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Brazilian Journal of Chemical Engineering

Print version ISSN 0104-6632

Braz. J. Chem. Eng. vol.19 no.3 São Paulo July/Sept. 2002

http://dx.doi.org/10.1590/S0104-66322002000300002 

DEVELOPMENT OF A BIOPROCESS FOR THE PRODUCTION OF ACTINOMYCIN-D

 

M.F.V.Q. Sousa1, C.E.Lopes1 and N.Pereira Jr.2
1Departamento de Antibióticos, Universidade Federal de Pernambuco,
Phone/Fax,(081) 3271-8346, 50670-901, Recife-PE, Brazil,, E-mail: mfvqs@npd.ufpe.br
2Departamento de Engenharia Bioquímica, UFRJ, Phone (021) 2562-7620,
21949-900, Rio de Janeiro - RJ, Brazil;
E-mail: nei@eq.ufrj.br

 

(Received: March 1, 2002 ; Accepted: June 25, 2002)

 

 

Abstract - S. parvulus was selected from three species of Streptomyces that produce actinomycins, as it has the greatest antibiotic activity (152 mg/L) and produces only actinomycin-D. Aiming at improving the antibiotic production in shaken flasks, the substitution of glucose by fructose in concentrations of 20, 30 and 40 g/L was investigated. In all cases this replacement led to an increase in the antibiotic production, reaching a maximum concentration of 635 mg/L for an initial fructose concentration of 30 g/L. In experiments conducted in a bioreactor at different degrees of aeration (0.5, 1.0 and 1.5 vvm) and stirring speeds (300 and 500 rpm), it was found that the greatest antibiotic production (1530 mg/L) occurred with a aeration of 1.5 vvm and a stirring speed of 500 rpm. The fermented medium showed the rheological behavior of a pseudoplastic fluid.
Keywords: actinomycin-D, S. parvulus, S. felleus, S. regensis, fermentation, rheology.

 

 

INTRODUCTION

Actinomycin-D is a chromopeptide antibiotic of indisputable therapeutic value, currently used in the treatment of several human neoplasias. This antibiotic can be synthesized by different species of Streptomyces as part of a mixture of several actinomycins (Korzybski et al., 1967).

Few studies have been done on the production of actinomycin-D (Williams and Katz, 1977; Dalili and Chau, 1988). Working with shaken flasks, Williams and Katz (1977) developed a chemically defined medium with a view to obtaining high levels of actinomycin-D (500 to 600 mg/L) with S. parvulus ATCC 12434. Using the same medium and the same strain immobilized in calcium alginate, Dalili and Chau (1988) achieved maximum actinomycin-D concentrations of around 50, 70 and 80 mg/L by employing batch, fed batch and continuous processes, respectively, in an airlift bioreactor.

Some studies have dealt with the rheological characterization of media fermented by actinomycete, though none refer to the production of actinomycin-D by Streptomyces parvulus.

The aim of this work was to maximize the production of this drug, addressing the following issues: selection of the most productive of the three species of Streptomyces; identification of the best composition of the production medium in shaken flasks; study of the most favourable aeration and agitation conditions in the bioreactor, using the selected species; and rheological characterization of the fermented medium.

 

MATERIALS AND METHODS

Microorganisms

The Streptomyces species used were S. regensis DAUFPE 3053, S. felleus DAUFPE 3079 and S. parvulus DAUFPE 3124 from the collection of microorganisms at the Departamento de Antibióticos at the UFPE. B. subtilis ATCC 6633 was used to measure antibiotic activity, as recommended by Farmacopéia Brasileira (1988).

Conditions and Media for Maintenance and Sporulation

The slope medium used for the maintenance and sporulation of the species of Streptomyces had the following composition: glucose 4 g/L, yeast extract 4 g/L, malt extract 10 g/L and agar medium 20 g/L, and the species were incubated at 30°C for five to seven days, after which time they were kept at 4°C. B. subtilis was maintained in slant tubes containing a nutrient agar medium (peptone 5 g/L, meat extract 3 g/L and agar 20 g/L), incubated at 37°C for 24 h and conserved at 4°C.

Preparation of the Spore Suspensions

The spores were skimmed off the surface of the slant tubes with 3 mL of physiological solution containing 0.1% (v/v) Tween 80, using the technique employed by Hopwood et al. (1985). Each spore suspension was quantified - S. parvulus (8.0 x 107 CFU/mL), S. regensis (1.25 x 104 CFU/mL), S. felleus (2.7 x 108 CFU/mL) - and stored at -4°C. For B. subtilis the method described in the Farmacopéia Brasileira (1988) was adopted.

Growth and Production Media

The growth medium used in all the tests had the following composition: tryptone 5 g/L and yeast extract 5 g/L. To evaluate the actinomycin production of the Streptomyces species, a culture medium with the following composition was used: glucose 20 g/L, soy milk 20 g/L, NaCl 5 g/L, K2HPO4 1.5 g/L and CaCO3 2 g/L. For the experiments carried out in a bioreactor, an optimized medium with the following composition was used: fructose 30 g/l, soy milk 30 g/L and CaCO3 2 g/L. In all the media, the pH was adjusted to between 7.0 and 7.2. The soy milk used was a commercially available brand call Soymilk, produced by Olvebra Industrial S.A.

Experimental Procedure

250 mL Erlenmeyer flasks containing 25 mL growth medium were inoculated with 100 µL suspensions of the species S. parvulus and S. felleus, which had been standardized at 1.14 x 107 CFU/mL, and S. regensis, which had a lower quantity of spores (1.25 x 104 CFU/mL). These flasks were incubated at 30±2ºC and shaken at 200 rpm for 42 hours (growth phase). After this period, 5 mL of each of the suspensions was used to inoculate the 250 mL Erlenmeyer flasks, containing 50 mL of the selected medium. These were then submitted to the same temperature and agitation conditions for 192 hours (production phase). The performance of each of the species was evaluated for antibiotic activity after 96 h and thereafter at 24-hour intervals. To optimize the production medium for the selected species, glucose and fructose as well as their initial concentrations were varied for the tests in shaken flasks. The flasks were initially inoculated with a spore suspension of the selected species (8.0 x 107 CFU/mL) and submitted to the temperature and agitation conditions already described. The experiments in the bioreactor were carried out at different degrees of aeration (0.5, 1.0 and 1.5 vvm) and stirring speeds (300 and 500 rpm). Samples were removed at 24-hour intervals and assessed for concentration of actinomycin D, of total reducing sugars and of dry weight.

Description of the Bioreactor

A 14-liter bioreactor, operating with an 8.0-liter volume, was used. Sterile air was supplied continuously through a porous metal sparger, and the stirrers were turbines with four flat blades. Two turbines were placed in the following layout: the first was placed directly above the sparger, the second at a distance from the first corresponding to one-third of the reactor's diameter. Whenever necessary, antifoam was added automatically using a fixed-flow peristaltic pump connected to a sensor. The temperature was maintained at 30°C by controlling the temperature of the water bath in which the bioreactor was immersed. Figure 1 shows a diagram of the bioreactor.

Analytical Methods

The antibiotic activity of each species of Streptomyces was evaluated by the agar diffusion method (Isaacson and Kirschbaum, 1986), using B. subtilis. Using ethyl acetate as solvent, for each species of Streptomyces only the extracts of the samples corresponding to 144 h were submitted to thin layer chromatography. Five mL of the extracts was placed on the chromatographic plate (5.0 x 7.0 cm), the absorbent agent used was the silica gel Polygram Sil G/UV254, and the mobile phase wasthe toluene-acetone system at a ratio of 7:3. Aspot of the commercially available actinomycinD, Dactinomycin, was also placed on the sameplate to serve as a standard. In the other production runs, the antibiotic was quantified using the spectrophotometric method reported on by Katz and Weissbach (1963). The concentration of total reducing sugars was measured using the 3.5 dinitrosalicylic acid method (Miller, 1959), while the biomass concentration was measured by quantifying the dry weight. The samples were centrifuged at 2041 g for 20 minutes and the sediment was washed with a 0.1N HCl solution and dried at 105°C until a constant weight was obtained.

Measurement of Rheological Properties

These properties were measured only at the end of the fermentation process at 25±1ºC, using a Brookfield Synchro-Lectric rotary viscometer, model RVT with spindle number 2 and 300mL of the sample at different rotation frequencies (5, 10, 20, 50 and 100 min-1).

 

RESULTS AND DISCUSSION

Figure 2 shows the production of actinomycin by the different species of Streptomyces. S. parvulus had the highest level of antibiotic activity (152 mg/L), followed by S. felleus, which had a maximum concentration of around 20 mg/L, and S. regensis, which did not exceed 12 mg/L. The same figure also shows that the antibiotic production curves reached their maximum values at around 144 h, which is consistent with the findings of Williams and Katz (1977). According to Martin et al. (1979), this is due to the fact that the extent of antibiotic production equals the tolerance of the cells to the antibiotic. In agreement with to Martin and Demain (1980), the cessation of antibiotic biosynthesis may be attributed to one of the following factors: a shortage of intermediate precursors, the feedback effect of the accumulated antibiotic or the irreversible decay of one or more enzymes.

 

 

According to the literature, S. parvulus has the advantage of producing predominantly actinomycin-D (Meienhofer and Atherton, 1973). To prove this statement, thin layer chromatography was prepared for the three microbial species, using Dactinomycin donated by LAFEPE (Laboratório Farmacêutico do Estado de Pernambuco) as a standard. The results of the thin layer chromatography are given in Table 1 andthey show that S. parvulus had only a single band for actinomycin-D, while the other species had five different compounds as well as the antibiotic in question. For this reason the species selected to continue this study was S. parvulus.

 

 

In previous research by Sousa et al. (1997) using the selected species, the production medium initially used was optimized, giving the following composition: soy milk 30 g/L, glucose 20 g/L and CaCO3 2 g/L, for which a maximum concentration of 530 mg actinomycin-D per liter was obtained. When glucose wassubstituted by fructose in the 20, 30 and 40 g/L concentrations, all the antibiotic concentrations were higher after 144 h production than with glucose, as can be seen in Figure 3. Furthermore, the optimum concentration was found to be 30 g fructose per liter, which yielded a maximum value of 635 mg/L.

 

 

Figures 4 and 5 show the concentration profiles for actinomycin-D obtained in the bioreactor using stirring speeds of 300 and 500 rpm, respectively, and different degrees of aeration (0.5 ,1.0 and 1.5vvm). The maximum values registered after 144h fermentation are higher than any that appear in the literature, as detailed below: 740 mg/L (500 rpm; 0.5 vvm), 1152 mg/L (500 rpm; 1.0 vvm), 1530 mg/L (500 rpm; 1.5 vvm), 617 mg/L (300 rpm; 0.5 vvm), 882 mg/L (300 rpm; 1.0 vvm) and 1422 mg/L (300 rpm; 1.5 vvm), resulting in the maximum yields and productivity of actinomycin-D, as can be seen in Table 2. The same table shows that at both stirring speeds (300 and 500 rpm) the aforementioned parameters increase as aeration is increased and that the values obtained at 500 rpm are greater than those at 300 rpm. Figures 4 and 5 also show that the concentration profile for the antibiotic produced at 300 rpm and 1.5 vvm has the highest actinomycin-D values until shortly before 144 h, although at this time, the greatest antibiotic concentration was found for 500 rpm and 1.5 vvm (1530 mg/L). The reason for this could be that at 500 rpm, there is a greater breaking up of air bubbles, resulting in a greater specific contact area for gas-liquid mass transfer, while the increased turbulence in the medium results in the diminished thickness of the gas and liquid films that provide resistance to the aforementioned oxygen mass transport.

 

 

 

 

The typical results obtained in the bioreactor can be seen in Figure 6 (300 rpm and 1.5 vvm), where mycelial growth occurs concomitantly with antibiotic production, rather than following the typical standard for a trophophase-idiophase fermentation of a secondary metabolite (Bu'Lock, 1961). This was also observed by Williams and Katz (1977) in their work with S. parvulus ATCC 12434 in a chemically defined medium.

 

 

So as to make an overall assessment of the results obtained, the histogram in Figure 7 was prepared. It shows an increase of around ten times the antibiotic concentration (from 152 to 1530 mg/L) in a complex medium by applying classic batch production technology, using optimized compositions for the media. This demonstrates how entirely dependent the selected species is on the composition of the culture medium and the operating conditions of the bioreactor in which the experiments are conducted.

 

 

Figure 8 shows the variation of shear stress with the shear rate in a typical experiment, where the concentration of dry weight at the end of a 168h fermentation was 29.1g/L. The rheogram clearly shows that the shape of the curve is typical of a pseudoplastic fluid, therefore obeying the Ostwald-de Waele power law model, in which the values of rheological parameters n and K are as follows: n=0.252 and K=28.423dyn.cm-2.s0.252.

 

 

In their work with three actinomycetes (Saccharopolyspora erythraea, Actinomadura roseorufa and Streptomyces rimosus) that synthesize secondary metabolites of commercial value (erythromycin, anti-coccidiostatic antibiotic and oxytetracycline, respectively), Warren et al. (1995) noted that in submerged cultivation, the rheology of the three broths obeyed pseudoplastic fluid behavior, obtaining values for the power law index (n) of 0.20 to 0.25 and for the consistency index (K) varying from 20 to 70 dyn.cm-2.sn (S. erythraea), 5 to 95 dyn.cm-2.sn (A. roseorufa) and 5 to 70 dyn.cm-2.sn (S. rimosus). The same authors observed that the value of this latter rheological parameter increases with the concentration of biomass, although it decreases at the end of the antibiotic fermentation. Atkinson and Mavituna (1983) report variations in the pseudoplastic characteristics of the medium during the fermentation with Streptomyces aureofaciens, which produces tetracycline, showing values for n of between 0.25 and 0.45 and values for the consistency index K of between 30 and 90 dyn.cm-2.sn.

Banks (1977) explains that the occurrence of pseudoplastic behavior in mycelial suspensions is due to the alignment of the hyphae, which brings about a decrease in the apparent viscosity when high shear rates are applied.

 

CONCLUSIONS

S. parvulus was the species that had the highest level of antibiotic activity and produced only actinomycin-D. Fructose showed to be a better substrate than glucose for the antibiotic production, obtaining a maximum actinomycin-D concentration of 635mg/L for an initial fructose concentration of 30 g/L. The highest yield of actinomycin-D (1530 mg/L) in the bioreactor was obtained with 500 rpm and 1.5 vvm. The production of actinomycin-D did not follow a typical trophophase - idiophase dynamic, but rather a standard kinetic whereby growth is partially associated with product formation. The fermented medium showed rheological behavior typical of a pseudoplastic fluid.

 

ACKNOWLEDGEMENTS

This study received financial support from the Fundação de Amparo à Ciência e Tecnologia do Estado de Pernambuco - FACEPE.

 

NOMENCLATURE

 

REFERENCES

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