Strategies for high titre plasmid DNA production in Escherichia coli DH5α

The production of plasmid pEGFP-N1 in Escherichia coli DH5α was optimised. A strategy evaluating different media components separately was not successful (OD < 2.5, low plasmid titres), a statistical approach via a Plackett Burman design (11 parameters) allowed some improvement (7 mg/L plasmid, OD₆₀₀ 8.5). Generally, high biomass did not correlate with high plasmid titres. When conditions were transferred to the bioreactor (batch operation) little improvement in plasmid titres (10 mg/L plasmid, OD₆₀₀ 20) was observed. By switching to a fed-batch procedure with linear feeding these values increased to 20 mg/L plasmid (OD₆₀₀ 50). By using an adaptive feeding strategy, plasmid titres could be increased to 50 mg/L. Finally, by combining a growth controlled (reduced temperature (35 °C), low dO₂) initial batch phase with an adaptive feeding strategy in the fed-batch phase (37 °C, glucose-/dO₂-limitation) we were reproducibly able to produce up to 250 mg/L of plasmid DNA in cultures that reached a final OD₆₀₀ of 80.     

Heterologous production of a temperature and pH-stable laccase from Bacillus vallismortis fmb-103 in Escherichia coli and its application

To enhance laccase yield, the laccase gene from Bacillus vallismortis fmb-103 was cloned and heterologously expressed in Escherichia coli BL21 (DE3) cells. The auto-induction strategy was applied during fermentation, and the process was controlled, as follows: Cu²⁺ was added when the optical density at 600 nm (OD₆₀₀) was 0.3, the fermentation temperature was adjusted to 16 °C when the OD₆₀₀ was 0.9, and fermentation was stopped after 50 h. The yield of recombinant laccase was up to 3420 U/L, as assayed by 2,2-azino-bis(3-ethylbenzothiazoline-6-sulfonic acid). Recombinant laccase was purified 4.47-fold by heating for 10 min at 70 °C and dialyzing against 50–60% ammonium sulfate, retained more than 50% activity after 10 h at 70 °C, and demonstrated broad pH stability. Malachite green was efficiently degraded by recombinant laccase, especially in combination with mediators. These results provided a basis for the future application of recombinant laccase to malachite green degradation.     

Production of steviol from steviol glucosides using β-glycosidase from Sulfolobus solfataricus

Steviol is a diterpene isolated from the plant Stevia rebaudiana that has a potential role as an antihyperglycemic agent by stimulating insulin secretion from pancreatic beta cells and also has significant potential to diminish the renal clearance of anionic drugs and their metabolites. In this study, the lacS gene, which encodes a thermostable β-glycosidase (SSbgly) enzyme from the extremely thermoacidophillic archaeon Sulfolobus solfataricus, was cloned and expressed in E. coli Rossetta BL21(DE3)pLyS using lactose as an inducer. Through fermentation, SSbgly was expressed as a 61 kDa protein with activity of 24.3 U/mg and the OD₆₀₀ of 23 was reached after 18 h induction with 10 mM lactose. Purified protein was obtained by Ni-Sepharose chromatography with a yield of 92.3%. SSbgly hydrolyzed steviol glycosides to produce steviol with a yield of 99.2%. The optimum conditions for steviol production were 50 U/ml SSbgly and 90 mg/ml Ste at 75 °C as determined by the response surface method.     

Production of recombinant ghost bacterial vaccine against streptococcal disease of olive flounder

The simple fed-batch fermentation was carried out to produce E. coli XL1-Blue/pHCE-InaN-GAPDH Ghost 37 SDM as a ghost bacterial vaccine (GBV). The fermentation was carried out in four phases of batch fermentation (phase 1), fed-batch fermentation with intermittent feeding strategy (phase 2), thermal induction by temperature increase to 42 °C for the expression of lysis E gene (GBV formation, phase 3) and high temperature holding phase to increase the efficiency of GBV formation (phase 4). After the high temperature holding phase at 47 °C, efficiency of the GBV formation reached 99.7% with the culture OD₆₀₀ of 57.9. The maximum GBV of 22 g dcw/l was obtained. The protective efficacy of GBV was determined by a challenge test to immunized olive flounder using live Streptococcus iniae. In 14 days of challenge test, the positive and E. coli strain control groups showed 100% cumulative mortalities. Test groups immunized by formalin killed cell (FKC) vaccine, GBV with 42 °C and 47 °C heat shock showed 66%, 54% and 54% of cumulative mortalities, respectively. These results suggest that GBV showed the effectiveness for the protection from the streptococcal infection and had higher potential to induce protective antibodies than FKC vaccine.     

Effect of process change from perfusion to fed-batch on product comparability for biosimilar monoclonal antibody

A fed-batch process for the production of biosimilar monoclonal antibody was developed. Since the brand product is produced by perfusion process, the impact of process change from perfusion to fed-batch on product quality and cell performance was evaluated. Perfusion culture was performed at 0.47–1.00 (v/v/d) perfusion rate by spin-filter method with 15–17 μm mesh. Culture parameters such as pH (6.8–7.2), dissolved oxygen (40–70% air saturation), temperature (37 °C) and agitation speed (250 rpm) were applied in both culture modes. In terms of cell performance, volumetric productivity increased 3.7 times while process performance increased 7.5 times in fed-batch culture due to 10 times higher scalability. Considering the glycosylation pattern and charge variants, no significant changes in product quality were observed upon process change, although intact IgG level slightly decreased in fed-batch mode. The change of production media showed more effect on glycosylation patterns than the operation in different culture modes. Furthermore, there were no differences in biological activity, including TNFα, FcγRIIIa, and C1q-binding affinity. Through a scale-up study from 3 L to 12,500 L, it was confirmed that cell performance and product quality could be maintained. In conclusion, product quality of the fed-batch process was comparable to that of the reference product.     

Alkaline lipase from a novel strain Burkholderia multivorans: Statistical medium optimization and production in a bioreactor

An alkaline lipase from Burkholderia multivorans was produced within 15 h of growth in a 14 L bioreactor. An overall 12-fold enhanced production (58 U mL⁻¹ and 36 U mg⁻¹ protein) was achieved after medium optimization following the “one-variable-at-a-time” and the statistical approaches. The optimal composition of the lipase production medium was determined to be (% w/v or v/v): KH₂PO₄ 0.1; K₂HPO₄ 0.3; NH₄Cl 0.5; MgSO₄·7H₂O 0.01; yeast extract 0.36; glucose 0.1; olive oil 3.0; CaCl₂ 0.4 mM; pH 7.0; inoculum density 3% (v/v) and incubation time 36 h in shake flasks. Lipase production was maximally influenced by olive oil/oleic acid as the inducer and yeast extract as the additive nitrogen. Plackett–Burman screening suggested catabolite repression by glucose. Amongst the divalent cations, Ca²⁺ was a positive signal while Mg²⁺ was a negative signal for lipase production. RSM predicted that incubation time, inoculum density and oil were required at their higher levels (36 h, 3% (v/v) and 3% (v/v), respectively) while glucose and yeast extract were required at their minimal levels for maximum lipase production in shake flasks. The production conditions were validated in a 14 L bioreactor where the incubation time was reduced to 15 h.     

Effects of post-induction feed strategies on secretory production of recombinant streptokinase in Escherichia coli

The effects of post-induction nutrient feed rates, on recombinant streptokinase production in fed-batch processes, were investigated using various feed profiles. Recombinant streptokinase was produced using a secretory expression system and was induced by a temperature up-shift, using a temperature-sensitive λ_PL promoter. The specific growth rates decreased sharply upon induction of recombinant protein expression, thus necessitating a variable feed strategy in the post-induction phase. The various feed profiles employed in the post-induction phase included constant feed rates, linearly increasing feed rate and exponentially varying feed rates. Significant differences were obtained in the specific activity of streptokinase produced in these fed-batch processes. A maximum activity per unit biomass of 4.96 × 10⁶ and 4.43 × 10⁶ IU/g DCW was achieved for exponentially decreasing feed and linearly increasing feed, respectively. The decrease in specific growth rate during the post-induction phase was also less pronounced in these cases in comparison to other fed-batch experiments. It was observed that streptokinase productivity is governed by the nutrient feed rate per unit biomass at a critical juncture after induction. The highest activity per unit biomass was obtained when the nutrient feed rate per unit biomass was around 0.7–0.8 g glucose (g DCW)⁻¹ h⁻¹, between 2 and 4 h after induction.     

Biotransformation of 2-phenylethanol to phenylacetaldehyde in a two-phase fed-batch system

Phenylacetaldehyde (PA) can be produced by the oxidation of 2-phenylethanol (PE) through biotransformation. In order to prevent substrate and product inhibitions and the transformation of the PA to phenylacetic acid (PAA), utilization of a two-phase system is very attractive. Gluconobacter oxydans B-72 was used as the microorganism and iso-octane as the solvent. The effect of initial substrate concentration on the PA production was investigated in single- and two-phase systems. In the single-phase system, substrate inhibition occurred above 5 g/l, and in the two-phase system, above 7.5 g/l. Substrate inhibition kinetics were also studied in the two-phase system and kinetic constants were determined as r_max=0.64 g/l min, K_M=8.15 g/l, K_PA=2.5 g/l. Because it was observed that two-phase system is insufficient to remove the substrate inhibition effect, fed-batch operation was utilised in this study. For 7.5 g/l of PE, 1.65, 3.85, and 7.35 g/l of PA were obtained in the single-phase, two-phase, and two-phase three fed-batch systems, respectively. Effect of biotransformation time, initial substrate concentration, agitation speed, and fed-batch number on the PA production was investigated in a two-phase fed-batch system by the response surface methodology (RSM). The optimum values were found as 3 fed-batch number, 2.75 g/l initial substrate concentration, 150 rpm agitation speed, and 65 min of one batch biotransformation time. In order to verify these results, an experiment was performed at these optimum conditions and 7.10 g/l of PA concentration was obtained.     

Site-directed mutagenesis of an Aspergillus niger xylanase B and its expression,purification and enzymatic characterization in Pichia pastoris

Xylanase is an important industrial enzyme. In this research, to improve the thermostability and biochemical properties of a xylanase from Aspergillus niger F19, five arginine substitutions and a disulfide bond were introduced by site-directed mutagenesis. The wild-type gene xylB and the mutant gene xylCX8 were expressed in Pichia pastoris. Compare to those of the wild-type enzyme, the optimal reaction temperature for the mutant enzyme increased from 45 °C to 50 °C, the half-life of the mutant enzyme extended from 10 min to 180 min, and the specific activity increased from 2127 U/mg to 3330 U/mg. However, the V_max and K_m of the mutant xylanase decreased. The enzyme activity in broth obtained from shake flask cultures could be induced to 1850 U/mL in 7 days, which is higher than results reported previously. Furthermore, the highest achievable enzyme activity was 7340 U/mL from 140 g/L of biomass in a 3 L fermentor used in our study.     

Repeated fed-batch cultivation of Arthrospira (Spirulina) platensis using urea as nitrogen source

Arthrospira (Spirulina) platensis (Nordstedt) Gomont was autotrophically cultivated for biomass production in repeated fed-batch process using urea as nitrogen source, with the aim of making large-scale production easier, increasing cell productivity and then reducing the production costs. It was investigated the influence of the ratio of renewed volume to total volume (R), the urea feeding time (t_f) and the number of successive repeated fed-batch cycles on the maximum cell concentration (X_m), cell productivity (P_x), nitrogen-to-cell conversion yield (Y_x/n), maximum specific growth rate (μ_m) and protein content of dry biomass. The experimental results demonstrated that R = 0.80 and t_f = 6 d were the best cultivation conditions, being able to simultaneously ensure, throughout the three fed-batch cycles, the highest average values of three of the five responses (X_m = 2101 ± 113 mg L^?1, P_x = 219 ± 13 mg L^?1 d^?1 and Y_x/n = 10.3 ± 0.8 g g^?1).     

Simplified feeding strategies for fed-batch cultivation of Kluyveromyces marxianus in cheese whey

The present work reports the effect of simple feeding strategies to obtain high-cell-density cultures of Kluyveromyces marxianus maximizing β-galactosidase productivity using cheese whey as basic medium. Linear and exponential feeding strategies, with feeding times of 20, 25 and 35 h, and three different feeding media concentrations (140 g/L, 210 g/L, and 280 g/L lactose concentration), were tested. Final biomass concentration reached 35 g cells dry weight/L and our results showed that continuous lactose addition to culture were able to produce high specific enzyme activities, consequently improving volumetric activities of β-galactosidase when compared to batch cultivations. The best fed-batch strategy, which was the feeding of three-fold lactose concentration in the cheese whey-medium during 25 h, resulted in β-galactosidase productivity of 291 U/L h, representing an increase of more than 50% compared to batch cultivations.     

High production of poly-β-hydroxybutyrate (PHB) by an Azotobacter vinelandii mutant altered in PHB regulation using a fed-batch fermentation process

A mixed fermentation strategy based on exponentially fed-batch cultures (EFBC) and nutrient pulses with sucrose and yeast extract was developed to achieve a high concentration of PHB by Azotobacter vinelandii OPNA, which carries a mutation on the regulatory systems PTSNtr and RsmA-RsmZ/Y, that negatively regulate the synthesis of PHB. Culture of the OPNA strain in shake flaks containing PY-sucrose medium significantly improved growth and PHB production with respect to the results obtained from the cultures with the parental strain (OP). When the OPNA strain was cultured in a batch fermentation keeping constant the DOT at 4%, the maximal growth rate (0.16 h⁻¹) and PHB yield (0.30 g_PHB g_Suc⁻¹) were reached. Later, in EFBC, the OPNA strain increased three fold the biomass and 2.2 fold the PHB concentration in relation to the values obtained from the batch cultures. Finally, using a strategy of exponential feeding coupled with nutrient pulses (with sucrose and yeast extract) the production of PHB increased 7-fold to reach a maximal PHB concentration of 27.3 ± 3.2 g L⁻¹ at 60 h of fermentation. Overall, the use of the mutant of A. vinelandii OPNA, impaired in the PHB regulatory systems, in combination with a mixed fermentation strategy could be a feasible strategy to optimize the PHB production at industrial level.     

Inulinase production by the marine yeast Cryptococcus aureus G7a and inulin hydrolysis by the crude inulinase

The marine yeast strain G7a isolated from sediment of China South Sea was found to secrete a large amount of inulinase into the medium. This marine yeast strain was identified to be a strain of Cryptococcus aureus according to the results of routine yeast identification and molecular methods. The crude inulinase produced by this marine yeast showed the highest activity at pH 5.0 and 50 °C. The optimal medium for inulinase production was artificial seawater containing inulin 4.0% (w/v), K₂HPO₄ 0.3% (w/v), yeast extract 0.5% (w/v), KCl 0.5% (w/v), CaCl₂ 0.12% (w/v), NaCl 4.0% (w/v) and MgCl₂·6H₂O 0.6% (w/v), while the optimal cultivation conditions for inulinase production were pH 5.0, a temperature of 28 °C and a shaking speed of 170 rpm. Under the optimal conditions, over 85.0 U/ml of inulinase activity was produced within 42 h of fermentation at shake flask level. This is very high level of inulinase activity produced by yeasts. A large amount of monosaccharides and oligosaccharides were detected after inulin hydrolysis by the crude inulinase.     

Evaluation of distant carbon sources in biosurfactant production by a gamma ray-induced Pseudomonas putida mutant

Pseudomonas putida 33 wild strain, subjected to gamma ray mutagenesis and designated as P. putida 300-B mutant was used as microbial rhamnolipid-producer by using distant carbon sources (viz. hydrocarbons, waste frying oils ‘WFOs’, vegetable oil refinery wastes and molasses) in the minimal media under shake flask conditions. The behavior of glucose as co-substrate and growth initiator was examined. The 300-B mutant strain showed its ability to grow on all the substrates tested and produced rhamnolipid surfactants to different extents however; soybean and corn WFOs were observed to be preferred carbon sources followed by kerosene and paraffin oils, respectively. The best cell biomass (3.5 g l⁻¹) and rhamnolipids yield (4.1 g l⁻¹) were obtained with soybean WFO as carbon source and glucose as growth initiator under fed-batch cultivation showing an optimum specific growth rate (μ) of 0.272 h⁻¹, specific product yield (q_p) of 0.318 g g⁻¹ h and volumetric productivity (P_V) of 0.024 g l⁻¹ h. The critical micelle concentration of its culture supernatant was observed to be 91 mg rhamnolipids l⁻¹ and surface tension as 31.2 mN m⁻¹.     

Production of pediocin SM-1 by Pediococcus pentosaceus Mees 1934 in fed-batch fermentation: Effects of sucrose concentration in a complex medium and process modeling

Production of pediocin SM-1 by Pediococcus pentosaceus Mees 1934 was investigated in semi-aerobic, pH-controlled, batch and fed-batch fermentations using a complex medium containing sucrose as the main source of carbon. The effects of sucrose concentration were studied in fed-batch fermentations in which a sucrose solution was added at stable feeding rates (5, 7, 9 and 10 g/l/h). The results showed that pediocin is produced as a product of the primary metabolism and its titer could be greatly improved by adjusting the sucrose feeding rate in fed-batch fermentation. The maximum titer of pediocin of 145 AU/ml was obtained in the fed-batch culture with 7 g/l/h feeding rate and that was 119% higher compared to the titer obtained in batch culture. Higher feeding rates (9 and 10 g/l/h) resulted in decreased pediocin yields while biomass levels appeared to be rather unaffected. The specific rate of pediocin formation was also sensitive to sucrose concentration levels. A mathematical model developed on the basis of well-known rate equations for batch and fed-batch cultures and growth associated production, described successfully cell growth, sucrose assimilation, lactate production and pediocin production in fed-batch culture.     

Characterization and site-directed mutagenesis of a novel class II 5-enopyruvylshikimate-3-phosphate (EPSP) synthase from the deep-sea bacterium Alcanivorax sp. L27

The 5-enolpyruvylshikimate-3-phosphate synthase (EPSPS) is a key enzyme in the aromatic amino acid biosynthetic pathway in microorganisms and plants, which catalyzes the formation of 5-enolpyruvylshikimate-3-phosphate (EPSP) from shikimate-3-phosphate (S3P) and phosphoenolpyruvate (PEP). In this study, a novel AroA-encoding gene was identified from the deep sea bacterium Alcanivorax sp. L27 through screening the genomic library and termed as AroA_A.sp. A phylogenetic analysis revealed that AroA_A.sp (1317 bp and 438 amino acids) is a class II AroA. This enzyme exhibited considerable activity between pH 5.5 and pH 8.0 and notable activity at low temperatures. The K_M for PEP and IC₅₀ [glyphosate] values (the concentration of glyphosate that inhibited enzyme activity by 50%) of AroA_A.sp were 78 μM and 1.5 mM, respectively. Furthermore, site-directed mutagenesis revealed that the G100A mutant had a 30-fold increase in the IC₅₀ [glyphosate] value; while the L105P mutant showed only 20% catalytic activity compared to wild-type AroA_A.sp. The specific activity of the wild-type AroA_A.sp, the G100A mutant and the L105P mutant were 7.78 U/mg, 7.26 U/mg and 1.76 U/mg, respectively. This is the first report showing that the G100A mutant of AroA displays considerably improved glyphosate resistance and demonstrates that Leu105 is essential for the enzyme's activity.     

Determination of mildronate by LC–MS/MS and its application to a pharmacokinetic study in healthy Chinese volunteers

A simple, rapid and accurate liquid chromatography–tandem mass spectrometry (LC–MS/MS) method has been developed and validated for the determination of mildronate in human plasma. Following a simple protein precipitation with methanol, the analyte was separated on a C₁₈ column by isocratic elution with methanol and 10 mM ammonium acetate (55:45; v/v), and then analyzed by mass spectrometry in the positive ion MRM mode. Good linearity was achieved over a wide range of 0.01–20 μg/mL. The intra- and inter-batch precisions (as RSD, %) were less than 7.1%. The average extraction recovery was 87.5%. The method described above has been used, for the first time, to reveal the pharmacokinetics of mildronate injection in healthy subjects. After single intravenously administration of 250, 500 and 1000 mg mildronate, the elimination half-life (t_1/2) were (5.56 ± 1.55), (6.46 ± 1.07) and (6.55 ± 1.17) h, respectively. The Student–Newman–Keuls test results showed that peak plasma concentration (C_max) and the area under the plasma concentration versus time curve from time 0 to 24 h (AUC_0–24) were both linearly related to dose. The pharmacokinetics of mildronate fitted the linear dynamic feature over the dose range studied. The essential pharmacokinetic parameters of multidoses administration intravenously (500 mg, b.i.d) were as follows: t_1/2 was (15.34 ± 3.14) h; C_max was (25.50 ± 3.63) μg/mL; AUC_0–24 was (58.56 ± 5.57) mg h/L. The t_1/2 and AUC of multidoses administration intravenously were different from those of single-dose administration significantly. These findings suggested that accumulation of mildronate in plasma occurred.     

Efficient production of (R)-(−)-mandelic acid with highly substrate/product tolerant and enantioselective nitrilase of recombinant Alcaligenes sp.

For efficient production of (R)-(−)-mandelic acid, a nitrilase gene from Alcaligenes sp. ECU0401 was cloned and overexpressed in Escherichia coli. After simple optimization of the culture conditions, the biocatalyst production was greatly increased from 500 to 7000 U/l. The recombinant E. coli whole cells showed strong tolerance against a high substrate concentration of up to 200 mM, and the concentration of (R)-(−)-mandelic acid after only 4 h of transformation reached 197 mM with an enantiomeric excess (ee_p) of 99%. In a fed-batch reaction with 600 mM mandelonitrile as the substrate, the cumulative production of (R)-(−)-mandelic acid after 17.5 h of conversion reached 520 mM. The recombinant E. coli cells could also be repeatedly used in the biotransformation, retaining 40% of the initial activity after 10 batches of reaction. The highly substrate/product tolerable and enantioselective nature of this recombinant nitrilase suggests that it is of great potential for the practical production of optically pure (R)-(−)-mandelic acid.