Monosaccharide precursors for boosting chondroitin-like capsular polysaccharide production

Chondroitin sulfate is a well-known bioactive molecule, widely used as an anti-osteoarthritis drug, that is nowadays mainly produced by animal tissue sources with unsafe extraction procedures. Recent studies have explored an integrated biotechnological–chemical strategy to obtain a chondroitin sulfate precursor from Escherichia coli K4 capsular polysaccharide, demonstrating the influence of environmental and growth conditions on capsule synthesis. In this research work, the flexibility of the strain biosynthetic machinery was investigated to enhance the K4 capsular polysaccharide production by supplementing the growth medium with the monosaccharides (glucuronic acid, galactosamine and fructose) that constitute the chain. Shake flask experiments were performed by adding the sugars singularly or together, by testing monosaccharide different concentrations and times of addition and by observing the bacterial sugar consumption. A K4 capsular polysaccharide production enhancement, compared to the control, was observed in all cases of supplementation and, in particular, significant 68 and 57 % increases were observed when adding 0.385 mM glucuronic acid plus galactosamine or 0.385 mM fructose, respectively. Increased expression levels of the gene kfoC, coding for a K4 polymerase, evaluated in different growth conditions, confirmed the results at the molecular level. Furthermore, batch fermentations, performed in lab-scale reactors (2 L), allowed to double the K4 capsular polysaccharide production values obtained in shake flask conditions, by means of a strict control of the growth parameters.     

Kinetics of kojic acid fermentation byAspergillus flavus link S44-1 using sucrose as a carbon source under different pH conditions

Kojic acid production byAspergillus flavus strain S44-1 using sucrose as a carbon source was carried out in a 250-mL shake flask and a 2-L stirred tank fermenter. For comparison, production of kojic acid using glucose, fructose and its mixture was also carried out. Kojic acid production in shake flask fermentation was 25.8 g/L using glucose as the sole carbon source, 23.6 g/L with sucrose, and 6.4 g/L from fructose. Reduced kojic acid production (13.5 g/L) was observed when a combination of glucose and fructose was used as a carbon source. The highest production of kojic acid (40.2 g/L) was obtained from 150 g/L sucrose in a 2 L fermenter, while the lowest kojic acid production (10.3 g/L) was seen in fermentation using fructose as the sole carbon source. The experimental data from batch fermentation and resuspended cell system was analysed in order to form the basis for a kinetic model of the process. An unstructured model based on logistic and Luedeking-Piret equations was found suitable to describe the growth, substrate consumption, and efficiency of kojic acid production byA. flavus in batch fermentation using sucrose. From this model, it was found that kojic acid production byA. flavus was not a growth-associated process. Fermentation without pH control (from an initial culture pH of 3.0) showed higher kojic acid production than single-phase pH-controlled fermentation (pH 2.5, 2.75, and 3.0).     

Kojic acid production byAspergillus flavus using gelatinized and hydrolyzed sago starch as carbon sources

Direct conversion of gelatinized sago starch into kojic acid byAspergillus flavus strain having amylolytic enzymes was carried out at two different scales of submerged batch fermentation in a 250-mL shake flask and in a 50-L stirred-tank fermentor. For comparison, fermentations were also carried out using glucose and glucose hydrolyzate from enzymic hydrolysis of sago starch as carbon sources. During kojic acid fermentation of starch, starch was first hydrolyzed to glucose by the action of α-amylase and glucoamylase during active growth phase. The glucose remaining during the production phase (non-growing phase) was then converted to kojic acid. Kojic acid production (23.5g/L) using 100 g/L sago starch in a shake flask was comparable to fermentation of glucose (31.5 g/L) and glucose hydrolyzate (27.9 g/L) but in the 50-L fermentor was greatly reduced due to non-optimal aeration conditions. Kojic acid production using glucose was higher in the 50-L fermentor than in the shake flask.     

Effect of chemical and physical parameters on the production of L-asparaginase from a newly isolated Serratia marcescens SK-07

Aims: The objective of this study is to optimize the levels of carbon and nitrogen sources of the medium in shake flask experiments and evaluate the effect of pH and dissolved oxygen (DO) on the production of l ‐asparaginase from a newly isolated Serratia marcescens SK‐07 in a batch bioreactor. Methods and Results: Central composite rotatable design (CCRD) was applied to optimize the levels of carbon and nitrogen sources of the medium in shake flask experiments. The optimal levels of l ‐asparagine, glucose, yeast extract and peptone were found to be 4·93, 3·81, 3·65 and 1·47 g l^?1, respectively, and maximal l ‐asparaginase production of 25·02 U mg^?1 was obtained under these conditions. Among the carbon sources tested, l ‐asparagine was identified to be the most favourable carbon source for enhanced production of l ‐asparaginase. The maximum l ‐asparaginase production of 29·89 U mg^?1 was achieved in a batch bioreactor at initial pH of 6·5 (uncontrolled) and DO level of 40% in the culture. Conclusions: We have isolated, screened and identified the potential micro‐organism, S. marcescens, for the production of l ‐asparaginase. An overall 5·55‐fold increase in the production was achieved under optimal levels of carbon and nitrogen sources, DO level and at initial pH of 6·5 (uncontrolled). Significance and Impact of the Study: The experiments illustrate the importance of statistical method for optimization of carbon and nitrogen sources and study the effect of physical process parameters on the production of l ‐asparaginase in shake flask and bioreactor, respectively. This study would be helpful for bioprocess development of bacterial l ‐asparaginase production.     

Engineering Escherichia coli BL21 (DE3) for high-yield production of germacrene A,a precursor of β-elemene via combinatorial metabolic engineering strategies

β-elemene is one of the most commonly used antineoplastic drugs in cancer treatment. As a plant-derived natural chemical, biologically engineering microorganisms to produce germacrene A to be converted to β-elemene harbors great expectations since chemical synthesis and plant isolation methods come with their production deficiencies. In this study, we report the design of an Escherichia coli cell factory for the de novo production of germacrene A to be converted to β-elemene from a simple carbon source. A series of systematic approaches of engineering the isoprenoid and central carbon pathways, translational and protein engineering of the sesquiterpene synthase, and exporter engineering yielded high-efficient β-elemene production. Specifically, deleting competing pathways in the central carbon pathway ensured the availability of acetyl-coA, pyruvate, and glyceraldehyde-3-phosphate for the isoprenoid pathways. Adopting lycopene color as a high throughput screening method, an optimized NS^Y305N was obtained via error-prone polymerase chain reaction mutagenesis. Further overexpression of key pathway enzymes, exporter genes, and translational engineering produced 1161.09 mg/L of β-elemene in a shake flask. Finally, we detected the highest reported titer of 3.52 g/L of β-elemene and 2.13 g/L germacrene A produced by an E. coli cell factory in a 4-L fed-batch fermentation. The systematic engineering reported here generally applies to microbial production of a broader range of chemicals. This illustrates that rewiring E. coli central metabolism is viable for producing acetyl-coA-derived and pyruvate-derived molecules cost-effectively.     

Microbioreactor (micro-Matrix) potential in aerobic and anaerobic conditions with different industrially relevant microbial strains

Microscale fermentation systems are important high throughput tools in clone selection, and bioprocess set up and optimization, since they provide several parallel experiments in controlled conditions of pH, temperature, agitation, and gas flow rate. In this work we evaluated the performance of biotechnologically relevant strains with different respiratory requirements in the micro-Matrix microbioreactor. In particular Escherichia coli K4 requires well aerated fermentation conditions to improve its native production of chondroitin-like capsular polysaccharide, a biomedically attractive polymer. Results from batch and fed-batch experiments demonstrated high reproducibility with those obtained on 2 L reactors, although highlighting a pronounced volume loss for longer-term experiments. Basfia succiniciproducens and Actinobacillus succinogenes need CO₂ addition for the production of succinic acid, a building block with several industrial applications. Different CO₂ supply modes were tested for the two strains in 24 h batch experiments and results well compared with those obtained on lab-scale bioreactors. Overall, it was demonstrated that the micro-Matrix is a useful scale-down tool that is suitable for growing metabolically different strains in simple batch process, however, a series of issues should still be addressed in order to fully exploit its potential.     

High cell density cultivation of <Emphasis Type="Italic">Escherichia coli</Emphasis> K4 in a microfiltration bioreactor: a step towards improvement of chondroitin precursor production

Background  

The bacteria Escherichia coli K4 produces a capsular polysaccharide (K4 CPS) whose backbone is similar to the non sulphated chondroitin chain. The chondroitin sulphate is one of the major components of the extra-cellular matrix of the vertebrate connective tissues and a high value molecule, widely employed as active principle in the treatment of osteoarthritis. It is usually obtained by extraction from animal tissues, but the risk of virus contaminations, as well as the scarceness of raw material, makes this productive process unsafe and unable to satisfy the growing market demand. In previous studies a new biotechnological process to produce chondroitin from Escherichia coli K4 capsular polysaccharide was investigated and a 1.4 g·L^-1 K4 CPS concentration was reached using fed-batch fermentation techniques. In this work, on the trail of these results, we exploited new fermentation strategies to further improve the capsular polysaccharide production.     

Improved Production of Bioactive Glucosylmannosyl-Glycerolipid by Sponge-Associated <Emphasis Type="Italic">Microbacterium</Emphasis> Species

The marine Microbacterium species HP2 (DSM 12583), isolated from the sponge Halichondria panicea, is able to produce a glucosylmannosyl-glycerolipid when grown on a complex medium with glucose. Optimizing the carbon sources in shake flask experiments has shown that glycerol affords the highest specific glycoglycerolipid production. The product yield approached 300 mg/L or 25 mg/g biomass upon scaling up in a 40-L bioreactor volume. The native diglycosyl-glycerolipid GGL.2 strongly inhibited growth of the tumor cell lines HM02 and Hep G2 (50% inhibition at 0.4 to 3 µg/mL), while the related deacylated compound (GG.2) showed a potent anti-tumor-promoting activity.     

Improvement of Panax notoginseng cell culture for production of ginseng saponin and polysaccharide by high density cultivation in pneumatically agitated bioreactors

A Panax notoginseng cell culture was successfully scaled up from shake flask to 1.0-L bubble column reactor and concentric-tube airlift reactor. High-density bioreactor batch cultivation was carried out using a modified MS medium. The maximum cell density in batch cultures reached 20.1, 21.0 and 24.1 g/L in the shake flask, bubble column and airlift reactors, respectively, and their corresponding biomass productivity was 950, 1140 and 1350 mg/(L x d) for each. The productivity of ginseng saponin was 70, 96 and 99 mg/(L x d) in the flask, bubble column and airlift reactors, respectively; and the polysaccharide productivity reached 104, 119 and 151 mg/(L x d) for each. Furthermore, a fed-batch cultivation strategy was developed on the basis of specific oxygen uptake rate (SOUR), i.e., sucrose feeding before a sharp decrease of SOUR, and the highest cell density of 29.7 g/L was successfully achieved in the airlift bioreactor on day 17 with a very high biomass productivity of 1520 mg/(L x d). The concentrations of ginseng saponin and polysaccharide reached about 2.1 and 3.0 g/L, respectively, and their productivity was 106 (saponin) and 158 mg/(L x d) (polysaccharide). This work successfully demonstrated the high-density bioreactor cultivation of P. notoginseng cells in pneumatically agitated bioreactors and the reproduction of the shake flask culture results in bioreactors. The cell density, biomass productivity, production titer and productivity of both ginseng saponin and polysaccharide obtained here were the highest that have been reported on a reactor scale for all the ginseng species.     

IS2-mediated overexpression of kfoC in E. coli K4 increases chondroitin-like capsular polysaccharide production

Transposons are developing molecular tools commonly used for several applications: one of these is the delivery of genes into microorganisms. These mobile genetic elements are characterised by two repeated insertion sequences that flank a sequence encoding one or more orfs for a specific transposase that moves these sequences to other DNA sites. In the present paper, the IS2 transposon of Escherichia coli K4 was modified in vitro by replacing the sequence coding for the transposase with that of the kfoC gene that codes for chondroitin polymerase. KfoC is responsible for the polymerisation of the bacterial capsular polysaccharide whose structure is analogous to that of chondroitin sulphate, a glycosaminoglycan with established and emerging biomedical applications. The recombinant construct was stably integrated into the genome of E. coli K4 by exploiting the transposase from endogenous copies of IS2 in the E. coli chromosome. A significant improvement of the polysaccharide production was observed, resulting in 80 % higher titres in 2.5-L fed-batch cultivations and up to 3.5 g/L in 22-L fed-batch cultures.     

In situ pH management for microbial culture in shake flasks and its application to increase plasmid yield

Shake flasks are widely used to culture microorganisms, but they do not allow for pH control without additional infrastructure. In the presence of a carbon source like glucose, culture pH typically decreases due to overflow metabolism and can limit the growth of microorganisms in shake flasks. In this study, we demonstrate the use of magnesium hydroxide-loaded pH managing hydrogels (m-pHmH) for in situ base release to counter the decrease in culture pH in shake flasks using Escherichia coli as a model organism, in both complex and mineral salts medium. Base release from m-pHmH is shown to increase with decreasing pH (22-fold increase in release rate from pH 8 to 5), thus providing feedback from culture pH. The addition of m-pHmH resulted in better pH maintenance and higher biomass yields of E. coli K12 in media containing glucose as a carbon source. The use of m-pHmH with additional buffer resulted in pH being maintained above 6.9 while pH decreases below 5 without m-pHmH. We demonstrate one application of such in situ pH management to increase the volumetric plasmid yield from E. coli in shake flask culture. In situ glucose release through a hydrogel to mimic fed-batch culture along with the addition of m-pHmH resulted in a 395 % increase in volumetric plasmid yield to 38 μg/ml in shake flask culture.     

Economical parallel protein expression screening and scale-up in Escherichia coli

A novel microfermentation and scale-up platform for parallel protein production in Escherichia coli is described. The vertical shaker device Vertiga, which generates low-volume high density (A₆₀₀ ∼ 20) Escherichia coli cultures in 96-position deep-well plates without auxiliary oxygen supplementation, has been coupled to a new disposable shake flask design, the Ultra Yield^TM flask, that allows for equally high cell culture densities to be obtained. The Ultra Yield^TM flask, which accommodates up to 1 l in culture volume, has a baffled base and a more vertical wall construction compared to traditional shake flask designs. Experimental data is presented demonstrating that the Ultra Yield^TM flask generates, on average, an equivalent amount of recombinant protein per unit cell culture density as do traditional shake flask designs but at a substantially greater amount per unit volume. The combination of Vertiga and the Ultra Yield^TM flask provides a convenient and scalable low-cost solution to parallel protein production in Escherichia coli.     

Application of a 22L scale membrane bioreactor and cross-flow ultrafiltration to obtain purified chondroitin

Recently, the possibility of producing fructosylated chondroitin from the capsular polysaccharide of Escherichia coli O5:K4:H4, in fed‐batch and microfiltration experiments was assessed on a 2 L bioreactor. In this work, a first scale‐up step was set on a 22 L membrane reactor with modified baffles to insert ad hoc designed microfiltration modules permanently inside the bioreactor vessel. Moreover, the downstream polysaccharide purification process, recently established on the A¨?KTA cross‐flow instrument, was translated to a UNIFLUX‐10, a tangential flow filtration system suitable for prepilot scale. In particular, the microfiltered permeates obtained throughout the fermentation, and the supernatant recovered from the centrifuged broth at the end of the process, were treated as two separate samples in the following ultrafiltration procedure, and the differences in the two streams and how these affected the ultrafiltration/diafiltration process performance were analysed. The total amount of K4 capsular polysaccharide was about 85% in the broth and 15% in the microfiltered permeates. However, the downstream treatment was more efficient when applied to the latter. The major contaminant, the lipopolysaccharide, could easily be separated by a mild hydrolysis that also results in the elimination of the unwanted fructosyl residue, which is linked to the C‐3 of glucuronic acid residues. The tangential ultrafiltration/diafiltration protocols developed in a previous work were effectively scaled‐up, and therefore in this research proof of principle was established for the biotechnological production of chondroitin from the wild‐type strain E. coli O5:K4:H4. The complete downstream procedure yielded about 80% chondroitin with 90% purity. © 2012 American Institute of Chemical Engineers Biotechnol. Prog., 28: 1012–1018, 2012     

E. coli K5 fermentation and the preparation of heparosan,a bioengineered heparin precursor

Heparosan is an acidic polysaccharide natural product, which serves as the critical precursor in heparin biosynthesis and in the chemoenzymatic synthesis of bioengineered heparin. Heparosan is also the capsular polysaccharide of Escherichia coli K5 strain. The current study was focused on the examination of the fermentation of E. coli K5 with the goal of producing heparosan in high yield and volumetric productivity. The structure and molecular weight properties of this bacterial heparosan were determined using polyacrylamide gel electrophoresis (PAGE) and Fourier transform mass spectrometry. Fermentation of E. coli K5 in a defined medium using exponential fed‐batch glucose addition with oxygen enrichment afforded heparosan at 15 g/L having a number average molecular weight of 58,000 Da and a weight average molecular weight of 84,000 Da. Biotechnol. Bioeng. 2010;107: 964–973. © 2010 Wiley Periodicals, Inc.     

STATISTICAL OPTIMIZATION OF GREEN FLUORESCENT PROTEIN PRODUCTION FROM Escherichia coli BL21(DE3)

An optimized cultivation condition is needed to maximize the functional green fluorescent protein (GFP) production. Six process variables (agitation rate, temperature, initial medium pH, concentration of inducer, time of induction, and inoculum density) were screened using the fractional factorial design. Three variables (agitation rate, temperature, and time of induction) exerted significant effects on functional GFP production in E. coli shake flask cultivation and were optimized subsequently using the Box–Behnken design. An agitation rate of 206 rpm at 31°C and induction of the protein expression when the cell density (OD_600nm) reaches 1.04 could enhance the yield of functional GFP production from 0.025 g/L to 0.241 g/L, which is about ninefold higher than the unoptimized conditions. Unoptimized cultivation conditions resulted in protein aggregation and hence reduced the quantity of functional GFP. The model and regression equation based on the shake flask cultivation could be applied to a 2-L bioreactor for maximum functional GFP production.     

The scale up of mycelial shake flask fermentations: A case study of gamma linolenic acid production byMucor hiemalis IRL 51

Summary Production of gamma linolenic acid (GLA) by the filamentous fungusMucor hiemalis IRL 51 was studied in both shake flask culture and in a 10-L stirred tank fermenter. This study was conducted to assess how the results from shake flask media screening trials compared to those obtained in a 10-L stirred tank fermenter, which is assumed to be more representative of an industrial system. The results show that the biological performance in 10-L fermenters is usually the same as that in shake flask culture. There were some inconsistencies which could possibly be attributed to scale, but no large differences were systematically seen. These results show that for this filamentous fungus, shake flask culture provides a quick and inexpensive way of optimizing medium composition.     

Production of extracellular water insoluble β-1,3-glucan (curdlan) fromBacillus sp. SNC07

β-1,3-Glucan (curdlan) is a water-insoluble polysaccharide composed exclusively of β-1,3 linked glucose residues. Extracellular curdlan was mostly synthesized byAgrobacterium species andAlcaligenes faecalis under nitrogen-limiting conditions. In this study, we screened the microorganisms capable of producing extracellular curdlan from soil samples. For the first time, we reported Gram-positive bacteriumBacillus sp. SNC 107 capable of producing extracellular curdlan in appreciable amounts. The effect of different carbon sources on curdlan production was studied and found that the yield of curdlan was more when glucose was used as carbon source. It was also found that maximum production was achieved when the initial concentration of ammonium and phosphate in the medium was 0.5 and 1.9 g/L respectively. In this study the curdlan production was increased from 3 to 7 g/L in shake flask cultures.     

Production of recombinant beta-amylase of Bacillus aryabhattai

In this study, the effects of carbon source, nitrogen source, and metal ions on cell growth and Bacillus aryabhattai β-amylase production in recombinant Brevibacillus choshinensis were investigated. The optimal medium for β-amylase production, containing glucose (7.5?g·L^?1), pig bone peptone (40.0?g·L^?1), Mg²⁺ (0.05?mol·L^?1), and trace metal elements, was determined through single-factor experiments in shake flasks. When cultured in the optimized medium, the β-amylase yield reached 925.4?U mL^?1, which was 7.2-fold higher than that obtained in the initial medium. Besides, a modified feeding strategy was proposed and applied in a 3-L fermentor fed with glucose, which achieved a dry cell weight of 15.4?g L^?1. Through this cultivation approached 30?°C with 0?g·L^?1 initial glucose concentration, the maximum β-amylase activity reached 5371.8?U mL^?1, which was 41.7-fold higher than that obtained with the initial medium in shake flask.     

Optimization of lipase production byPseudomonas aeruginosa MB 5001 in batch cultivation

Summary The production ofPseudomonas aeruginosa MB 5001 extracellular lipase was optimized by batch cultivation employing shake flasks and 23-L bioreactors. This enzyme efficiently and selectively bioconverts dimethyl 5-(3-(2-(7-chloroquinolin-2-yl)ethyl)phenyl)4,6-dithianonanedioate (diester) to its (S)-ester acid. Process development studies focused on the identification and optimization of the physicochemical parameters required to achieve maximum lipase production. Of the media evaluated, a peptonized milk-based medium was found to support excellent lipase production and stability. Medium composition and process parameters that supported optimal lipase production were different from those supporting maximum biomass formation. Of the parameters investigated, dissolved oxygen tension had the most significant and unexpected impact on lipase production. Elevated lipase production was achieved whenP. aeruginosa MB 5001 was cultivated in a dissolved oxygen limited environment. Overall, these process development studies resulted in a 100% increase in lipase production when compared to the original shake flask process employing skim milk.