Removal of the product from the culture medium strongly enhances free fatty acid production by genetically engineered Synechococcus elongatus
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Cyanobacterial mutants engineered for production of free fatty acids (FFAs) secrete the products to the medium and hence are thought to be useful for biofuel production. The dAS1T mutant constructed from Synechococcus elongatus PCC 7942 has indeed a large capacity of FFA production, which is comparable to that of triacylglycerol production in green algae, but the yield of secreted FFAs is low because the cells accumulate most of the FFAs intracellularly and eventually die of their toxicity. To increase the FFA productivity, enhancement of FFA secretion is required.
Growth of dAS1T cells but not WT cells was inhibited in a liquid medium supplemented with 0.13 g L−1 of palmitic acid. This suggested that when FFA accumulates in the medium, it would inhibit the release of FFA from the cell, leading to FFA accumulation in the cell to a toxic level. To remove FFAs from the medium during cultivation, an aqueous-organic two-phase culture system was developed. When the dAS1T culture was overlaid with isopropyl myristate (IM), the final cell density, cellular chlorophyll content, and the photosynthetic yield of PSII were greatly improved. The total amount of extracellular FFA was more than three times larger than that in the control culture grown without IM, with most of the secreted FFAs being recovered in the IM layer. The cellular FFA content was decreased by more than 85% by the presence of the IM layer. Thus, the two-phase culture system effectively facilitated FFA secretion out of the cell. An average FFA excretion rate of 1.5 mg L−1 h−1 was attained in the 432 h of cultivation, with a total amount of excreted FFA being 0.64 g L−1 of culture. These figures were more than three times higher than those reported previously for the cyanobacteria-based FFA production systems.
Removal of FFA from the culture medium is important for improving the productivity of the FFA production system using cyanobacteria. Further increase in productivity would require an increase in both the rates of FFA production in the cell and active FFA export across the plasma membrane.
KeywordsCyanobacteria Biofuel production Free fatty acids Two-phase culture system
acyl carrier protein
dry cell weight
free fatty acids
small plasmid cured
Photosynthetic microorganisms including cyanobacteria and eukaryotic algae appear to be promising hosts for sustainable biofuel production because they have a high capacity for oxygenic photosynthesis [1, 2]. Actually, some research efforts have reported that their oil yields per unit area are more than three times higher than those of land plants including corn and oil palm [3, 4]. However, commercial success of algae-based biofuel production has not been achieved yet, mainly because of its high processing cost. Although green algae can accumulate triacylglycerol (TAG) in the cells to a level corresponding to 50% of cell dry weight , the high costs in recovery of the cells from the growth medium and extraction of lipid from the cells hamper the commercialization of the TAG-based biofuel production [6, 7].
Unlike TAG production using green algae, production of free fatty acids (FFA) using genetically engineered cyanobacteria results in secretion of the product into the medium [8, 9, 10]. If the rate of FFA secretion is raised to a level comparable to the TAG production rate of algal cultures, the cyanobacterial system would be advantageous over the algal production system as the cost-intensive steps in biofuel extraction can be omitted. Construction of FFA-producing cyanobacterial mutants involves the following two gene manipulations. Firstly, the aas gene coding for acyl-ACP synthetase, which activates FFAs via esterification to acyl carrier protein (ACP), is inactivated to prevent the recycling of the FFAs released from membrane lipids [11, 12]. Secondly, a gene encoding a truncated form of the thioesterase from Escherichia coli (‘tesA)  is introduced to cleave the thioester bond of acyl-ACP . Among the three model cyanobacterial species used for construction of FFA-producing strains, i.e., Synechocystis sp. PCC 6803, Synechococcus elongatus PCC 7942, and Synechococcus sp. PCC 7002, Synechocystis sp. PCC 6803 has been the most successful [8, 9, 10]. In this strain, FFA productivity was successfully increased by the additional gene manipulations aimed at weakening of the peptidoglycan layer, inactivation of the PHB biosynthesis pathway, overexpression of acetyl-CoA carboxylase, and expression of thioesterases from plants and bacteria. The resultant SD277 mutant secreted FFAs at an average rate of 0.44 mg L−1 h−1 for 450 h . However, this figure was still much lower than the rate of TAG production attained by cultures of eukaryotic algae, e.g., Chlorella vulgaris and Nannochloropsis gaditana, ranging from 2 to 3 mg L−1 h−1 [14, 15].
Although all the FFA-producing strains constructed from S. elongatus PCC 7942 were less active in FFA secretion than the SD277 mutant of Synechocystis sp. PCC 6803 [10, 16], Kato et al. found that the dAS1T strain, constructed from S. elongatus PCC 7942 simply by inactivation of aas and introduction of ‘tesA, has a much larger capacity to produce fatty acids; it turned out that unlike the SD277 strain that secrete ~90% of FFA out of the cell , dAS1T retains most of FFA in the cell . Cultures of dAS1T were thus shown to produce FFAs at a rate of 1.9 mg L−1 h−1, while secreting FFA at a rate of 0.35 mg L−1 h−1 . This resulted in intracellular accumulation of FFA to a toxic level, causing cell death in 240 h of cultivation. The total amount of secreted FFA was also less than half of that attained by SD277. Impairment of synthesis of the hydrophilic O-antigen layer on the cell surface partially rescued the early-death phenotype of dAS1T by facilitating FFA release from the cells, suggesting that enhancement of FFA secretion is important for the construction of an efficient and robust FFA production system using S. elongatus .
In this study, we developed an aqueous-organic two-phase culture system to remove FFAs from the medium during cultivation of dAS1T. The rate of FFA secretion and the total amount of secreted FFA in the two-phase system were more than three times higher than those reported for the SD277 strain, verifying the importance of removal of FFAs from the culture medium in the enhancement of FFA production. Effects of the two-phase culture system on growth and FFA productivity of the dAS1T strain are described and the strategy for further improvement of FFA production is discussed.
FFA accumulation in the medium inhibits growth of dAS1T
Aqueous-organic two-phase cultivation with isopropyl myristate alleviated the toxic effects of FFA production on cell growth
Figure 2Ba, b compare the effects of IM on the growth of WT and dAS1T. The growth curves of the WT cells confirmed that IM had no adverse effects on cell growth (Fig. 2Ba). As previously observed , dAS1T cells grew slower than WT cells and died in 240 h of cultivation with complete loss of chlorophyll in the absence of IM (Fig. 2Ba, b). The cellular chlorophyll content of dAS1T was ~60% of the WT level during the first 200 h of cultivation and then sharply declined (Fig. 2Bc). When grown with IM, on the other hand, growth of dAS1T was very much improved and the cells remained green in 240 h (Fig. 2Ba, b), with the chlorophyll content being similar to the WT level during the entire course of cultivation (Fig. 2Bc). At t = 192 h, the photosynthetic yield of PSII, as determined by measuring the Fv/Fm ratio, was close to zero in dAS1T cultivated without the IM layer (Fig. 2Bd), indicating that PSII had been almost completely inactivated, whereas the cells cultivated with IM showed a significant Fv/Fm value, showing the operation of PSII (Fig. 2Bd). These results showed that the presence of the IM layer alleviated the adverse effects of FFA production in dAS1T.
Two-phase culture system facilitated FFA secretion
While the cellular FFA content of dAS1T increased sharply during cultivation in the absence of IM as previously observed (Fig. 3B), it remained low in the presence of the IM layer during the entire course of cultivation (Fig. 3B). These results indicated that extraction of FFA by IM from the culture medium facilitated secretion of FFA from the FFA-producing cells, allowing for robust growth of the cells up to t = 240 h.
Figure 3C shows the effects of IM on the yield of extracellular FFA per dry cell weight (DCW). In the presence of the IM layer, dAS1T excreted 0.22 ± 0.01 g of FFA per g of DCW in 240 h, which was 60% higher than the yield in the absence of IM (0.14 ± 0.01 g of FFA per g of DCW). Thus, the two-phase culture system increased the per-cell production of FFA.
Two-phase culture system allowed for sustained production of FFA
The FFA-producing strains constructed from S. elongatus PCC 7942 die out under high-light conditions due to intracellular accumulation of excess FFA, which results from the slower rate of FFA excretion as compared to the rate of FFA production in the cell . We previously showed that FFAs can be secreted by both active transport and passive diffusion. S. elongatus PCC 7942 has two gene clusters encoding respectively a membrane component and a periplasmic component of a tripartite efflux pump of the resistance-nodulation-cell division (RND) family. Targeted disruption of one of these (rndA1–rndB1) rendered the cells highly sensitive to FFAs, indicating its involvement in FFA export . Passive efflux of FFA was stimulated by removal of the hydrophilic O-antigen layer on the cell surface by gene manipulation . However, the enhancement of passive efflux or that of the active FFA export could only partially rescue the growth defect of the FFA-producing strains [16, 21]. By contrast, the aqueous-organic two-phase culture system effectively enhanced FFA secretion and remarkably improved growth of the dAS1T strain (Figs. 2B, 3A, B). This is probably due to facilitation of passive diffusion of FFAs. The amount of FFA in the aqueous phase was decreased by the presence of the IM layer to 30% of that of the control culture, which seemed to have helped maintaining the FFA concentration gradient across the plasma membrane. These results indicated that removal of FFA from the culture medium is essential for the enhancement of FFA secretion and hence of FFA production.
The FFA productivity obtained with the dAS1T cultures overlaid with IM was the highest ever reported for cyanobacterial FFA-producing mutants. The cells excreted 0.64 g of FFA per L of culture in 432 h with an average FFA excretion rate of 1.5 mg L−1 h−1 (Fig. 4b). These figures are more than three times larger than those reported for the SD277 mutant of Synechocystis sp. PCC 6803, i.e., 0.20 g L−1 and 0.44 mg L−1 h−1 , and about five times larger than those reported for the S07 mutant of Synechococcus sp. PCC 7002, i.e., 0.13 g L−1 and 0.27 mg L−1 h−1 . Unlike dAS1T, SD277 and S07 have some gene manipulations in addition to inactivation of aas and introduction of ‘tesA. Increasing the activity of the CO2 fixation and fatty acid biosynthesis pathways were required in order to maximize FFA production [8, 9]. Since much higher FFA productivity was achieved in dAS1T simply by enhancement of FFA secretion, it is deduced that S. elongatus PCC 7942 naturally has a large capacity of CO2 fixation and fatty acid biosynthesis.
Ruffing previously reported that overexpression of ribulose-1, 5-bisphosphate carboxylase/oxygenase and acetyl-CoA carboxylase had adverse effects on the growth of S. elongatus FFA-producing mutants , effects of which can be accounted for by the toxic effect of enhanced accumulation of intracellular FFA. The observation also indicates that fatty acid biosynthesis activity of dAS1T can be further enhanced by these gene manipulations. To fully exploit the enhanced activity of fatty acid biosynthesis for FFA production, it would be required to enhance cellular activity of active FFA export. Even in the two-phase cultivation system, the color of the dAS1T cells but not the WT cells became slightly bluish at t = 432 h (Fig. 4a) and died in 450 h of cultivation (data not shown), suggesting intracellular accumulation of FFA after prolonged cultivation. Functional expression of FFA transporters is not simple in cyanobacteria , but is essential for further increase of the FFA productivity.
FFA-producing cyanobacterial mutants secrete FFA, but accumulation of FFA in the medium interferes with the release of FFA from the cell. In the dAS1T mutant constructed from S. elongatus PCC 7942, intracellular FFA increases to a lethal level due to its large capacity of fatty acid biosynthesis. Removal of FFA from the medium facilitates FFA release from dAS1T cells and rescues them from FFA toxicity, enhancing the productivity of extracellular FFA to the highest level ever reported for cyanobacteria. Further increase of FFA production would require an enhancement of active FFA transport out of the cell.
Strains and growth conditions
A derivative of S. elongatus PCC 7942, which is cured of the resident small plasmid pUH24 (SPc), was used as WT in this study . The FFA-producing strain designated as dAS1T was the aas-deficient mutant expressing a foreign thioesterase gene from E. coli (‘tesA) transcriptionally fused to the nirA promoter of S. elongatus PCC7942 . The basal medium used in this study was a modification of the BG11 medium  prepared as described by Suzuki et al. . The medium was buffered with 20 mM HEPES–KOH (pH 8.2) and supplemented with 15 mM KNO3 as a nitrogen source and when appropriate, supplemented with 0.1% ethanol and 0.13 g L−1 of palmitic acid (PA). WT and dAS1T cells were grown at 30 °C under high-light conditions (180 µE m−2 s−1) with aeration with 2% (vol/vol) CO2. In all the experiments, cells precultured under low-light conditions (50 µE m−2 s−1) to the exponential phase of growth (OD730 = 0.5–1.5) were used for inoculation of fresh medium, because the PSII activity of dAS1T sharply declines during the stationary phase of growth under the high-light conditions . For two-phase cultivation of cyanobacterial cells, 50 mL of culture was overlaid with 20 mL of IM unless otherwise stated.
Optical density at 730 nm (OD730) of the cultures was determined using a Shimadzu UV1700 spectrophotometer. Dry weight of cyanobacterial biomass in liquid cultures was estimated from OD730 of the cultures (Additional file 1: Figure S1). To determine the relationship between OD730 and dry cell weight (DCW) in a unit volume of culture, 10 mL aliquots of the cultures of various cell density (OD730 = 2.0–13.8) were vacuum-filtered through a pre-weighed MF-Millipore™ Membrane Filter (pore size: 0.45 µm, Merck Millipore). The cells on the filter were washed three times with 10 mL of deionized water and then dried at 75 °C until constant weight was reached. When DCW of the cultures overlaid with IM was measured, cells from 10 mL aliquots of the cultures were collected by centrifugation at 1700g for 10 min and washed three times with 10 mL of deionized water by resuspension and recentrifugation before vacuum filtration so that the effects of contaminating IM is minimized. For estimation of the amount of IM absorbed to the membrane filter, the BG-11 medium was overlaid with IM without cyanobacterial cells and incubated just as the cyanobacterial cultures. The IM-treated medium was passed through a pre-weighted membrane filter, and the filter was washed and dried for weighing. Twenty-six sets of data obtained with independent cultures were fitted to a linear relationship (y = 0.255x − 0.144, r 2 = 0.942) (Additional file 1: Figure S1), which was used for estimation of the cell dry matter content of a culture from the OD730 value.
Chlorophyll was determined as described by Mackinney  and the content was normalized to OD730. The photosynthetic yield of PSII was determined using an AquaPen-C fluorometer (AP-C100, Photon Systems Instruments).
The concentration of FFA in the culture medium (or the aqueous layer in the two-phase cultivation system) and the cellular FFA content were determined as described by Kato et al. . The concentration of FFA in the IM layer was enzymatically determined using the Free Fatty Acid Quantification Kit (BioVision) as follows. 1 μL aliquots of the IM layer was mixed with 49 μL of Assay Buffer in the kit in a 96-well plate and then analyzed according to the manufacturer’s instruction. The volume of the IM layer used for FFA determination was limited to one-fiftieth of the assay mixture, because larger amounts of IM caused artifactual coloration at 570 nm in the absence of FFA (Additional file 2: Figure S2). Absorbance at 570 nm was measured using a Multiskan™ GO microplate spectrophotometer (Thermo Fisher Scientific). A standard curve for FFA was generated for each measurement, using a concentration series of PA dissolved in IM (0, 2, 4, 6, 8, 10 mM) (Additional file 3: Figure S3). The amount of FFA in the IM layer was normalized to the culture volume and expressed in g L−1.
AK designed and executed the experiments, participated in data analysis and drafting the manuscript. NT helped to design the experiments and participated in drafting the manuscript. KI performed the analysis of cellular FFA content using LC–MS and analyzed the data. SM helped to design the experiments. TO supervised and coordinated the study, and helped to draft the manuscript. All authors read and approved the manuscript.
The authors declare that they have no competing interests.
Availability of data and materials
The data that support the findings of this study are included within the article and its additional files.
This study was supported by the Japan Science and Technology Agency CREST funding program in the area of 'Creation of Basic Technology for Improved Bioenergy Production through Functional Analysis and Regulation of Algae and Other Aquatic Microorganism.'
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