Metabolic modelling of polyhydroxyalkanoate copolymers production by mixed microbial cultures
- João ML Dias†1,
- Adrian Oehmen†1,
- Luísa S Serafim†1,
- Paulo C Lemos†1,
- Maria AM Reis†1 and
- Rui Oliveira1Email author
© Dias et al; licensee BioMed Central Ltd. 2008
Received: 31 January 2008
Accepted: 08 July 2008
Published: 08 July 2008
This paper presents a metabolic model describing the production of polyhydroxyalkanoate (PHA) copolymers in mixed microbial cultures, using mixtures of acetic and propionic acid as carbon source material. Material and energetic balances were established on the basis of previously elucidated metabolic pathways. Equations were derived for the theoretical yields for cell growth and PHA production on mixtures of acetic and propionic acid as functions of the oxidative phosphorylation efficiency, P/O ratio. The oxidative phosphorylation efficiency was estimated from rate measurements, which in turn allowed the estimation of the theoretical yield coefficients.
The model was validated with experimental data collected in a sequencing batch reactor (SBR) operated under varying feeding conditions: feeding of acetic and propionic acid separately (control experiments), and the feeding of acetic and propionic acid simultaneously. Two different feast and famine culture enrichment strategies were studied: (i) either with acetate or (ii) with propionate as carbon source material. Metabolic flux analysis (MFA) was performed for the different feeding conditions and culture enrichment strategies. Flux balance analysis (FBA) was used to calculate optimal feeding scenarios for high quality PHA polymers production, where it was found that a suitable polymer would be obtained when acetate is fed in excess and the feeding rate of propionate is limited to ~0.17 C-mol/(C-mol.h). The results were compared with published pure culture metabolic studies.
Acetate was more conducive toward the enrichment of a microbial culture with higher PHA storage fluxes and yields as compared to propionate. The P/O ratio was not only influenced by the selected microbial culture, but also by the carbon substrate fed to each culture, where higher P/O ratio values were consistently observed for acetate than propionate. MFA studies suggest that when mixtures of acetate and propionate are fed to the cultures, the catabolic activity is primarily guaranteed through acetate uptake, and the characteristic P/O ratio of acetate prevails over that of propionate. This study suggests that the PHA production process by mixed microbial cultures has the potential to be comparable or even more favourable than pure cultures.
Polyhydroxyalkanoates are biopolymers with physico-chemical properties similar to polypropylene but with the advantage of being biodegradable and biocompatible. Industrial PHA production technology is currently based on bacteria cultivation using pure cultures grown in well-defined nutrient deficient synthetic media with single substrates . The relatively high production costs constitute presently the most important barrier to PHA becoming a commodity polymer in direct competition with oil-based polymers. The cost of the substrate and of the equipment required for aseptic operation is responsible for about 40% of the total PHA production cost .
Potential strategies for reducing both the operational and capital expenses of PHA production are the use of open mixed cultures of microorganisms instead of pure cultures, and the use of waste materials as the carbon substrate. Activated sludge is known to accumulate up to 65% PHA per cell dry weight [2–4]. There are currently many possibilities of industrial and agricultural wastes that could be directed to the production of PHA on the basis of open mixed microbial systems [5, 6].
The properties and quality of PHA are highly dependent on the monomeric composition, which, in turn, is dependent on the VFA mixture adopted as carbon source. PHB is a relatively low quality polymer since it is too brittle for many applications [1, 11]. In terms of PHA processing, the production of copolymers appears to be of higher commercial interest [12–14]. The production of PHB homopolymer and copolymers of 3-hydroxybutyrate (3HB), 3-hydroxyvalerate (3HV) and 3-hydroxy-2-methylvalerate (3H2MV) from mixtures of acetic and propionic acid has been studied by several researchers [11, 15–17]. There are, however, no metabolic models currently available describing the production of such copolymers. Metabolic models can be used to facilitate process optimization, and also serve as a reference basis in the interpretation of data arising from the study of biological processes. The comparison of experimentally-determined stoichiometry with the theoretical model predictions allows a better understanding of the processes under study. The main objective of this work was to extend existing PHB models [8, 10] to the production of PHA copolymers from mixtures of VFA. This study will be focused on the PHA production phase, and is confined to mixtures of acetic and propionic acid, which are seen as the most promising for the synthesis of high quality PHAs [11, 18].
A schematic of the metabolic model developed in this study is shown in Figure 1. Acetate and propionate are taken up inside the cell, and used for PHA production and biomass growth. Energy is generated within the cells through oxidative phosphorylation, while a portion of this energy is also necessary for cell maintenance. A detailed description of the biochemical reactions, material and energy balances, kinetic reactions and metabolic fluxes is provided below.
Metabolic model of PHA production from mixtures of acetate and propionate by mixed microbial cultures
R 1 : Acetate Uptake
CH2O + ATP → CHO0.5 + 0.5·H2O
R 2 : Propionate Uptake
+ 0.67·ATP → + 0.33·H2O
R 3 : Propionyl-CoA converted to Acetyl-CoA
1.5· + H2O → CHO0.5 + 1.5·NADH2 + 0.5·CO2
R 4 : Growth on Acetyl-CoA
1.27·CHO0.5 + 0.2·NH3 + K1·ATP + 0.3·H2O → CH1.4N0.2O0.4 + 0.53·NADH2 + 0.27·CO2
R 5 : Growth on Propionyl-CoA
1.06· + 0.2·NH3 + K2·ATP + 0.17·H2O → CH1.4N0.2O0.4 + 0.47·NADH2 + 0.06·CO2
R 6 : Catabolism
CHO0.5 + 1.5·H2O → CO2 + 2·NADH2 + 0.5·ATP
R 7 : Maintenance
ATP → mATP
R 8 : Oxidative Phosphorylation
NADH2 + 0.5·O2 → H2O+δ·ATP
R 9 : Acetyl-CoA* Production
CHO0.5 + 0.25·NADH2 → CH1.5O0.5
R 10 : Propionyl-CoA* Production
+ 0.17·NADH2 →
R PHB : PHB Production
CH1.5O0.5 → PHB
R PHV : PHV Production
0.4·CH1.5O0.5 + 0.6· → PHV
R PH2MV : PH2MV Production
While acetate is converted to acetyl-CoA and propionyl-CoA is produced from propionate, it has also been observed that a portion of the propionyl-CoA produced from propionate uptake is converted into acetyl-CoA . This transformation may potentially proceed through 5 different biochemical pathways , however, the net material and reducing power transformations are identical through each pathway. The difference between the pathways lies only in the amount of energy generated. For the purposes of this model, it was assumed that propionyl-CoA was first converted to succinyl-CoA via the methylmalonyl-CoA pathway, then converted to oxaloacetate, pyruvate and acetyl-CoA. The net reaction is described in R3.
In PHA production, acetyl-CoA and propionyl-CoA are reduced and condensed to produce a polymer consisting of various 3-hydroxyalkanoates (3HAs) monomers. 3HB is formed from 2 acetyl-CoA monomers, one acetyl-CoA and one propionyl-CoA combine to form either 3HV or 3-hydroxy-2-methylbutyrate (3H2MB) (which are isomers of each other, and henceforth expressed only as 3HV, indicating the sum of these 2 compounds), while 2 propionyl-CoA monomers form 3H2MV. The fraction of each PHA monomer produced by the cells depends on the fluxes of acetyl-CoA and propionyl-CoA available for polymer production. It also depends on whether the cells tend to reduce and condense acetyl-CoA and propionyl-CoA in a random fashion, or whether preferential binding occurs between e.g. acetyl-CoA and propionyl-CoA. For the purposes of metabolic model development, however, it is necessary to express each reaction in relation to the overall mass, energy and redox transformations. Thus, it is more convenient to express the various potential PHA fractions produced by the cells in terms of the reduced and condensed monomers produced from acetyl-CoA or propionyl-CoA. As shown in R9 and R10, these monomers are represented as acetyl-CoA* and propionyl-CoA*, respectively, in a similar fashion as expressed by a previous study . The PHA formation process from acetyl-CoA* and propionyl-CoA* has no further demand for energy or reducing power.
Biomass growth occurs from acetyl-CoA and propionyl-CoA, respectively. The energy required for the production of 1 C-mol of biomass from acetyl-CoA is represented as K1, which has been estimated as 1.7 mol ATP . The reaction of biomass growth from acetyl-CoA was determined through stoichiometric and redox balancing, and is shown in R4. The amount of energy required for biomass synthesis from propionyl-CoA is represented as K2, which has been estimated to be 1.38 mol ATP per C-mol of biomass formed . Similarly, it was assumed that propionyl-CoA is converted to succinyl-CoA for biomass synthesis . The net reaction is shown in R5. The biomass formula was assumed to be CH1.4O0.4N0.2 .
Catabolism of acetyl-CoA and propionyl-CoA also occurs in the microbial cells. Acetyl-CoA is converted to CO2 through the tricarboxylic acid cycle (TCA) as described in R6 . The catabolism of propionyl-CoA is assumed to occur via acetyl-CoA, where R3 is followed by R6.
Energy in the form of ATP is produced from NADH2 through oxidative phosphorylation. The amount of ATP generated per mole of NADH2 oxidized is expressed by the P/O ratio, δ, which represents the efficiency of oxidative phosphorylation . This reaction is expressed in R8.
In addition to the energetic transformations described above, energy is also required for cell maintenance. The rate of ATP consumption for maintenance purposes is described in R7 as mATP.
Pseudo steady-state material balancing of intracellular intermediates
The metabolic network of Figure 1 has q = 13 metabolic reactions, m = 6 intracellular metabolites (marked by dashed lines), 4 input substrates (acetic and propionic acid, ammonia and oxygen) and 5 end-products [biomass, PHB, poly(3-hydroxyvalerate) (PHV), poly(2-methyl-3-hydroxyvalerate) (PH2MV) and CO2]. The steady state material balances to the m intracellular intermediates (acetyl-CoA, acetyl-CoA*, propionyl-CoA, propionyl-CoA*, NADH2 and ATP) are:
Ac-CoA: R1 + R3 - 1.27·R4 - R6 - R9= 0
Ac-CoA*: R9 - R PHB - 0.4·R PHV = 0
Prop-CoA: R2 - 1.5·R3 - 1.06·R5 - R10 = 0
Prop-CoA*: R10 - 0.6·R PHV - RPH 2MV= 0
NADH 2 : 1.5·R3 + 0.53·R4 + 0.47·R5 + 2·R6 - R8 - 0.25·R9 - 0.17·R10 = 0
ATP: -R1 - 0.67·R2 - K1·R4 - K2·R5 + 0.5·R6 - R7 + δ·R8 = 0
Constraints to the metabolic network
From acetyl-CoA* and propionyl-CoA*, the resulting PHA polymer can be comprised of either PHB (2 acetyl-CoA* molecules), PHV (one acetyl-CoA* and one propionyl-CoA*) and PH2MV (2 propionyl-CoA*). The PHA composition depends on whether selective or random condensation of acetyl-CoA* and propionyl-CoA* takes place. In the propionate enriched culture selective condensation was observed, where acetyl-CoA* preferentially bounds with propionyl-CoA*, forming PHV . Since acetyl-CoA* was generated in higher abundance than propionyl-CoA*, the remaining acetyl-CoA* condensed to form PHB, while PH2MV was not produced by the sludge. This selective condensation is expressed by the following three additional equations:
RPH 2MV= 0 (2c)
since RPH 2MV= 0 (Eq. 2c), Eqs. (2a–b) are linearly dependent to Eqs. (1a–f), only a single additional constraint is introduced with RPH2MV = 0.
In the acetate enriched culture, the PHA composition consisted of a lower PHV fraction and a higher PH2MV and PHB fraction, as is expected by microorganisms performing random condensation of acetyl-CoA* and propionyl-CoA*. In this latter case the following three equations are applied :
The R9 and R10 fluxes are sufficient to calculate the fluxes of R PHB , R PHV and RPH 2MV.
On the other hand, constraints (3a–c) automatically obey the material balances (1a–f) (see  for details), thus also a single additional constraint can also be added to the material balances here (1a–f).
Dynamic material balancing of substrates and end-products
The transient material balances in a batch system of input substrates (acetate, propionate, active biomass, ammonia) and intracellular contents of PHB, PHV and PH2MV are the following:
Theoretical yields and maintenance coefficients
Cell growth on acetate
Cell growth on propionate
R 4 : Growth on Acetyl-CoA
R 5 : Growth on Propionyl-CoA
R 6 : Catabolism
R 7 : Maintenance
R 9 : Acetyl-CoA* Production
R 10 : Propionyl-CoA* Production
Growth on acetyl-CoA (R4) is limited by the concentrations of acetate and ammonia.
Growth on propionyl-CoA (R5) is limited by the concentrations of propionate and ammonia.
Catabolism (R6) is limited by total VFA concentration. The kinetic equation for catabolism is only used for mixtures of acetate and propionate to fulfil the 6 fluxes required to perform MFA.
Maintenance (R7) is limited by total VFA concentration.
Acetyl-CoA* synthesis (R9) is limited by total VFA concentration and inhibited by the intracellular PHA content. Intracellular PHA inhibition has been validated experimentally by several authors [8–10, 25–27].
Propionyl-CoA* synthesis (R10) is limited by propionate concentration and inhibited by the intracellular PHA content.
In this study, two SBR for the production of PHA, were operated over four years. The sludge in each reactor was adapted to either acetate or propionate as the sole carbon source. The reactors working volume was 1 litre and the total SBR cycle duration was 12 h, consisting of 10.5 h of aerobiosis, 1 h of settling (agitation and air sparging switched off) and 0.5 h to withdraw half of the volume, which was replaced by the same volume of fresh medium during the first 15 min at the beginning of the next cycle. The hydraulic retention time (HRT) was therefore 1 day. At the end of each cycle, before settling, a defined volume of biomass was removed to keep the sludge retention time (SRT) at 10 days. Oxygen was supplied by an air compressor through a ceramic membrane disperser introduced inside the reactor at an airflow rate of 1.0 vvm (volume air/(volume reactor.min)), allowing for the dissolved oxygen (DO) concentration to be around 80% of the saturation value. The reactors were operated without pH control but its value was monitored on-line and ranged between 8.0 and 9.2; the temperature was controlled at 22°C and the stirring rate at 250 rpm.
The standard medium used in the SBRs was composed of (per litre of distilled water): 1.269 g CH3CH2COOH or 4.0796 g of CH3COONa.3H2O, 600 mg MgSO4.7H2O, 160 mg NH4Cl, 100 mg EDTA, 92 mg K2HPO4, 45 mg KH2PO4, 70 mg CaCl2.2H2O and 2 ml of trace elements solution. The trace solution consisted of (per litre of distilled water): 1500 mg FeCl3.6H2O, 150 mg H3BO3, 150 mg CoCl2.6H2O, 120 mg MnCl2.4H2O, 120 mg ZnSO4.7H2O, 60 mg Na2MoO4.2H2O, 30 mg CuSO4.5H2O and 30 mg of KI. Thiourea (10 mg/l) was added to inhibit nitrification. The pH of the salt solution was adjusted to 7.2 and then sterilized, where the phosphorus components of the solution was sterilized separately. After sterilization, the two solutions were allowed to cool, and were then mixed together.
In the batch experiments, different concentrations of acetate, propionate and ammonia were tested for the two systems and different feeding regimens were used. For the acetate reactor: the acetate concentrations tested with 1.4 N-mmol/l of ammonia were 15 C-mmol/l, 30 C-mmol/l and 60 C-mmol/l. The ammonia concentrations with 30 Cmmol/l of acetate: 0.7 N-mmol/l, 1.4 N-mmol/l and 2.8 N-mmol/l. The feeding regimen was tested by supplying multiple pulses of 60 C-mmol/l of acetate (3 tests with 3 pulses and 1 test with 4 pulses), where 0.7 N-mmol/l of ammonia was also added in the first pulse for these tests. Two more assays were performed by supplying a 30 C-mmol/l of propionate and a mixture of acetate and propionate with 15 C-mmol/l each. The batch tests performed in the propionate system analyzed the effect of different concentrations of propionate (30 C-mmol/l, 60 C-mmol/l, 90 C-mmol/l and 120 C-mmol/l) with 1.4 N-mmol/l of ammonia and the use of acetate (in one pulse of 30 C-mmol/l and mixed with propionate, 15 C-mmol/l each). In total, 18 batch tests were performed with the two systems.
Cell dry weight was determined as volatile suspended solids (VSS), according to Standard Methods . Acetate and propionate were analyzed by HPLC using a BioRad Aminex HPX-87H column, with 0.01 N sulphuric acid as eluent, an elution rate of 0.6 ml/min and an operating temperature of 50°C. A UV detector (Merck) set at 210 nm was used. Prior to injection, samples were filtered using a 0.2 μm membrane. PHA were determined by GC after acidic estherification (see [4, 11] for details). Ammonia was analyzed using an ammonia gas sensing combination electrode (ThermoOrion 9512).
with e the vector of residuals scaled by their maximum values, n the number of measurements and p the number of parameters to estimate.
The confidence bounds of the parameters were estimated by the approximation of the Hessian matrix, H, by the Jacobian matrix, J, at the minimum root mean squared error, rmse.
H = J T ·J·rmse (7)
Finally, confidence bounds, CBp, were obtained by the estimate of standard deviations for a level of confidence of 95%:
CB = diag(H)·t(1 - 0.95, n - p) (8)
with t the t-student distribution.
For the calculation of residuals, Eqs. (4a–g) were integrated using a 4th/5th order Runge-Kutta solver (MATLAB's ode45 function), with the obtained concentrations of acetate, propionate, PHB, PHV, PH2MV and oxygen subtracted from the respective measured values to give the residuals.
Metabolic Flux Analysis
Metabolic Flux Analysis (MFA) is a methodology that allows the determination of a set of unknown metabolic fluxes, v n , from a set of known fluxes, v b  by steady-state material balancing (here using Eqs. (1a–f)). In the present case, v b is composed of the modelled fluxes:
v b = [R4, R5, R6, R7, R9, R10]T
The remaining fluxes were calculated by solving the central MFA equation :
v n = -A n -1·A b ·v b
with v n the vector of unknown fluxes,
v n = [R1, R2, R3, R8, R PHB , R PHV , RPH 2MV]T
A n and A b are the corresponding stoichiometric matrices of the unknown and known fluxes respectively. Note that in this case A n is a square (7 × 7) matrix.
For single substrate feeding studies, either R1 or R2 equals zero, thus only 5 modelled
fluxes had to be included in v b , being R6 moved to v n .
Flux Balance Analysis
under the following constraints:
0 = A n ·v n + A b ·v b (12b)
0 = R PHB +R PHV + RPH 2MV- 0.76·R9 - 0.24·R10 (12c)
R4 = R5 = 0 (12d)
R7 = 0.02 (12e)
Parameters estimation results of acetate and propionate enriched cultures for the different feeding conditions
Number of experiments used for parameters estimation/model validation
P/O ratio, d (mol-ATP/mol-NADH2)
2.94 ± 0.16
1.08 ± 0.12
1.80 ± 0.19
0.94 ± 0.04
2.90 ± 0.27
1.78 ± 0.19
Maximum rates determined by metabolic model [C-mol/(C-mol.h)]
R 6, max
0.092 ± 0.017
0.094 ± 0.046
R 9, max
0.52 ± 0.03
0.13 ± 0.01
0.033 ± 0.005
0.053 ± 0.003
0.30 ± 0.03
0.18 ± 0.02
R 10 max
0.041 ± 0.004
0.052 ± 0.003
0.22 ± 0.02
0.13 ± 0.02
Maximum rates determined by MFA [C-mol/(C-mol.h)]
R 1 max
R 2 max
R 3 max
R 6 max
R 8 max
R PHB, max
R PHV, max
R PH 2MV, max
Results and discussion
Estimation of the kinetic parameters
Acetate enriched culture fed with acetate.
Acetate enriched culture fed with propionate.
Acetate enriched culture fed with mixtures of acetate and propionate.
Propionate enriched culture fed with acetate.
Propionate enriched culture fed with propionate.
Propionate enriched culture fed with mixtures of acetate and propionate.
The estimated parameter values and respective 95% confidence limits are compiled in Table 4. Note that the estimated confidence bounds are generally quite low, denoting the high sensitivity of residuals to parameters and the high statistical confidence of the estimated parameter values.
The P/O ratio is a measure of the efficiency of ATP synthesis coupled to cell respiration, indicative of the efficiency of catabolism. In acetate enriched cultures, the P/O ratio was significantly higher than in propionate enriched cultures (Table 4). Moreover, the acetate feast and famine enrichment strategy yielded an extremely energetically effective population with a P/O ratio close to the theoretical maximum, which is between 2–3 mol-ATP/mol-NADH2 in bacteria [9, 10, 31–33]. This result may suggest that the feast and famine strategy may induce not only the accumulation of intracellular reserves but also the optimization of the global energetic efficiency of the final selected culture.
The P/O ratio results in Table 4 also show that after a short term swap in substrate, the P/O ratio is highly affected. This behaviour is common to both cultures used in the present study. When propionate is the main source of energy, the P/O ratio is consistently much lower (~1 in both acetate enriched and propionate enriched cultures) than when acetate is the main source of energy (2.9 and 1.8 in acetate and propionate enriched cultures, respectively). This result is also consistent with the generally lower energetic efficiency associated with the propionate enriched culture. Interestingly, when mixtures of acetate and propionate are fed to the culture, the characteristic P/O ratio of acetate prevails over that of propionate, which suggests that catabolic activity and respiration is preferentially executed through acetate metabolism (see discussion below for more detail).
A detailed study about the P/O ratio for microbial cells using different substrates was performed by Stouthamer . In this study, a range of P/O ratios between 2.25 and 3 were found for different substrates, whereas 2.25 was the value calculated for acetate. On the other hand, Gottschalk  stated that P/O ratio may also vary with bacterial species and more specifically with the number of phospholylation sites they contain. In mixed cultures containing enrichments of polyphosphate and glycogen-accumulating organisms (PAO and GAO), different P/O ratios have been reported depending on the carbon source used for culture enrichment, namely acetate and propionate. The P/O ratio reported for acetate enriched cultures was 1.85 for PAO  and 1.73 for GAO , while in propionate enriched cultures the P/O ratio was reported as 1.37 for PAO and 1.29 for GAO . Furthermore, it was observed that the mixed microbial culture fed with acetate exhibited a significantly lower P/O ratio (1.38) at the beginning of the reactor operational period, before the acetate culture had adapted to a feast and famine regimen (data not shown). A very high P/O ratio (2.88) was also observed for a pure culture of Cupriavidus necator (formerly Ralstonia eutropha) when imposed to the feast and famine regimen for PHA production . These statements support the hypothesis that the carbon source affects the P/O ratio and the feast and famine regimen may enable the selection of bacteria with a higher P/O ratio, mainly in acetate enriched cultures.
Yields and maintenance coefficients for acetate and propionate enriched cultures for the different feeding conditions
Y X, Ac/S
Y X, Prop/S
Y PH 2MV/S
Y X, Ac/O 2
Y X, Prop/O 2
Y PHB/O 2
Y PHV/O 2
Y PH 2MV/O 2
m O 2
Metabolic flux distribution
On the other hand, if propionate is fed to both cultures, all fluxes, without exception, are higher in the propionate enriched culture when compared to the acetate culture (Figure 8b). These results confirm that the substrate used for culture enrichment is more effectively metabolized by the selected culture. However, the differences between the fluxes of both cultures in Figure (8b) are markedly lower than those of Figure (8a). In particular, the total carbon uptake and corresponding PHA storage are much higher in the acetate enriched culture fed with acetate. It seems that acetate was a much more effective substrate than propionate for selective enrichment of PHA producing cultures, leading to higher quantities of PHA stored.
The simultaneous feeding of acetate and propionate to the enriched cultures is shown in Figure 8c. Acetate and propionate are taken up at similar fluxes in each culture: 0.33 C-mol/(C-mol.h) of acetate and 0.34 C-mol/(C-mol.h) of propionate was taken up in acetate enriched cultures and 0.22 C-mol/(C-mol.h) of acetate and 0.23 C-mol/(C-mol.h) of propionate was taken up in propionate enriched cultures. The total carbon flux is 33% higher in acetate enriched cultures when compared to the propionate enriched cultures. The acetate enriched culture produced a total PHA flux of 0.52 C-mol/(C-mol.h), whereas the PHA flux in the propionate enriched culture is 0.31 C-mol/(C-mol.h) (40% lower). However, the catabolism flux, R6, is about the same in both cultures, suggesting that the percentage of carbon source spent for maintenance is higher for propionate enriched cultures due to the much lower P/O ratio in propionate enriched cultures. This is further confirmed by the higher oxidative phosphorylation flux, R8, for the propionate enriched culture.
It is also clear from Figures 8b–c that PH2MV was produced in the acetate culture and not in the propionate culture, due to the fact that acetyl-CoA* and propionyl-CoA* tended to condense randomly in the acetate culture and selectively in the propionate culture. A possible explanation for this result is that selective condensation of propionyl-CoA* with acetyl-CoA* may be a property of cells acclimatized to a propionate substrate, and that the acetate culture, which was never previously exposed to propionate, may have lacked the necessary enzymes or microbial population that is responsible for selective condensation.
Figure 8d shows a comparison of the fluxes for some of the main reactions in the two enriched cultures during the different feeding conditions. In acetate enriched cultures, the total VFA uptake capacity obtained with acetate feeding (0.73 C-mol/(C-mol.h)) was approximately equal to the sum of acetate and propionate uptake, when the substrates were fed simultaneously. Propionate enriched cultures showed a completely different behaviour. The total carbon uptake observed when both substrates were fed to this culture was approximately double that of the propionate or acetate uptake when the substrates were fed individually. A similar trend can be observed for the oxygen consumption flux and total PHA production flux, where the total flux in the propionate culture is approximately equal to the individual acetate and propionate fluxes combined, while the mixed substrate feed exhibited similar fluxes to the case of acetate feeding in the acetate culture. The mixed substrate feed had a synergistic effect on the individual metabolism of both substrates: both studied cultures were more able to take up propionate and convert it into PHA with a combined acetate/propionate feeding. This increase in VFA uptake was also observed in a culture adapted to a mixture of acetate, propionate and lactic acid . A possible explanation for this result is that the conversion of propionyl-CoA to acetyl-CoA is the rate limiting step for PHV synthesis using only propionate. The effect of this limitation on VFA uptake rate is attenuated when acetate is also fed, because the requirement of propionyl-CoA driven to acetyl-CoA is lower and more propionyl-CoA can be driven for propionyl-CoA* synthesis without losing carbon in reaction, R3.
Since the fraction of propionate per total VFA in the feed had a substantial influence on the amount of propionate uptake driven to acetyl-CoA, a relationship was established based on these two fractions, for each mixed culture under either a propionate or a mixed propionate-acetate feed (see Eq. 12f). The linear regression coefficient, r2, for this equation was found to be 0.98, based on the data presented in Table 4. It is clear that an increase in the propionate fraction fed to the mixed cultures leads to an increase in the amount of propionate converted through propionyl-CoA to acetyl-CoA. Thus, there was a higher requirement for acetyl-CoA production when the relative acetate uptake rate is lower. This supports the hypothesis discussed above, where it was proposed that energy generation through the catabolic activity of the cells are preferentially executed through acetyl-CoA.
Overall, the results from the tests with the simultaneous feeding of acetate and propionate again corroborate the hypothesis that acetate was a much more effective substrate than propionate for the selection of an optimal PHA producing culture through enrichment via the feast and famine regimen.
Flux balance analysis
From the results presented above, it is clear that acetate is a superior substrate to propionate for the enrichment of a microbial culture performing PHA production under the feast and famine regimen, due to the higher oxidative phosphorylation efficiency with this carbon source, resulting in higher PHA productivity. It is also clear that the feeding of both acetate and propionate carbon sources simultaneously resulted in either a similar or higher total PHA productivity, with a higher diversity of 3HA monomers as compared to the feeding of a single substrate. Thus, in PHA producing systems where the microbial culture enrichment and PHA production phases are separated, it is desirable to enrich the microbial culture using acetate, while feeding a combination of acetate and propionate in the PHA production phase.
Metabolic comparison of PHA production by pure and mixed cultures
Fluxes distribution for acetate and acetate + propionate feeding between mixed microbial cultures and Cupriavidus necator
Acetate + Propionate
Mixed microbial cultures (This work)
Mixed microbial cultures (This work)
Substrate uptake rate (C-mol/(C-mol.h))
VFA uptake rate
Acetate uptake rate
Propionate uptake rate
Carbon and oxygen flux distribution (%)
Carbon converted to growth
Carbon converted to CO 2
Oxygen consumed per carbon
Carbon converted to PHA
Carbon converted to Ac-CoA*
Carbon converted to Propionyl-CoA*
For the case of a Cupriavidus necator culture fed with a mixture of acetate and propionate , the VFA uptake kinetics were observed to be different from the mixed microbial cultures enriched with either acetate or propionate, despite the fact that the initial fraction of acetate and propionate were the same in all cases (50:50 on a C-mol basis). The VFA uptake rate observed in the acetate enriched culture is much higher than in pure cultures (about twofold), whereas, the propionate enriched culture has only a slightly higher VFA uptake rate as compared to the pure cultures. The PHA production fluxes were observed to be much higher for the cases of the mixed cultures (78.0 and 68.6%), as compared to the pure culture (41.2%), during the feeding of a mixture of acetate and propionate. Additionally, despite the fact that the relative propionate uptake rate is higher in pure cultures (63%) than in mixed cultures (51%), the fraction of propionyl-CoA driven to propionyl-CoA* is significantly lower (86% lower). This is due to the fact that a large portion of the propionate fed to Cupriavidus necator was first converted to acetyl-CoA prior to PHA production, unlike the mixed culture cases. This metabolic pathway causes a large loss of CO2 by the pure culture, thus lowering the PHA production efficiency. Furthermore, a large fraction of this propionyl-CoA converted to acetyl-CoA was then used for cell catabolism, contributing to the much higher carbon flux observed in the case of the pure culture as compared to the mixed cultures.
It should be noted that the carbon source used in pure culture studies [18, 37] was neither acetate nor propionate, but mixtures of yeast extract, meat extract and peptone. This could be one explanation for the inferior VFA uptake and PHA production results observed in these studies as compared to the present study, since the culture may require an adaptation period to synthesize the necessary enzymes for the metabolism of acetate and propionate carbon sources. Alternatively, it may be that the microorganisms present in the mixed cultures are more efficient PHA producers when compared to the pure cultures of Cupriavidus necator, due to the feast and famine regimen imposed. An increased VFA uptake rate was observed for a pure culture of Amaricoccus kaplicensis when the length of the famine period was increased .
• This paper presents a metabolic model of PHA copolymers production in mixed microbial cultures. The model was applied to two different cultures, obtained through two distinct enrichment protocols (selected with either acetate or propionate), under different feeding conditions (fed with either a single substrate or with mixtures of the two substrates). With this model, intracellular flux distributions for the different cases were calculated. Also, feeding scenarios were optimized by FBA targeting maximal productivity of a copolymer with a desired monomeric composition. These results were benchmarked with published results of pure cultures of Cupriavidus necator. From these studies the following main conclusions may be highlighted:
• The substrate used for culture enrichment by feast and famine feeding has a high selective pressure on the organisms that compose the final culture in the sense that the organisms selected are those that most effectively metabolize the adopted substrate.
• Sludge enrichment by acetate feeding through feast and famine regimen is much more selective towards a culture with high PHA storage fluxes and yields than when propionate is used.
• The P/O ratio is highly dependent on the substrate and the microbial culture selected. Acetate metabolism has a consistently higher P/O ratio (close to the theoretical maximum of 3 mol-ATP/mol-NADH2) than propionate metabolism.
• MFA studies suggest that when mixtures of acetate and propionate are fed to the cultures, the catabolic activity is primarily guaranteed through acetate uptake. Coherently, the acetate P/O ratio tends to prevail over that of propionate when both substrates are fed simultaneously.
• The application of FBA targeting the optimization of the PHA synthesis flux with a 24% (C-mol/C-mol) propionyl-CoA* composition revealed that acetate should be fed in excess whereas the feeding of propionate should be limited to ~0.17 C-mol/(C-mol.h). Under excess of both substrates the final propionyl-CoA* content is around 42% (C-mol/C-mol).
• By comparing metabolic fluxes between mixed and pure cultures of Cupriavidus necator it can be concluded that the PHA production process by mixed microbial cultures has the potential to be comparable or even more favourable than what is achieved by pure cultures.
• Although the metabolic characterization of mixed cultures was shown in this study to be highly favourable and promising, it should be noted that these results were obtained under ammonia limitation, thus, with conditions where cells growth is negligible. The compatibility of high cell growth rates with high PHA synthesis fluxes in mixed cultures is still not undoubtedly demonstrated in the literature.
- Acronyms :
ASM3: activated sludge model No. 3
- DO :
- FBA :
flux balance analysis
- GAO :
- 3HA :
- 3HB :
- 3H2MB :
- 3H2MV :
- 3HV :
- HRT :
hydraulic retention time
- MFA :
metabolic flux analysis
- MFD :
metabolic flux distribution
- PAO :
- PHA :
- PHB :
- PHV :
- PH2MV :
- P/O ratio :
ATP synthesis/oxygen consumption ratio
- rmse :
root mean squared error
- SBR :
sequencing batch reactor
- SRT :
sludge retention time
- TCA :
tricarboxylic acid cycle
- VFA :
volatile fatty acids
- VSS :
volatile suspended solids
- Symbols: Ac:
acetate/acetate concentration (C-mmol/l)
- f i :
intracellular PHA, PHB, PHV and PH2MV contents (C-mol/C-mol)
- K1, K2:
energy requirements for biomass synthesis (mol-ATP/C-mol)
- K S :
acetate and propionate half-saturation constants (C-mmol/l)
- K N :
ammonia half-saturation constant (N-mmol/l)
- m j :
maintenance on component j [C-mol/(C-mol.h)]
- m ATP :
maintenance coefficient on ATP [mol-ATP/(C-mol.h)]
- N :
ammonia/ammonia concentration (N-mmol/l)
- O 2 :
oxygen/oxygen concentration (mmol/l)
- Prop :
propionate/propionate concentration (C-mmol/l)
- R i :
specific rate of reaction on compound i [C-mol/(C-mol.h)]
- S :
total VFA/total VFA concentration (C-mmol/l)
- t :
culture runtime (h)
- X :
active biomass/active biomass concentration (C-mmol/l)
- y :
fraction of propionate uptake rate in the total VFA uptake rate
- Y i/j :
yield of component i on component j (C-mol/C-mol)
- α :
PHB production saturation order constant (dimensionless)
- δ :
efficiency of oxidative phosphorylation (mol-ATP/mol-NADH2).
This work was supported by Fundação para a Ciência e a Tecnologia (FCT) through the project POCI/BIO/55789/2004 and by the Integrated Project no. 026515-2: Bioproduction – Sustainable Microbial and Biocatalytic Production of Advanced Functional Materials. J. Dias, A. Oehmen and L. Serafim acknowledge FCT for grants SFRH/BD/13714/2003, SFRH/BPD/41486/2007 and SFRH/BPD/14663/2003.
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