC removal efficiencies was observed in correspondence to the 4‐aminobenzenesulfonic acid (4‐ABS) accumulation in the bioreactor. Although the oxygen transport rate improved the azo dye mineralization, the results suggest that the removal efficiency of azo dyes was affected by biofilm detachment at relatively high Q_GI and B_V,AZ values. After 225 days of continuous operation of the 2S‐RFBR, eight bacterial strains were isolated from the biofilm attached to the porous support. The identified genera were: Arthrobacter, Variovorax, Agrococcus, Sphingomonas, Sphingopyxis, Methylobacterium, Mesorhizobium, and Microbacterium.     

Shear stress effects on cell growth and <Emphasis Type="SmallCaps">L</Emphasis>-DOPA production by suspension culture of <Emphasis Type="Italic">Stizolobium hassjoo</Emphasis> cells in an agitated bioreactor

Suspension cultures of Stizolobium hassjoo cells were cultivated in a 7l bioreactor. The growth rate and intracellular L-DOPA content of the cells using two different turbine impellers were compared. There were distinct differences in growth behavior and L-DOPA productivity in the range of 100 to 500 rpm for flat-blade turbine impeller. Disk turbine retarded significantly the cell growth but not so significantly for L-DOPA production in the range of 200 to 300 rpm. The shear force intensity of the two impellers at various rotational rates was compared with shear force index (SFI), and power input per unit mass and eddy length scale. There was good consistency among the three indexes for shear force intensity. Thus with SFI the shear force intensity of bioreactor can be indirectly estimated. A critical shear stress that may cause sublytic effect in cells was identified for flat-blade turbine operated at 400 rpm. The common effect between the shear stress and the proton elicitation in the bioreactor was elucidated with a hypothesis of signal transduction by second messenger, H⁺. Our results suggested that H⁺ transduced the signal to protoplast when S. hassjoo cells were stimulated by shear stress. This resulted in an increase of H⁺ which triggered a similar reaction to the pH control of culture broth and enhanced the L-DOPA production.     

A Pdgf‐cCreERT2 knock‐in mouse model for tracing PDGF‐C cell lineages during development

PDGF‐C, a member of the platelet‐derived growth factor (PDGF) family, plays important roles in the development of craniofacial structures, the neural system, the vascular system, and tumors. PDGF‐C could also be required for the regulation of certain types of stem or progenitor cells as suggested by its expression in the regions where these cells are located. To further characterize the role of PDGF‐C in development, we generated a Pdgf‐c^CreERT2 mouse strain, in which a tamoxifen‐inducible Cre (CreERT2) cDNA was specifically targeted into the Pdgf‐c genomic locus and controlled by the endogenous Pdgf‐c regulatory elements. We also showed that Cre activity in this mouse strain could be specifically induced by tamoxifen, which allowed the fate of PDGF‐C‐expressing cells to be traced at various stages of development. Using this model system, we demonstrated for the first time that PDGF‐C‐expressing cells could be multipotent, generating multiple cell lineages required for the formation of the cerebellum. Therefore, the Pdgf‐c^CreERT2 mouse strain generated in this study will be a valuable transgenic tool for exploring the function of PDGF‐C in development and stem cell biology.     

Optimization of the Process for the Production of L(+)‐Lactic Acid from Cull Potato by Rhizopus oryzae

Cull potato is currently an under‐utilized biomass in the potato processing states of the USA. L(+)‐Lactic acid production by three Rhizopus strains and one homofermentative, facultative anaerobic Lactobacillus amylophilus strain was investigated using potatoes as the sole nutrient supply in the culture medium. Rhizopus oryzae NRRL 395 was chosen as the strain for further studies because it showed the highest lactate yield. The fermentation conditions for seed cultures were studied for three treatment structures using a completely randomized design. Optimum conditions for the seed culture were determined to be 2 % potato medium, 10⁴ spores/mL concentration, and 24 h of fermentation. Plackett‐Burman and central composite designs were used to screen and optimize the factors for lactic acid production. Substrate (potato) concentration, fermentation temperature, and shaking speed were found to be the most significant factors affecting both the yield and concentration of lactate. Optimum values for substrate concentration, fermentation temperature, and shaking speed were 10 %, 27 °C, and 170 rpm, respectively. Under these optimum conditions, the lactate concentration was predicted by the model to be 35.5 g/L, which was verified by the experimental data (33.3 g/L). The results indicate that cull potato can be an effective feedstock for R. ryzae NRRL 395 in the production of lactic acid.     

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     

The caveolin‐3 P104L mutation in LGMD‐1C patients inhibits non‐insulin‐stimulated glucose metabolism and growth but promotes myocyte proliferation

The caveolin‐3 (CAV3) protein is known to be specifically expressed in various myocytes, and skeletal muscle consumes most of the blood glucose as an energy source to maintain normal cell metabolism and function. The P104L mutation in the coding sequence of the human CAV3 gene leads to autosomal dominant disease limb‐girdle muscular dystrophy type 1C (LGMD‐1C). We previously reported that C2C12 cells transiently transfected with the P104L CAV3 mutant exhibited decreased glucose uptake and glycogen synthesis after insulin stimulation. The present study aimed to examine whether the P104L mutation affects C2C12 cell glucose metabolism, growth, and proliferation without insulin stimulation. C2C12 cells stably transfected with CAV3‐P104L were established, and biochemical assays, western blot analysis and confocal microscopy were used to observe glucose metabolism as well as cell growth and proliferation and to determine the effect of the P104L mutation on the PI3K/Akt signaling pathway. Without insulin stimulation, C2C12 cells stably transfected with the P104L CAV3 mutant exhibited decreased glucose uptake and glycogen synthesis, decreased CAV3 expression and reduced localization of CAV3 and GLUT4 on the cell membrane. The P104L mutant significantly reduced the cell diameters, but accelerated cell proliferation. Akt phosphorylation was inhibited, and protein expression of GLUT4, p‐GSK3β, and p‐p70s6K, which are molecules downstream of Akt, was significantly decreased. The CAV3‐P104L mutation inhibits glycometabolism and cell growth but accelerates C2C12 cell proliferation by reducing CAV3 protein expression and cell membrane localization, which may contribute to the pathogenesis of LGMD‐1C.     

Protein profile of basal prostate epithelial progenitor cells—stage‐specific embryonal antigen 4 expressing cells have enhanced regenerative potential in vivo

The long‐term propagation of basal prostate progenitor cells ex vivo has been very difficult in the past. The development of novel methods to expand prostate progenitor cells in vitro allows determining their cell surface phenotype in greater detail. Mouse (Lin^?Sca‐1⁺ CD49f⁺ Trop2^high‐phenotype) and human (Lin^? CD49f⁺ TROP2^high) basal prostate progenitor cells were expanded in vitro. Human and mouse cells were screened using 242 anti‐human or 176 antimouse monoclonal antibodies recognizing the cell surface protein profile. Quantitative expression was evaluated at the single‐cell level using flow cytometry. Differentially expressed cell surface proteins were evaluated in conjunction with the known CD49f⁺/TROP2^high phenotype of basal prostate progenitor cells and characterized by in vivo sandwich‐transplantation experiments using nude mice. The phenotype of basal prostate progenitor cells was determined as CD9⁺/CD24⁺/CD29⁺/CD44⁺/CD47⁺/CD49f⁺/CD104⁺/CD147⁺/CD326⁺/Trop2^high of mouse as well as human origin. Our analysis revealed several proteins, such as CD13, Syndecan‐1 and stage‐specific embryonal antigens (SSEAs), as being differentially expressed on murine and human CD49f⁺ TROP2⁺ basal prostate progenitor cells. Transplantation experiments suggest that CD49f⁺ TROP2^high SSEA‐4^high human prostate basal progenitor cells to be more potent to regenerate prostate tubules in vivo as compared with CD49f⁺ TROP2^high or CD49f⁺ TROP2^high SSEA‐4^low cells. Determination of the cell surface protein profile of functionally defined murine and human basal prostate progenitor cells reveals differentially expressed proteins that may change the potency and regenerative function of epithelial progenitor cells within the prostate. SSEA‐4 is a candidate cell surface marker that putatively enables a more accurate identification of the basal PESC lineage.