Relationship between morphology and docosahexaenoic acid production by Schizochytrium sp. BCC 25505 and 25509 in batch and pulsed-batch cultivation.
The largest source of PUFAs, especially DHA, comes from marine fish, but other organisms also can synthesize DHA at high yields, including Aurantiochytrium (9), Crypthecodinium cohnii (10-12), and thraustochytrids (13-18). Thraustochytrids are marine protists, whose dominant genera are Thraustochytrium, Aurantiochytrium and Schizochytrium and belong to the kingdom Chromista (16). Schizochytrium sp. can synthesize PUFAs containing 30-40% DHA (19-22) and has become an industrial source of DHA (23).
Cultivation of Schizochytrium for industrial production of DHA involves two phases: cell growth (biomass production) and lipid accumulation. The early stage of cell growth is dependent on nitrogen supply and the later stage of cell enlargement for lipid accumulation on carbon supply (24-25) (Figure 1). In order to achieve high accumulation of lipids and DHA production, synchronous Schizochytrium cell morphologies have to be controlled during both phases of growth at high cell density and lipid accumulation (26).
Although Schizochytrium is an established microorganism for the commercial production of long-chain PUFAs including DHA at low cost, there is still a need to develop an optimal fermentation process that can provide increased biomass via high-cell density cultivation (6, 25). In the present study, the relationship between Schizochytrium sp. morphology and DHA production in batch and pulsed-batch fermentation processes were compared. Morphological control using pulsed-batch cultivation was investigated.
MATERIALS AND METHODS
Schizochytrium sp. BCC 25505 and BCC 25509, marine protists, were collected from mangrove leaf in the gulf of Thailand and identified by Dr. Panida Unagul, National Center for Genetic Engineering and Biotechnology (BIOTEC), National Science and Technology Development Agency, Thailand. The microbes were deposited in BIOTEC Culture Collection. Schizochytrium sp. BCC 25505 and BCC 25509 were maintained at 22 [degrees]C by monthly sub-cultivation on GPY medium (glucose 10 g/L; peptone 1 g/L; yeast extract 1 g/ L) supplemented with 15 g/L agar (Difco, Franklin Lakes, USA) and 15 g/L artificial sea salts (Sigma, St. Louis, USA). Schizochytrium sp. BCC 25509 had higher growth rate and higher lipid content than BCC 25505.
Schizochytrium sp. BCC 25505 and BCC 25509, stored in 20% (v/v) glycerol at -80[degrees]C, were grown in GYP medium (20 g/L glucose, 10 g/L peptone and 5 g/L yeast extract) at 28[degrees]C for 3 days. Seed cultures were prepared in a basal medium comprising of 40 g/L glucose, 17.57 g/L yeast extract, 2.56 g/L ammonium dihydrogen phosphate, 12.32 g/L MgS[O.sub.4].7[H.sub.2]O, 1 mL/L Ami G (waste from glutamic acid production; Ajinomoto Co., Ltd, Samutprakarn, Thailand), and 1 mL/L multivitamins complex (Blackmores, NSW, Australia), on a rotary shaker (250 rpm) at 28[degrees]C for 24-36 h. A 10% (v/v) inoculum was used as starter culture in each experiment.
Medium used in a 5-L batch bioreactor (B. Braun, Goettingen, Germany) consisted of 40 g/L glucose, 17.57 g/L yeast extract, 2.56 g/L ammonium dihydrogen phosphate, 12.32 g/L MgS[O.sub.4].7[H.sub.2]O, 1 mL/L Ami G, and 1 mL/L vitamins complex, with a working volume of 3.5 L, cultivation temperature of 28[degrees]C, agitation at 300 rpm, aeration rate of 1 vvm and cultivation for 2-3 days. A 1 mL aliquot of fermentation broth was removed every 3 h for measurements of dry weight, residual glucose concentration, Schizochytrium sp. morphology, and DHA and TFA contents.
When 1-5 g/L glucose was left in the fermentation broth of the batch cultivation, fresh medium (800 g/L glucose, 12 g/L sodium nitrate, 0.5 g/L KCl, 2.0 g/L MgS[O.sub.4].7[H.sub.2]O, 0.65 g/L [K.sub.2]S[O.sub.4], 3.0 g/L K[H.sub.2]P[O.sub.4], 10 g/L [(N[H.sub.4]).sub.2]S[O.sub.4], 0.17 g/L Ca[Cl.sub.2].2[H.sub.2]O, 3.0 g/L yeast extract, 10.0 g/L N[H.sub.2][H.sub.2]P[O.sub.2], 1 mL/L vitamins solution, 0.35 mL/L antifoam (PMX-200, Dow Corning, MI, USA), and 1 mL/L trace solution (4.5 g/L Ca[Cl.sub.2].2[H.sub.2]O, 0.3 g/L Co[Cl.sub.2].6[H.sub.2]O, 0.3 g/L CuS[O.sub.4].5[H.sub.2]O, 3.0 g/L FeS[O.sub.4].7[H.sub.2]O, 1.0 g/L [H.sub.3]B[O.sub.4], 0.1 g/L KI, 1.0 g/L Mn[Cl.sub.2].4[H.sub.2]O, 0.4 g/L NaMo[O.sub.4].2[H.sub.2]O, 4.5 g/L ZnS[O.sub.4].7[H.sub.2]O) was pulsed into the bioreactor to obtain a medium of 40 g/L glucose.
Dry biomass determination
Cells were harvested by centrifugation at 10.000 g for 5 min and washed twice with distilled water followed by freeze-dried in pre-weighed tubes for 72-96 h. Tubes were weighed and the amounts of dry biomass calculated.
Fatty acid extraction and analysis
Two mL aliquot of 4% sulfuric acid in methanol containing butylated hydroxytoluene (0.1 g/L) (as anti-oxidant) and C17:0 (as internal standard) was added to freeze-dried cell pellet (10-20 mg) in a vial equipped with tightly fitting Teflonlined cap, and incubated at 90[degrees]C for 1 h. Following rapid cooling, the produced fatty acid methyl esters were extracted twice with 2 ml of hexane:water (1:1) solution and a few grains of sodium sulfate were added to the hexane layer to absorb any remaining water. Then the hexane sample was injected using an auto-injector with a 1:100 split into a Shimadzu GC-17A instrument (Osaka, Japan) equipped with Supelco Omegawax-250 (Supelco, Bellefonte, USA) fused silica capillary column (30 m in length, 0.25 mm internal diameter). Injector and detector temperature was 250 and 260[degrees]C respectively. Carrier gas was helium with a linear flow of 30 cm/s. Column temperature was kept at 200[degrees]C for 10 min and then increased to 230[degrees]C at a rate of 10[degrees]C/min. After 17 min at 230[degrees]C, the column was cooled to 200[degrees]C and a new cycle initiated. Calibration was performed using a mixture of fatty acid methyl ester (FAME) standards (Sigma no 189-19) as well as DHA-FAME (Sigma). In addition, the procedure was tested using methylated C17:0 and DHA (Sigma) and recovery was determined against FAME standards.
Protist morphologies were visualized under a compound microscope (Leica Microsystems CMS GmbH, Germany) (400x magnification) and counted using a hematocytometer.
Supernatant was centrifuged at 10,000 g for 10 min and filtered through a 0.22 pm paper filter (Millex, MA, USA). Filtrate was subjected to HPLC analysis using Aminex HPX-87H column (Bio-Rad, Hercules, Calif.) in a (Waters, MA, U SA) equipped with a Waters 410 differential refractometer detector (Millipore Corp., Milford, MA, USA) at 60[degrees]C using 5 mM [H.sub.2]S[O.sub.4] as a mobile phase at a flow rate of 0.6 mL/min.
RESULTS AND DISCUSSION
DHA production by Schizochytrium sp. BCC 25505 and BCC 25509 in 5-L batch bioreactor
Batch cultivation in a 5-L bioreactor of Schizochytrium sp. BCC 25505 and BCC 25509 produced highest biomass of 38.7 [+ or -] 0.14 g/L at 72 h and 41.35 [+ or -] 0.46 g/L at 72 h (Fig. 2A and 3A), complete glucose consumption after 63 h with highest DHA yield of 5.9 [+ or -] 1.56 g/L and after 54 h with 12.09 [+ or -] 0.81 g/L (at 69 h) (Fig. 2B and 3B), and highest total fatty acid content of 13.03 [+ or -] 0.09 g/L at 54 h with DHA/TFA ratio ranging from 27.3 to 50.75% and 26.32 [+ or -] 2.28 g/L at 66 h with ratio ranging from 24 to 53% (Fig. 2B and 3B), respectively.
For Schizochytrium sp. BCC 25505, 67100% vegetative cells were observed throughout the first 60 h of cultivation but decreased thereafter. When glucose was completely consumed (after 63 h), increasing numbers of zoospores were observed (Fig. 4A). As for Schizochytrium sp. BCC 25509, 70-100% vegetative cells were observed throughout 72 h of cultivation (Fig. 4B).
The medium used in this study is optimized for growth and DHA production of Schizochytrium sp., in which high concentrations (50 mM) of magnesium salts are included to maintain osmotic pressure in order to allow the protists to grow synchronously as vegetative cells in a medium of high nitrogen content followed by that of high carbon content for lipid production (26). Synchronous vegetative growth of Schizochytrium sp. BCC 25505 and BCC 25509 were obtained during the early phase (48 h) in the condition of nitrogen excess, and low amounts of DHA and TFA were synthesized. During the later phase of excess of carbon source from non-glucose repression medium, lipid accumulation occurred resulting in higher DHA and TFA content. The higher number of synchronous vegetative Schizochytrium sp. BCC 25509 cells compared to BCC 25505 accounts for the better performance of the former strain in terms of biomass, DHA and TFA production.
DHA production by Schizochytrium sp. BCC 25505 and BCC 25509 in 5-L pulsed-batch bioreactor
Pulsed-batch cultivation in a 5-L bioreactor of Schizochytrium sp. BCC 25505 and BCC 25509 produced the highest biomass of 97.05 [+ or -] 1.63 g/L at 166 h and 101.75 [+ or -] 2.19 g/L at 166 h (Fig. 5A and 6A), highest DHA yield of 20.73 [+ or -] 1.21 at 166 h and 20.0 [+ or -] 1.31 g/L at 143 h, highest total fatty acid content of 35.24 [+ or -] 3.27 at 166 h and 36.48 [+ or -] 3.97 g/L g/L at 118 h (Fig. 5B and 6B), and DHA/ TFA ratio of 40% and 35-44% (Fig. 5A and 6A), respectively. For Schizochytrium sp. BCC 25505, 57-86% vegetative cell were observed during 166 h of cultivation but amoeboid cells, with 2, 4 and 6 partitions, were found thereafter (Fig. 7A). As for Schizochytrium sp. BCC 25509, 72-94% vegetative cells were observed during 166 h of cultivation (Fig 7B). At 166 h of fed-batch cultivation, Schizochytrium sp. BCC 25505 and BCC 25509 had larger lipid- accumulating cells compared to those in the earlier stages of cultivation (Fig. 8). The majority of Schizochytrium sp. cells were maintained at the vegetative stage throughout the pulsed-batch cultivation process.
In pulsed-batch cultivation, both strains had similar numbers of vegetative cells and production of DHA, but different TFA content, and this might be due to the non-glucose repression level. Under stress conditions of glucose depletion and glucose repression, protist morphologies changed to other stages (viz. zoospores and released zoospores) resulting in lower DHA production. As Schizochytrium is a slow growing heterotroph consuming glucose at a slow rate, wai cultivation in a non carbon catabolite repression condition or in an increased acetyl-CoA synthethase state gives rise to higher growth and glucose consumption rates (27). Similar findings have been reported regarding excess nitrogen supply for optimal cell growth and excess carbon feeding for cell enlargement to accommodate lipid accumulation (24). Synchronous growth of Schizochytrium limacinum SR21 affects lipid and fatty acid composition (28). Fed-batch process of high cell density has been reported to be the more efficient in DHA production by Schizochytrium sp. compared with batch process (25).
Thus, in order to obtain high DHA production by Schizochytrium sp., early phase synchronous vegetative growth has to be maintained by supplying high nitrogen content, which is then followed by controlled high glucose supply to allow size enlargement of vegetative cells for lipid accumulation. This strategy is recommended for high cell density cultivation of oleaginous protists for industrial production of polyunsaturated fatty acids, especially E-3 fatty acids such as DHA.
This research project was financially supported by Cluster and Program Management Office (CPMO), National Science and Technology Development Agency (NSTDA), Thailand. The authors thank Prof. Prapon Wilairat for assistance in the English writing.
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Wai Prathumpai * and Pranee Rachtawee
Bioresources Technology Unit, National Center for Genetic Engineering and Biotechnology, National Science and Technology Development Agency, 113 Thailand Science Park, Paholyothin Rd., Klong Nueng, Klong Luang, Pathum Thani, 12120, Thailand.
(Received: 19 May 2016; accepted: 20 July 2016)
* To whom all correspondence should be addressed.
Tel: +66 2564 6700 ext. 3525-6; Fax: +66 2564 6707; E-mail: email@example.com
Caption: Fig. 1. Growth and lipid accumulation phases of oleaginous microorganisms.
Caption: Fig. 2. Time profile of (A) glucose concentration, dry weight (DW), and ratio of docosahexaenoic acid (DHA)/total fatty acid (TFA) and of (B) DHA and TFA of Schizochytrium sp. BCC 25505 cultivated in a 5-L batch bioreactor
Caption: Fig. 3. Time profile of (A) glucose concentration, dry weight (DW), ratio of docosahexaenoic acid (DHA)/ total fatty acid (TFA) and of (B) DHA and TFA of Schizochytrium sp. BCC 25509 cultivated in 5-L batch bioreactor
Caption: Fig. 4. Time profile of morphology of (A) Schizochytrium sp. BCC 25505 and (B) Schizochytrium sp. BCC 25509, during batch cultivation in 5-L bioreactor.
Caption: Fig. 5. Time profile of docosahexaenoic acid (DHA), total fatty acid (TFA), ratio of DHA/TFA, glucose concentration and dry weight (DW) of Schizochytrium sp. BCC 25505 cultivated in a 5-L pulsed-batch bioreactor
Caption: Fig. 6. Time profile of docosahexaenoic acid (DHA), total fatty acid (TFA), ratio of DHA/TFA, glucose concentration and dry weight (DW) of Schizochytrium sp. BCC 25509 cultivated in 5-L pulsed-batch bioreactor.
Caption: Fig. 7. Time profile of morphology of (A) Schizochytrium sp. BCC 25505 and (B) Schizochytrium sp. BCC 25509, during batch cultivation in a 5-L bioreactor.
Caption: Fig. 8. Cell morphology of Schizochytrium sp. BCC 25505 and BCC 25509 during pulsed-batch cultivation visualized under a light microscope (400x). Schizochytrium sp. BCC 25505: (A) 0 h, (B) 24 h, (C) 70 h, (D) 166 h. Schizochytrium sp. BCC 25509: (E) 0 h, (F) 24 h, (G) 70 h, (H) 166 h
Table 1. Maximum biomass, docosahexaenoic acid (DHA), total fatty acid (TFA) and amount of vegetative cells of Schizochytrium sp. BCC 25505 and BCC 25509 in batch and pulsed-batch fermentation processes Variable Schizochytrium sp. BCC 25505 Batch Pulsed-batch Biomass (g/L) 38.70 [+ or -] 0.14 97.05 [+ or -] 1.63 DHA (g/L) 5.90 [+ or -] 1.56 20.73 [+ or -] 1.21 TFA (g/L) 13.03 [+ or -] 0.09 35.24 [+ or -] 3.27 Vegetative cells (%) 60-100 57-86 Average vegetative 82.10 [+ or -] 15.31 71.32 [+ or -] 10.12 cells (%) Variable Schizochytrium sp. BCC 25509 Batch Pulsed-batch Biomass (g/L) 41.35 [+ or -] 0.46 101.75 [+ or -] 2.19 DHA (g/L) 12.09 [+ or -] 0.81 20.00 [+ or -] 1.31 TFA (g/L) 26.32 [+ or -] 2.28 36.48 [+ or -] 3.97 Vegetative cells (%) 70-100 72-94 Average vegetative 89.50 [+ or -] 8.90 73.17 [+ or -] 20.64 cells (%)
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|Author:||Prathumpai, Wai; Rachtawee, Pranee|
|Publication:||Journal of Pure and Applied Microbiology|
|Date:||Sep 1, 2016|
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